CN113105937A - Waste mineral oil treatment system and treatment method - Google Patents
Waste mineral oil treatment system and treatment method Download PDFInfo
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- CN113105937A CN113105937A CN202110402719.8A CN202110402719A CN113105937A CN 113105937 A CN113105937 A CN 113105937A CN 202110402719 A CN202110402719 A CN 202110402719A CN 113105937 A CN113105937 A CN 113105937A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
- C10M175/0033—Working-up used lubricants to recover useful products ; Cleaning by thermal processes using distillation processes; devices therefor
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/02—Working-up used lubricants to recover useful products ; Cleaning mineral-oil based
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
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Abstract
The invention provides a system and a method for treating waste mineral oil. The treatment system comprises a pretreatment device, a reduced pressure rectification device, a base oil adjusting device, N extraction devices, N flash evaporation devices and a gas stripping device, wherein the pretreatment device obtains pretreated waste mineral oil; carrying out vacuum rectification treatment on the pretreated waste mineral oil by using a vacuum rectification device; the base oil adjusting device is connected with N lateral line outlets of the vacuum rectification device and is prepared to obtain N base oils; the extraction devices are connected with the base oil adjusting devices in a one-to-one correspondence manner, and N groups of extraction phases and raffinate phases are obtained through extraction treatment; the flash evaporation device is connected with each extraction device in a one-to-one correspondence manner, and flash evaporation treatment is carried out to obtain corresponding tower bottom oil; the gas stripping device is connected with each flash evaporation device in a one-to-one correspondence manner, and gas stripping treatment is carried out to obtain corresponding mineral oil at the bottom of each tower, wherein N is more than or equal to 3. The treatment system of the waste mineral oil can greatly simplify pretreatment equipment, reduce cost and avoid secondary pollution.
Description
Technical Field
The invention relates to the technical field of waste mineral oil treatment, in particular to a waste mineral oil treatment system and a waste mineral oil treatment method.
Background
The mineral oil is a mixture obtained by refining petroleum, specifically crude oil, which is subjected to atmospheric and vacuum fractionation, solvent extraction and dewaxing, and hydrorefining to obtain mineral oil containing C as main component15～C36And alkanes, Polycyclic Aromatic Hydrocarbons (PAHs), alkenes, benzenes, phenols, and the like. The method is widely applied to various industries of national economy, and is mainly used for mechanical equipment, power devices, transportation equipment, electrical equipment, metal processing industry and the like of industrial and mining enterprises. The waste mineral oil is mainly used as waste lubricating oil, engine oil, hydraulic oil, transformer oil, antirust oil, solvent oil and the like after the equipment is replaced, and used lubricating oil, waste engine oil and the like after transportation tools (automobiles, trains, ships and aircrafts) are used for replacement. The original physical and chemical properties are changed due to the external factors such as impurity pollution, oxidation or thermal decomposition in the processing and using processes, and the product can not be used continuously. And the waste mineral oil contains various toxic substances and has certain harm to human health. Once a large amount of the fertilizer enters the environment, the fertilizer can pollute water and soil and affect the living environment of animals, plants and human beings.
Mineral oil is used as a chemical product, is refined by a complex process, and has high use cost. In fact, the deteriorated portion of the waste mineral oil may be present in a smaller proportion and still have a higher recycling value. Therefore, the waste mineral oil is refined and purified by adopting a proper process to meet the requirement of reuse, the pollution of the waste mineral oil to the environment can be effectively reduced, the resources can be saved, and the method has good economic benefit and environmental benefit.
At present, the refining process of the waste mineral oil mainly comprises 1) distillation-acid cleaning-clay process, and has the defects of generating a large amount of waste acid, waste water, waste gas and waste residue, so that the secondary pollution is serious, and the post-treatment cost is increased; 2) the distillation-hydrogenation process has the main defects that the waste mineral oil contains more impurities, the catalyst is easy to deactivate, the quality requirement on the waste mineral oil is higher, and the hydrogenation process has higher requirements on safety and operation; 3) the distillation-solvent refining process has the main defects that the quality of the traditional distillation-solvent refining product is low, the volatility is high, and unqualified products are easy to generate; in addition, the waste mineral oil has wide sources and complex components, and a large amount of unqualified products are easy to generate, so that the production continuity is poor and the vehicles are frequently stopped. At the same time, the lack of recovery process of the extractant further results in the production of large amounts of hazardous waste; 4) the membrane separation process has the main defects that the viscosity of the waste lubricating oil is high, a filtering membrane is easy to block, the processing capacity of the membrane separation method is low, and the large-scale production is difficult particularly.
Disclosure of Invention
The invention mainly aims to provide a waste mineral oil treatment system and a waste mineral oil treatment method, and aims to solve the problems of poor universality, serious pollution and high cost of a waste mineral oil treatment process in the prior art.
In order to achieve the above object, according to one aspect of the present invention, a waste mineral oil treatment system is provided, the treatment system includes a pretreatment device, a vacuum rectification device, a base oil adjusting device, N extraction devices, N flash evaporation devices, and a gas stripping device, the pretreatment device is configured to perform preliminary solid impurity removal treatment and dehydration treatment on waste mineral oil to obtain pretreated waste mineral oil; the vacuum rectification device is directly connected with the pretreatment device through a pipeline and is used for carrying out vacuum rectification treatment on the pretreated waste mineral oil, and the vacuum rectification device is provided with N side line outlets; the base oil adjusting device is connected with N side outlets of the vacuum rectification device, and N base oils are obtained by blending N side oil products of the vacuum rectification device; the extraction devices are connected with the base oil adjusting devices in a one-to-one correspondence manner and are used for respectively and independently carrying out extraction treatment on each base oil to obtain N groups of extraction phases and raffinate phases; the flash evaporation device is connected with each extraction device in a one-to-one correspondence manner and is used for independently carrying out flash evaporation treatment on each raffinate phase to obtain corresponding bottom oil of each tower; the gas stripping device is connected with each flash evaporation device in a one-to-one correspondence manner and is used for carrying out gas stripping treatment on the bottom oil of each tower respectively and independently to obtain corresponding bottom mineral oil of each tower, wherein N is more than or equal to 3.
Further, the vacuum rectification device comprises a heater and a vacuum rectification tower, wherein the heater is connected with the pretreatment device and is used for heating the pretreated waste mineral oil to obtain heated waste mineral oil; the vacuum rectification tower is connected with the heater and is used for carrying out vacuum rectification treatment on the heated waste mineral oil, and the N lateral line outlets are arranged on the vacuum rectification tower.
Further, the pretreatment device comprises an impurity removal processor and a dehydration tower, wherein the impurity removal processor is used for carrying out primary solid impurity removal treatment on the waste mineral oil to obtain liquid after impurity removal; the dehydration tower is connected with an outlet of the impurity removal processor and used for dehydrating the liquid after impurity removal, pretreated waste mineral oil is obtained at the bottom of the tower, and optionally, a first preheater is arranged on a pipeline between the impurity removal processor and the dehydration tower and connected with at least one side line outlet of the reduced pressure rectification device to use side line produced oil of the at least one side line outlet as a heat source.
Further, the base oil adjusting device comprises N preparation tanks connected with each side outlet, and the side outlet of each side outlet is prepared according to a preset proportion to obtain each base oil with different viscosity specifications, preferably, each preparation tank is provided with an online viscosity monitoring device for detecting the viscosity value of each base oil, the online viscosity monitoring device is in electric signal connection with a vacuum rectification tower, the vacuum rectification tower adjusts the temperature and reflux ratio of vacuum rectification treatment according to the viscosity value, optionally, the base oil adjusting device further comprises N buffer tanks connected with each side outlet in a one-to-one correspondence manner, the buffer tanks are arranged at the upstream of each preparation tank, and any one preparation tank is selectively connected with the outlet of each buffer tank.
Further, each extraction device comprises an M-level centrifugal extractor which is connected with the base oil adjusting device and is used for carrying out M-level extraction treatment on each base oil to obtain an extract phase and a raffinate phase, wherein M is more than or equal to 3 and less than or equal to 6; optionally, the extraction device further comprises a solvent recovery tower connected with the last centrifugal extractor of each M-stage centrifugal extractor to obtain the tower top solvent and the tower bottom heavy oil.
Further, each of the above flash evaporation apparatuses includes a flash evaporation tower connected to each of the extraction apparatuses in a one-to-one correspondence manner for performing flash evaporation treatment on the raffinate phase to obtain bottom oil and top steam, and optionally, a second preheater is provided on a pipeline between the flash evaporation apparatus and the M-stage centrifugal extractor, and the second preheater is connected to at least one side outlet of the vacuum rectification apparatus to use side product oil of the at least one side outlet as a heat source.
Further, each gas stripping device comprises a gas stripping tower which is connected with each flash evaporation device in a one-to-one correspondence manner and is used for carrying out gas stripping treatment on the tower bottom oil to obtain corresponding tower bottom mineral oil and tower top gas; preferably, the stripping apparatus further comprises a nitrogen source connected to the bottom inlet of the stripper column.
Furthermore, the processing system also comprises a refining device, wherein the refining device comprises N refiners, is connected with the gas stripping device and is used for further refining and removing impurities from the mineral oil at the bottom of the tower; preferably, the refining apparatus further comprises a source of clay connected in one-to-one correspondence with the inlet of each refiner.
According to another aspect of the present application, there is provided a method of treating waste mineral oil, the method comprising: step S1, performing primary solid impurity removal treatment and dehydration treatment on the waste mineral oil to obtain pretreated waste mineral oil; step S2, carrying out vacuum rectification treatment on the pretreated waste mineral oil to obtain N kinds of side-stream produced oil; step S3, blending the side oil to obtain N base oils; step S4, extracting each base oil to obtain N groups of extract phases and raffinate phases; step S5, carrying out flash evaporation treatment on each raffinate phase to obtain corresponding bottom oil of each tower; and step S6, carrying out gas stripping treatment on the bottom oil to obtain corresponding bottom mineral oil, wherein N is more than or equal to 3.
Further, the step S1 includes: carrying out primary solid impurity removal treatment on the waste mineral oil to obtain liquid after impurity removal; dehydrating the liquid after impurity removal to obtain pretreated waste mineral oil; preferably, before the dehydration treatment, at least one side-stream produced oil is used as a heat source to carry out first preheating treatment on the liquid after impurity removal to obtain preheated liquid, the temperature of the preheated liquid is preferably 80-90 ℃, the water content of the pretreated waste mineral oil is preferably 0.5-1%, and the preliminary solid impurity removal treatment is preferably filtration.
Further, the step S2 includes: heating the pretreated waste mineral oil to obtain heated waste mineral oil; and (3) carrying out vacuum rectification treatment on the heated waste mineral oil to obtain N kinds of side-stream produced oil, wherein the temperature of the heated waste mineral oil is preferably 340-370 ℃.
Further, in the step S3, during the blending process, the temperature and reflux ratio of the vacuum distillation process are feedback-adjusted according to the viscosity test value of each base oil, and when N is 3 is further preferred, the N types of side-stream produced oil include a first side-stream produced oil, a second side-stream produced oil, and a third side-stream produced oil, the base oil includes a first base oil, a second base oil, and a third base oil, the reflux ratio of the vacuum distillation process is 3-3.5: 1, the temperature of the first side-stream produced oil is 175-200 ℃, the temperature of the second side-stream produced oil is 250-270 ℃, and the temperature of the third side-stream produced oil is 295-305 ℃; preferably when the viscosity of the first base oil is < 45mm2(s) viscosity of the second base oil is less than 29mm2S and the viscosity of the third base oil is less than 17mm2When the pressure is in the range of 4-5: 1, preferably adjusting the reflux ratio of the vacuum rectification treatment, and preferably adjusting the temperature of the vacuum rectification treatment to enable the temperature of the oil produced by the first side line, the temperature of the oil produced by the second side line and the temperature of the oil produced by the third side line to rise by 5-10 ℃ respectively and independently; preferably, buffering treatment is carried out on the oil output from each side line to obtain N types of buffered oil; and blending the oil subjected to the buffer treatment to obtain N kinds of base oil.
Further, in step S4, performing M-stage extraction on each base oil to obtain N groups of extract phases and raffinate phases; preferably, each extraction phase is subjected to solvent recovery treatment to obtain an overhead solvent and bottom heavy oil, preferably, the extractant in the M-stage extraction treatment is selected from any one or more of N-methylpyrrolidone, butane, N-dimethylformamide, furfural and N-butanol, and the volume ratio of each base oil to the extractant is preferably 1: 0.5-3, preferably the temperature of each stage of extraction treatment is 50-70 ℃, wherein M is more than or equal to 3.
Further, the step S5 includes: carrying out second preheating treatment on the raffinate phase to obtain a preheated phase; carrying out flash evaporation treatment on the preheated phase to obtain tower bottom oil and tower top steam; preferably, at least one side-stream oil is used as a heat source to carry out second preheating treatment on the raffinate phase, and the temperature of the preheated phase is preferably 130-150 ℃.
Further, the gas stripping treatment is carried out in a nitrogen atmosphere, and optionally, after the temperature of the mineral oil at the bottom of each tower is reduced to 60-80 ℃, clay is used for refining and removing impurities of the mineral oil at the bottom of each tower.
By applying the technical scheme of the invention, the pretreated waste mineral oil is obtained by carrying out preliminary solid impurity removal treatment and dehydration treatment on the waste mineral oil in the pretreatment device, namely the pretreated waste mineral oil can be directly subjected to vacuum rectification treatment in the vacuum rectification device, then N types of side-stream produced oil in the vacuum rectification device are blended through the base oil adjusting device to obtain N types of base oil, and then the N types of base oil are respectively and independently subjected to extraction treatment in the extraction device to remove impurities such as aromatic hydrocarbon, cyclane, colloid, asphaltene and the like in the N types of side-stream produced oil, so that the raffinate phase with a large amount of impurities removed is obtained. And (3) further carrying out flash evaporation treatment and gas stripping treatment on the raffinate phase in a flash evaporation device and a gas stripping device respectively, and removing an extracting agent in the raffinate phase so as to obtain the tower bottom mineral oil with higher purity. The processing system of the waste mineral oil can greatly simplify the pretreatment equipment of the waste mineral oil, and the processing system does not need to introduce additional reagents except the extracting agent, thereby reducing the cost and avoiding secondary pollution, and the processing system is almost suitable for processing all the waste mineral oil. Meanwhile, the treatment system for treating the waste mineral oil can effectively reduce the pollution of the waste mineral oil to the environment, save resources and have good economic benefit and environmental benefit.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:
fig. 1 shows a system diagram for treating waste mineral oil provided in example 1 of the present invention.
Wherein the figures include the following reference numerals:
1. a pretreatment device; 2. a vacuum rectification device; 3. a base oil conditioning device; 4. an extraction device; 5. a flash evaporation device; 6. a gas stripping device; 7. a refining device; 11. an impurity removal processor; 12. a dehydration tower; 21. a heater; 22. a reduced pressure rectifying tower; 31. preparing a tank; 32. a buffer tank; 41. an M-grade centrifugal extractor; 42. a solvent recovery column; 51. a flash column; 61. a stripper column; 71. a refining device.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
As analyzed by the background art, the problems of poor universality, serious pollution and high cost of the treatment process of the waste mineral oil in the prior art are solved, and the invention provides a treatment system and a treatment method of the waste mineral oil.
In an exemplary embodiment of the present application, a processing system of waste mineral oil is provided, as shown in fig. 1, the processing system includes a pretreatment device 1, a vacuum rectification device 2, a base oil adjusting device 3, N extraction devices 4, N flash evaporation devices 5, and a gas stripping device 6, the pretreatment device 1 is configured to perform preliminary solid impurity removal treatment and dehydration treatment on the waste mineral oil to obtain pretreated waste mineral oil; the vacuum rectification device 2 is directly connected with the pretreatment device 1 through a pipeline and is used for carrying out vacuum rectification treatment on the pretreated waste mineral oil, and the vacuum rectification device 2 is provided with N side line outlets; the base oil adjusting device 3 is connected with N side outlets of the vacuum rectification device 2, and N base oils are obtained by blending N side oil products of the vacuum rectification device 2; the extraction devices 4 are connected with the base oil adjusting devices 3 in a one-to-one correspondence manner and are used for respectively and independently carrying out extraction treatment on each base oil to obtain N groups of extraction phases and raffinate phases; the flash evaporation device 5 is connected with each extraction device 4 in a one-to-one correspondence manner and is used for independently carrying out flash evaporation treatment on each raffinate phase to obtain corresponding bottom oil of each tower; the gas stripping device 6 is connected with each flash evaporation device 5 in a one-to-one correspondence manner and is used for carrying out gas stripping treatment on each tower bottom oil independently to obtain corresponding tower bottom mineral oil, wherein N is more than or equal to 3.
The method comprises the steps of carrying out preliminary solid impurity removal treatment on waste mineral oil in a pretreatment device 1, carrying out dehydration treatment on the obtained pretreated waste mineral oil, namely directly carrying out vacuum rectification treatment on the pretreated waste mineral oil in a vacuum rectification device 2, then blending N types of side-stream produced oil in the vacuum rectification device 2 through a base oil adjusting device 3 to obtain N types of base oil, and then respectively and independently carrying out extraction treatment on the N types of base oil in an extraction device 4 to remove impurities such as aromatic hydrocarbon, cycloparaffin, colloid, asphaltene and the like in the N types of side-stream produced oil so as to obtain a raffinate phase with a large amount of impurities removed. And (3) further carrying out flash evaporation treatment and stripping treatment on the raffinate phase in a flash evaporation device 5 and a stripping device 6 respectively, and removing an extracting agent in the raffinate phase so as to obtain the tower bottom mineral oil with higher purity. The processing system of the waste mineral oil can greatly simplify the pretreatment equipment of the waste mineral oil, and the processing system does not need to introduce additional reagents except the extracting agent, thereby reducing the cost and avoiding secondary pollution, and the processing system is almost suitable for processing all the waste mineral oil. Meanwhile, the treatment system for treating the waste mineral oil can effectively reduce the pollution of the waste mineral oil to the environment, save resources and have good economic benefit and environmental benefit.
In an embodiment of the present application, as shown in fig. 1, the vacuum rectification apparatus 2 includes a heater 21 and a vacuum rectification tower 22, the heater 21 is connected to the pretreatment apparatus 1, and is configured to heat the pretreated waste mineral oil to obtain a heated waste mineral oil; the vacuum rectification tower 22 is connected with the heater 21 and is used for carrying out vacuum rectification treatment on the heated waste mineral oil, and N lateral line outlets are arranged on the vacuum rectification tower 22.
The heater 21 connected with the pretreatment device 1 can directly heat the pretreated waste mineral oil, then the heated waste mineral oil is subjected to vacuum rectification treatment in the vacuum rectification tower 22 connected with the heater 21, and N side-stream produced oil with different components is obtained through N side-stream outlets on the vacuum rectification tower 22, so that the vacuum rectification device 2 can separate the waste mineral oil as far as possible from the source.
When the vacuum rectification tower 22 is used, structured packing is filled in the tower, heat conduction oil is used as a heat carrier, N lateral line outlets are arranged on the tower body according to different distillation ranges of materials, light fuel oil is separated from the top of the tower and enters a light oil tank, the N lateral line outlets respectively refine lateral line output oil raw materials with different physical properties, heavy components at the bottom of the tower extract residual oil, and the residual oil enters a residual oil tank.
In an embodiment of the present application, as shown in fig. 1, the pretreatment apparatus 1 includes an impurity removal processor 11 and a dehydration tower 12, where the impurity removal processor 11 is configured to perform a preliminary solid impurity removal process on the waste mineral oil to obtain an impurity-removed liquid; the dehydration tower 12 is connected with an outlet of the impurity removal processor 11 and is used for dehydrating the liquid after impurity removal, pretreated waste mineral oil is obtained at the bottom of the tower, and optionally, a first preheater is arranged on a pipeline between the impurity removal processor 11 and the dehydration tower 12 and is connected with at least one side outlet of the vacuum rectification device 2 to use side outlet oil of at least one side outlet as a heat source.
Above-mentioned preprocessing device 1 can carry out abundant edulcoration, dehydration to waste mineral oil as far as, obtains the waste mineral oil after the higher preliminary treatment of purity, avoids causing the damage to processing system. The first preheater is provided with a selective heating device for heating the liquid after impurity removal, so that the dehydration treatment is more sufficiently assisted, the side-line produced oil of at least one side-line outlet is used as a heat source, the waste heat of the side-line produced oil can be fully utilized, the energy consumption is further reduced, and the cost is reduced.
In an embodiment of the present application, as shown in fig. 1, the above-mentioned base oil adjusting device 3 includes N preparation tanks 31 connected to each side outlet, and the side outlet of each side outlet is prepared according to a predetermined ratio to obtain each base oil with different viscosity specifications, preferably, each preparation tank 31 is provided with an online viscosity monitoring device for detecting a viscosity value of each base oil, the online viscosity monitoring device is electrically connected to the vacuum rectification tower 22, the vacuum rectification tower 22 adjusts a temperature and a reflux ratio of the vacuum rectification process according to the viscosity value, optionally, the base oil adjusting device 3 further includes N buffer tanks 32 connected to each side outlet in a one-to-one correspondence manner, the buffer tanks 32 are disposed upstream of each preparation tank 31, and any one preparation tank 31 is selectively connected to an outlet of each buffer tank 32.
In the N preparation tanks 31 of the base oil adjusting device 3, the N types of side-stream produced oil obtained after the vacuum rectification treatment can be directly prepared on line to obtain the base oil with different viscosity specifications. The on-line viscosity monitoring device provided on each of the preparation tanks 31 can better monitor the viscosity value of each base oil to ensure that each base oil of a predetermined viscosity specification is obtained. And the temperature and reflux ratio of the vacuum rectification treatment can be further adjusted in the vacuum rectification tower 22 through the electric signal connection of the online viscosity monitoring device and the vacuum rectification tower 22, so that the viscosity value of the side-line produced oil is controlled from the source, and further the base oil can be obtained more favorably. The base oil adjusting device 3 comprises N buffer tanks 32 which can buffer the flowing side-stream produced oil so as to keep the viscosity thereof within a certain range as much as possible, thereby facilitating the viscosity adjustment of the side-stream produced oil in each preparation tank 31 to obtain each base oil meeting the requirements. Of course, the buffer tank 32 in the art can also be a buffer device that is conventional in the art and can buffer the fluid, and will not be described in detail herein.
In addition, when the oil produced from each side line is used as a heat source, the oil enters the buffer tank 32 for buffering after heat exchange.
In order to further improve the purity of each base oil, as shown in fig. 1, each extraction device 4 preferably comprises an M-stage centrifugal extractor 41 connected with the base oil adjusting device 3, and is used for performing M-stage extraction treatment on each base oil to obtain an extract phase and a raffinate phase, wherein M is greater than or equal to 3 and less than or equal to 6; optionally, the extraction device 4 further comprises a solvent recovery tower 42 connected to the last centrifugal extractor of each M-stage centrifugal extractor 41 to obtain an overhead solvent and a bottom heavy oil. As M increases, it is more advantageous to remove impurities from the base oil, and preferably 3. ltoreq. M.ltoreq.6 for cost reasons. The solvent recovery column 42 of the extraction unit 4 facilitates recovery of the solvent while simultaneously obtaining a heavy oil by-product, thereby further reducing costs and reducing environmental pressure. The solvent recovery column 42 heats it by means of heat transfer oil.
In an embodiment of the present application, as shown in fig. 1, each of the above-mentioned flash evaporation apparatuses 5 comprises a flash evaporation tower 51 connected to each of the extraction apparatuses 4 in a one-to-one correspondence manner for performing a flash evaporation treatment on the raffinate phase to obtain a bottom oil and an overhead vapor, and optionally, a second preheater is provided in a pipeline between the flash evaporation apparatus 5 and the M-stage centrifugal extractor 41, and is connected to at least one side outlet of the vacuum distillation apparatus 2 to use a side product oil of the at least one side outlet as a heat source.
The flash evaporation devices 5 connected to the extraction devices 4 in a one-to-one correspondence may perform flash evaporation treatment on the raffinate phase to remove the solvent remaining in the raffinate phase and improve the purity thereof. The second preheater and the waste heat of the side-line produced oil can be fully utilized by taking the side-line produced oil as a heat source, so that the special heat source in the flash evaporation treatment is avoided, and the energy consumption is reduced.
For further removing the residual solvent in the bottom oil, as shown in fig. 1, preferably, each of the stripping devices 6 includes a stripping tower 61 connected to each of the flashing devices 5 in a one-to-one correspondence manner for stripping the bottom oil to obtain each of the corresponding bottom mineral oil and the corresponding top gas; preferably, the stripping apparatus 6 further comprises a nitrogen source connected to the bottom inlet of the stripper column 61. The nitrogen is used for reducing the gas phase partial pressure of the extracting agent, so that the aim of regenerating the solvent is fulfilled, and the possibility is provided for removing and recovering the residual extracting agent in the tower bottom oil.
Optionally, in order to meet the requirement of higher purity of the bottom mineral oil, as shown in fig. 1, it is preferable that the processing system further comprises a refining device 7, and the refining device 7 comprises N refiners 71 connected to the stripping device 6 for further refining and impurity removal of the bottom mineral oil; preferably, the refining apparatus 7 further comprises a source of clay connected in one-to-one correspondence with the inlet of each refiner 71. The clay can adsorb a small amount of heavy components, solvents and other impurities in the tower bottom mineral oil to achieve the purpose of improving the purity of the tower bottom mineral oil. Of course, if the purity of the mineral oil at the bottom of the tower is up to the requirement, the mineral oil does not need to be refined and purified.
In another exemplary embodiment of the present application, there is provided a method for treating waste mineral oil, the method comprising: step S1, performing primary solid impurity removal treatment and dehydration treatment on the waste mineral oil to obtain pretreated waste mineral oil; step S2, carrying out vacuum rectification treatment on the pretreated waste mineral oil to obtain N kinds of side-stream produced oil; step S3, blending the side oil to obtain N base oils; step S4, extracting each base oil to obtain N groups of extract phases and raffinate phases; step S5, carrying out flash evaporation treatment on each raffinate phase to obtain corresponding bottom oil of each tower; and step S6, carrying out gas stripping treatment on the bottom oil to obtain corresponding bottom mineral oil, wherein N is more than or equal to 3.
The method comprises the steps of carrying out preliminary solid impurity removal treatment on waste mineral oil, dewatering the waste mineral oil to obtain pretreated waste mineral oil, directly carrying out vacuum rectification treatment on the pretreated waste mineral oil, then blending N kinds of side-line produced oil to obtain N kinds of base oil, and then carrying out extraction treatment on the N kinds of base oil respectively and independently to remove impurities such as aromatic hydrocarbon, cyclane, colloid, asphaltene and the like in the N kinds of side-line produced oil to obtain a raffinate phase with a large amount of impurities removed. And (3) respectively carrying out flash evaporation treatment and gas stripping treatment on the raffinate phase to remove the extractant in the raffinate phase, thereby obtaining the tower bottom mineral oil with higher purity. The treatment method does not need to introduce additional reagents, thereby reducing the cost and avoiding secondary pollution, and the treatment method is almost suitable for treating all waste mineral oil. Meanwhile, the treatment method for the waste mineral oil can effectively reduce the pollution of the waste mineral oil to the environment, save resources and have good economic benefit and environmental protection advantage.
In order to increase the purity of the pretreated waste mineral oil as much as possible so as to perform the vacuum distillation treatment, it is preferable that the step S1 includes: carrying out primary solid impurity removal treatment on the waste mineral oil to obtain liquid after impurity removal; dehydrating the liquid after impurity removal to obtain pretreated waste mineral oil; preferably, before the dehydration treatment, at least one side-stream produced oil is used as a heat source to carry out first preheating treatment on the liquid after impurity removal to obtain preheated liquid, the temperature of the preheated liquid is preferably 80-90 ℃, the water content of the pretreated waste mineral oil is preferably 0.5-1%, and the preliminary solid impurity removal treatment is preferably filtration. The temperature of the preheated liquid is preferably 80-90 ℃, which is beneficial to improving the fluidity of the preheated liquid, so that the preheated liquid is beneficial to entering a dehydration treatment stage and the evaporation of water in the liquid, and the efficiency of dehydration treatment is improved. The pretreated waste mineral oil with the water content is beneficial to improving the efficiency of the vacuum rectification treatment. The liquid after impurity removal is subjected to first preheating treatment by taking at least one side-line produced oil as a heat source to obtain the preheated liquid, so that the energy consumption can be further reduced, and the cost is reduced.
In an embodiment of the present application, the step S2 includes: heating the pretreated waste mineral oil to obtain heated waste mineral oil; and (3) carrying out vacuum rectification treatment on the heated waste mineral oil to obtain N kinds of side-stream produced oil, wherein the temperature of the heated waste mineral oil is preferably 340-370 ℃.
The heated waste mineral oil at the temperature is beneficial to full vacuum rectification treatment, so that N kinds of side-stream produced oil are obtained.
In order to obtain base oil meeting the viscosity specification, preferably in step S3, during blending, the temperature and reflux ratio of the vacuum rectification treatment are feedback-adjusted according to the viscosity test value of each base oil, and further preferably when N is 3, the N types of side-stream produced oil include first side-stream produced oil, second side-stream produced oil, and third side-stream produced oil, the base oil includes first base oil, second base oil, and third base oil, the reflux ratio of the vacuum rectification treatment is preferably 3-3.5: 1, the temperature of the first side-stream produced oil is preferably 175-200 ℃, the temperature of the second side-stream produced oil is preferably 250-270 ℃, and the temperature of the third side-stream produced oil is preferably 295-305 ℃; preferably when the viscosity of the first base oil is < 45mm2/s、The viscosity of the second base oil is less than 29mm2S and the viscosity of the third base oil is less than 17mm2When the pressure is in the range of 4-5: 1, preferably adjusting the reflux ratio of the vacuum rectification treatment, and preferably adjusting the temperature of the vacuum rectification treatment to enable the temperature of the oil produced by the first side line, the temperature of the oil produced by the second side line and the temperature of the oil produced by the third side line to rise by 5-10 ℃ respectively and independently; preferably, buffering treatment is carried out on the oil output from each side line to obtain N types of buffered oil; and blending the oil subjected to the buffer treatment to obtain N kinds of base oil. The buffering treatment is beneficial to stabilizing the viscosity of the oil produced at each side line as much as possible, and the viscosity value of each base oil is better tested and the base oil is allocated, so that the temperature and reflux ratio of the vacuum distillation treatment are more accurately fed back and adjusted, and the base oil meeting the requirements is obtained.
In an embodiment of the present application, in step S4, performing M-stage extraction treatment on each base oil to obtain N groups of extract phases and raffinate phases; preferably, each extraction phase is subjected to solvent recovery treatment to obtain an overhead solvent and bottom heavy oil, preferably, the extractant in the M-stage extraction treatment is selected from any one or more of N-methylpyrrolidone, butane, N-dimethylformamide, furfural and N-butanol, and the volume ratio of each base oil to the extractant is preferably 1: 0.5-3, preferably the temperature of each stage of extraction treatment is 50-70 ℃, wherein M is more than or equal to 3.
The solvent recovery treatment of each extraction phase is beneficial to improving the recovery rate of the extraction phase, reducing the cost and improving the environmental protection. In order to further improve the extraction efficiency, the above-mentioned extraction agent and extraction conditions are preferred.
In order to effectively reduce the residual rate of the solvent in the raffinate phase, the step S5 preferably includes: carrying out second preheating treatment on the raffinate phase to obtain a preheated phase; carrying out flash evaporation treatment on the preheated phase to obtain tower bottom oil and tower top steam; preferably, at least one side-stream oil is used as a heat source to carry out second preheating treatment on the raffinate phase, and the temperature of the preheated phase is preferably 130-150 ℃.
The preheated phase at the temperature is beneficial to improving the efficiency of flash evaporation treatment, and the oil produced by at least one side line is taken as a heat source, so that the energy consumption is reduced, and the cost is reduced.
In order to improve the effect of solvent removal in the gas stripping treatment, the gas stripping treatment is preferably performed in a nitrogen atmosphere, and optionally, after the temperature of the mineral oil at the bottom of each tower is reduced to 60-80 ℃, the mineral oil at the bottom of each tower is refined and subjected to impurity removal by using argil.
The nitrogen is utilized to reduce the gas phase partial pressure of the extracting agent, thereby achieving the aim of solvent regeneration, and facilitating the removal and recovery of the residual extracting agent in the tower bottom oil. The aim of improving the purity of the mineral oil at the tower bottom is achieved by adopting clay to adsorb a small amount of heavy components, solvents and other impurities in the mineral oil at the tower bottom. Of course, if the purity of the mineral oil at the bottom of the tower is up to the requirement, the mineral oil does not need to be refined and purified.
The following description will explain advantageous effects of the present application with reference to specific examples.
Example 1
Referring to the processing system diagram of the waste mineral oil shown in fig. 1, firstly, the waste mineral oil raw materials (waste engine oil, waste gear oil, waste hydraulic oil, waste lubricating oil, etc. generated in the motor vehicle maintenance, enterprise production and operation processes) are filtered in an impurity removal processor 11 to remove large-particle impurities in the waste mineral oil raw materials, and a liquid after impurity removal is obtained. And then pumping the liquid after impurity removal into a raw material tank for storage and carrying out steam tracing on the liquid, ensuring that the liquid in the raw material tank after impurity removal is maintained at about 30 ℃, and keeping the liquidity of the liquid after impurity removal.
The liquid in the raw material tank after impurity removal exchanges heat with the first side line produced material of the vacuum rectification tower 22 through the tubular heat exchanger, so that the temperature of the liquid after impurity removal rises to 80-90 ℃, and then the liquid enters the dehydration tower 12, the temperature of the tower kettle is maintained at 110 ℃ through steam heating of the dehydration tower 12, water is separated from the top of the tower by utilizing the difference of oil and water boiling points, and the condensed liquid goes to a wastewater treatment device. The pretreated waste mineral oil at the bottom of the tower is sent to a tubular heating furnace 21 for heating, the heating furnace 21 is heated by natural gas, and waste gas and non-condensed steam generated in the production link are led to the heating furnace for burning. Heating the pretreated waste mineral oil to 370 ℃ to obtain heated waste mineral oil, introducing the heated waste mineral oil into a vacuum rectification tower 22 for vacuum rectification, wherein the reflux ratio of the vacuum rectification is 3:1, the vacuum degree of the tower top is-50 to-90 KPa, the temperature of the tower top is controlled to be 120 to 140 ℃, three side line extraction ports are arranged on the tower top, light component media can be instantly gasified by utilizing different oil components with different boiling points, wherein light fuel oil is separated from the tower top, is condensed by a condenser on the tower top, is collected by a buffer tank on the tower top, is sent to a light oil tank for storage and can be used as fuel oil, and three side lines are respectively separated to obtain first side line produced oil (180 ℃), second side line produced oil (250 ℃) and third side line produced oil (300 ℃).
The oil produced by the first side line, the oil produced by the second side line and the oil produced by the third side line are respectively collected by a buffer tank 32 to obtain three types of buffered oil, the three types of buffered oil are respectively sent to a preparation tank 31, an online viscosity monitoring device is arranged on the preparation tank 31 and is in electric signal connection with a reduced pressure rectifying tower 22, and first base oil, second base oil and third base oil are obtained in each preparation tank 31. When the viscosity of the first base oil is less than 45mm2(s) viscosity of the second base oil is less than 29mm2S and the viscosity of the third base oil is less than 17mm2When the pressure is in the range of 4:1, the reflux ratio of the vacuum distillation treatment is adjusted to be 4:1, and the temperature of the vacuum distillation treatment is adjusted to ensure that the first side line produces oil (190 ℃), the second side line produces oil (260 ℃) and the third side line produces oil (310 ℃).
Unqualified products generated in the startup and shutdown and process adjustment processes are sent to a crude oil tank and treated in the vacuum rectification device 2 again, and the heavy components at the bottom of the rectification tower are sent to the residual oil tank to be sold as residual oil.
And respectively carrying out three-stage extraction treatment on the first base oil, the second base oil and the third base oil in three-stage centrifugal extractors to obtain an extract phase and a raffinate phase, wherein the last-stage centrifugal extractor of each three-stage centrifugal extractor is connected with a solvent recovery tower 42 to obtain a tower top solvent and tower bottom heavy oil. Each flash column 51 performs flash evaporation treatment on the raffinate phase to obtain bottom oil and top steam. And a second preheater which takes the oil produced by the second side line as a heat source is arranged on the pipeline between the flash device 5 and the three-stage centrifugal extractor.
And (3) carrying out gas stripping treatment on the bottom oil in a gas stripping tower 61 in nitrogen atmosphere to obtain 75SN, 150SN and 250SN corresponding bottom mineral oil and top gas.
From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects:
according to the method, the pre-treated waste mineral oil is obtained by performing primary impurity removal treatment and dehydration treatment on the waste mineral oil in the pre-treatment device, namely the pre-treated waste mineral oil can be directly subjected to vacuum rectification treatment in the vacuum rectification device, then N types of side-stream produced oil in the vacuum rectification device are blended through the base oil adjusting device to obtain N types of base oil, and then the N types of base oil are respectively and independently subjected to extraction treatment in the extraction device to remove impurities such as aromatic hydrocarbon, cyclane, colloid, asphaltene and the like in the N types of side-stream produced oil, so that a raffinate phase with a large amount of impurities removed is obtained. And (3) further carrying out flash evaporation treatment and gas stripping treatment on the raffinate phase in a flash evaporation device and a gas stripping device respectively, and removing an extracting agent in the raffinate phase so as to obtain the tower bottom mineral oil with higher purity. The processing system of the waste mineral oil can greatly simplify the pretreatment equipment of the waste mineral oil, and the processing system does not need to introduce additional reagents except the extracting agent, thereby reducing the cost and avoiding secondary pollution, and the processing system is almost suitable for processing all the waste mineral oil. Meanwhile, the treatment system for treating the waste mineral oil can effectively reduce the pollution of the waste mineral oil to the environment, save resources and have good economic benefit and environmental benefit.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (15)
1. A waste mineral oil processing system, comprising:
the pretreatment device (1) is used for carrying out preliminary solid impurity removal treatment and dehydration treatment on the waste mineral oil to obtain pretreated waste mineral oil;
the vacuum rectification device (2) is directly connected with the pretreatment device (1) through a pipeline and is used for carrying out vacuum rectification treatment on the pretreated waste mineral oil, and the vacuum rectification device (2) is provided with N side line outlets;
the base oil adjusting device (3) is connected with N side outlets of the vacuum rectification device (2) and is used for blending N types of base oil by using N types of side outlet oil of the vacuum rectification device (2);
the N extraction devices (4) are connected with the base oil adjusting devices (3) in a one-to-one correspondence manner and are used for respectively and independently carrying out extraction treatment on each base oil to obtain N groups of extraction phases and raffinate phases;
n flash evaporation devices (5) which are connected with the extraction devices (4) in a one-to-one correspondence manner and are used for independently carrying out flash evaporation treatment on the raffinate phases to obtain corresponding tower bottom oil; and
and the gas stripping devices (6) are connected with the flash evaporation devices (5) in a one-to-one correspondence manner and are used for performing gas stripping treatment on the bottom oil of each tower respectively and independently to obtain corresponding bottom mineral oil of each tower, wherein N is more than or equal to 3.
2. The processing system according to claim 1, wherein the vacuum rectification apparatus (2) comprises:
the heater (21) is connected with the pretreatment device (1) and is used for heating the pretreated waste mineral oil to obtain heated waste mineral oil;
and the vacuum rectification tower (22) is connected with the heater (21) and is used for carrying out vacuum rectification on the heated waste mineral oil, and the N lateral line outlets are arranged on the vacuum rectification tower (22).
3. The treatment system according to claim 1, wherein the pre-treatment device (1) comprises:
the impurity removal processor (11) is used for carrying out primary solid impurity removal processing on the waste mineral oil to obtain impurity-removed liquid;
and the dehydrating tower (12) is connected with an outlet of the impurity removal processor (11) and is used for dehydrating the liquid after impurity removal, and the pretreated waste mineral oil is obtained at the bottom of the tower, optionally, a first preheater is arranged on a pipeline between the impurity removal processor (11) and the dehydrating tower (12), and the first preheater is connected with at least one side outlet of the vacuum rectification device (2) to use the side-stream produced oil adopting at least one side outlet as a heat source.
4. The treatment system according to claim 2, wherein the base oil conditioning device (3) comprises:
n preparation tanks (31) connected with the side outlets, and used for performing the preparation on the side output oil of the side outlets according to a preset proportion to obtain the base oil with different viscosity specifications,
preferably, each preparation tank (31) is provided with an online viscosity monitoring device for detecting the viscosity value of each base oil, the online viscosity monitoring device is in electric signal connection with the vacuum rectification tower (22), the vacuum rectification tower (22) adjusts the temperature and reflux ratio of the vacuum rectification treatment according to the viscosity value,
optionally, the base oil adjusting device (3) further comprises N buffer tanks (32) connected with the side outlets in a one-to-one correspondence manner, the buffer tanks (32) are arranged at the upstream of the preparation tanks (31), and any one of the preparation tanks (31) is selectively connected with the outlet of each buffer tank (32).
5. The treatment system according to claim 1, wherein each of said extraction devices (4) comprises:
the M-level centrifugal extractor (41) is connected with the base oil adjusting device (3) and is used for carrying out M-level extraction treatment on each base oil to obtain the extract phase and the raffinate phase, wherein M is more than or equal to 3 and less than or equal to 6;
optionally, the extraction device (4) further comprises a solvent recovery tower (42) connected with the last centrifugal extractor of each M-stage centrifugal extractor (41) to obtain an overhead solvent and a bottom heavy oil.
6. The treatment system according to claim 5, wherein each of said flash evaporation devices (5) comprises:
flash towers (51) which are connected with the extraction devices (4) in a one-to-one correspondence manner and are used for carrying out flash processing on the raffinate phase to obtain the tower bottom oil and the tower top steam,
optionally, a second preheater is arranged on a pipeline between the flash distillation device (5) and the M-stage centrifugal extractor (41), and the second preheater is connected with at least one side outlet of the vacuum rectification device (2) to use the side product oil of the at least one side outlet as a heat source.
7. The treatment system according to claim 1, wherein each of said stripping devices (6) comprises:
the gas stripping tower (61) is connected with each flash evaporation device (5) in a one-to-one correspondence manner and is used for carrying out gas stripping treatment on the tower bottom oil to obtain corresponding tower bottom mineral oil and tower top gas;
preferably, the stripping device (6) further comprises a nitrogen source connected to the bottom inlet of the stripping column (61).
8. The treatment system according to claim 1, further comprising a refining device (7), the refining device (7) comprising:
n refiners (71) connected with the stripping device (6) and used for further refining and removing impurities from the tower bottom mineral oil;
preferably, the refining apparatus (7) further comprises a clay source connected in one-to-one correspondence with an inlet of each of the refiners (71).
9. A method for treating waste mineral oil, comprising:
step S1, performing primary solid impurity removal treatment and dehydration treatment on the waste mineral oil to obtain pretreated waste mineral oil;
step S2, carrying out vacuum rectification treatment on the pretreated waste mineral oil to obtain N kinds of side-stream produced oil;
step S3, blending the side oil to obtain N base oils;
step S4, extracting each base oil to obtain N groups of extract phases and raffinate phases;
step S5, carrying out flash evaporation treatment on each raffinate phase to obtain corresponding bottom oil of each tower; and
and step S6, performing gas stripping treatment on the tower bottom oil to obtain corresponding tower bottom mineral oil, wherein N is more than or equal to 3.
10. The processing method according to claim 9, wherein the step S1 includes:
carrying out the preliminary solid impurity removal treatment on the waste mineral oil to obtain impurity-removed liquid;
carrying out dehydration treatment on the liquid after impurity removal to obtain the pretreated waste mineral oil;
preferably, before the dehydration treatment, at least one side-stream produced oil is used as a heat source to carry out first preheating treatment on the liquid after impurity removal to obtain preheated liquid, preferably, the temperature of the preheated liquid is 80-90 ℃, preferably, the water content of the pretreated waste mineral oil is 0.5-1%, and preferably, the preliminary solid impurity removal treatment is filtration.
11. The processing method according to claim 9, wherein the step S2 includes:
heating the pretreated waste mineral oil to obtain heated waste mineral oil;
carrying out the vacuum rectification treatment on the heated waste mineral oil to obtain the N kinds of side-stream produced oil,
preferably, the temperature of the heated waste mineral oil is 340-370 ℃.
12. The processing method according to claim 9, wherein, in the step S3,
in the blending process, the temperature and reflux ratio of the vacuum rectification treatment are adjusted in a feedback mode through the viscosity test value of each base oil, and when N is preferably 3, the N types of side-line produced oil comprise first side-line produced oil, second side-line produced oil and third side-line produced oil, the base oil comprises first base oil, second base oil and third base oil, the reflux ratio of the vacuum rectification treatment is preferably 3-3.5: 1, the temperature of the first side-line produced oil is preferably 175-200 ℃, the temperature of the second side-line produced oil is preferably 250-270 ℃, and the temperature of the third side-line produced oil is preferably 295-305 ℃;
preferably when the viscosity of the first base oil is < 45mm2(s) the viscosity of the second base oil is less than 29mm2S and the viscosity of the third base oil is less than 17mm2When the pressure is in the range of 4-5: 1, preferably adjusting the reflux ratio of the vacuum rectification treatment, and preferably adjusting the temperature of the vacuum rectification treatment to enable the temperature of the first side line produced oil, the temperature of the second side line produced oil and the temperature of the third side line produced oil to be respectively and independently increased by 5-10 ℃;
preferably, buffering each side-stream output oil to obtain N types of buffered oil;
and blending the buffered oils to obtain the N types of base oil.
13. The processing method according to claim 9, wherein, in the step S4,
performing M-level extraction treatment on each base oil to obtain N groups of extract phases and raffinate phases;
preferably, each extraction phase is subjected to solvent recovery treatment to obtain a tower top solvent and tower bottom heavy oil,
preferably, the extractant in the M-stage extraction treatment is selected from any one or more of N-methylpyrrolidone, butane, N-dimethylformamide, furfural and N-butanol, and the volume ratio of each base oil to the extractant is 1: 0.5-3, preferably the temperature of each stage of extraction treatment is 50-70 ℃, wherein M is more than or equal to 3.
14. The processing method according to claim 9, wherein the step S5 includes:
carrying out second preheating treatment on the raffinate phase to obtain a preheated phase;
carrying out flash evaporation treatment on the preheated phase to obtain tower bottom oil and tower top steam;
preferably, at least one side-stream oil is used as a heat source to carry out the second preheating treatment on the raffinate phase, and the temperature of the preheated phase is preferably 130-150 ℃.
15. The treatment method according to claim 9, wherein the gas stripping treatment is performed in a nitrogen atmosphere, and optionally, after the temperature of the mineral oil at the bottom of each tower is reduced to 60-80 ℃, clay is used for refining and impurity removal of the mineral oil at the bottom of each tower.
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