CN114212948A - Treatment method of waste engine oil/lubricating oil regeneration distillation wastewater - Google Patents
Treatment method of waste engine oil/lubricating oil regeneration distillation wastewater Download PDFInfo
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- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/06—Nutrients for stimulating the growth of microorganisms
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
-
- 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
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention discloses a method for treating waste oil/lubricating oil regeneration distillation wastewater, belonging to the technical field of environmental protection. The method comprises the following steps: firstly, pumping the waste engine oil/lubricating oil regeneration distillation waste water into an intermittent reaction tank, adjusting the pH value to be acidic, then carrying out low-temperature evaporation by using a low-temperature evaporator, discharging the obtained concentrated solution to a solid-liquid separation device, and discharging the distilled water generated by evaporation to a distilled water collecting barrel; after solid-liquid separation is carried out on the obtained concentrated solution, discharging the filtrate into a batch reaction tank, and circularly evaporating until all the wastewater in the batch reaction tank is evaporated to be solid; adding alkali into distilled water generated by evaporation to adjust the pH value to be neutral, supplementing a nitrogen source, a phosphorus source or domestic sewage, and lifting the distilled water to an anaerobic tower for anaerobic biogas generation reaction; the effluent of the anaerobic tower enters an aerobic biological reaction tank; the effluent of the aerobic biological tank enters a secondary sedimentation tank or an MBR membrane tank for sludge-water separation; discharging the clear liquid after reaching the standard, and dewatering the sludge in a solid-liquid separation device. The treatment method has no residual mother liquor, and reduces the treatment cost.
Description
Technical Field
The invention relates to the technical field of environmental protection, in particular to a method for treating waste oil/lubricating oil regeneration distillation wastewater.
Background
With the increase of machines and vehicles, the usage amount of oil/lubricating oil is increasing. After the engine oil/lubricating oil is used for a period of time, when the lubricating and performance indexes thereof are reduced to a certain degree, the oil must be changed to ensure the normal operation of the equipment, and the change of the lubricating oil can generate a large amount of waste hydraulic oil, gear oil, dirty oil of washing parts and the like. Because the waste lubricating oil also contains a large amount of valuable lubricating oil base oil, the waste lubricating oil is recycled, which is beneficial to saving resources, changing waste into valuables, fully utilizing petroleum resources, preventing environmental pollution and having considerable economic and social benefits. At present, the regeneration process of domestic waste lubricating oil mainly comprises a distillation-acid washing-clay refining process, a distillation-furfural refining-clay refining process, a sedimentation-distillation-acid washing-calcium soil refining process and the like. When the waste lubricating oil is recycled and regenerated, the quality of the lubricating oil product is improved by the raw materials through storage tank layering, hydrofining, gas stripping, alkaline washing and other processes, and qualified high-quality lubricating oil products are obtained after refining (CN205616863U, CN211302132U, CN107312612A and CN 109758778A). In the series of regeneration processes, a small amount of high-COD, high-salt, high-ammonia nitrogen and high-total nitrogen waste liquid is generated, and the main components are chemical components such as organic sulfides, organic ammonium salts, ethers, alkoxy organic matters and the like; wherein, the COD of the waste liquid is more than or equal to 30 ten thousand mg/L, and the ammonia nitrogen is more than or equal to 5000mg/L, TDS and more than or equal to 20 percent; the waste liquid has extremely high toxicity, and the direct discharge can cause serious pollution to the environment. The waste liquid is usually treated as hazardous waste by incineration, but the waste liquid still contains a large amount of moisture, so that the incineration cost is up to thousands of yuan/ton.
The traditional treatment of waste oil regeneration distillation wastewater (high-salt, high-COD and high-ammonia nitrogen wastewater) has no high-efficiency treatment process which is better and specially aimed at the wastewater. There are mainly the following problems: 1) the conventional evaporation technology is to evaporate under a neutral condition, and ammonia nitrogen and organic nitrogen belong to volatile substances under the neutral condition, so that the ammonia nitrogen and the organic nitrogen in the wastewater are greatly transferred into distilled water, and a complex distilled water denitrification process, such as membrane concentration, a denitrification biochemical treatment reactor and the like, needs to be built; 2) traditional evaporation technologies, such as a triple-effect evaporator, an MVR evaporator and the like, can generate about 5% -15% of evaporation mother liquor (the water content is still higher than 50%), and the mother liquor contains high-concentration organic matters, so that the viscosity of the mother liquor is very high, and pipelines are easily blocked, and therefore the mother liquor is often treated as hazardous waste; 3) for waste oil regeneration distillation wastewater, fresh steam or electricity is adopted in a traditional evaporator, so that the comprehensive evaporation cost per ton of water exceeds 100 yuan. The investment and operation costs of the treatment device for the waste engine oil regeneration distillation wastewater are high due to the above problems, and the enterprise burden is large.
Patent CN111410382A discloses an adopt triple effect evaporation + tertiary RO + ozone catalysis + multistage AO + MBR's combined process, and triple effect evaporation concentrate and tertiary RO concentrate are through incineration disposal and recovery heat energy again, and this method shortcoming mainly is: 1) the investment and the operation cost are high, and the method mainly comes from triple effect evaporation, three-level RO, ozone catalysis and an incinerator; 2) the triple effect evaporation and the three-stage RO can generate more than 30% of concentrated solution; 3) because the ammonia nitrogen and the total nitrogen concentration in the original wastewater are high, the ammonia nitrogen and the total nitrogen concentration of the distilled water generated by evaporation of the triple-effect evaporator are still high, so that a complex distilled water denitrification treatment process is required; 4) the concentrated solution contains chlorine, the operation risk of the incinerator is high, the generation of dioxin needs to be avoided in the flue gas treatment, and the process is complex.
Disclosure of Invention
In order to overcome the defects in the prior art, the invention aims to provide the method for treating the waste oil/lubricating oil regeneration distillation wastewater, which has the advantages of extremely low operation cost, no generation of additional waste liquid, no generation of secondary pollutants in the whole process and stable effect.
In order to achieve the purpose, the technical scheme adopted by the invention is as follows:
a method for treating waste oil/lubricating oil regeneration distillation wastewater comprises the following steps:
(1) raw water pretreatment and evaporation:
pumping the waste engine oil/lubricating oil regeneration distillation wastewater into an intermittent reaction tank, and adding sulfuric acid to adjust the pH value of the wastewater to acidity;
(2) performing low-temperature evaporation on the wastewater of which the pH is adjusted in the step (1) in batches by using a low-temperature evaporator, discharging the obtained concentrated solution to a solid-liquid separation device for solid-liquid separation after evaporation weight loss is 70-80%, and discharging distilled water generated by evaporation of the low-temperature evaporator to a distilled water collecting barrel;
(3) carrying out solid-liquid separation on the concentrated solution obtained in the step (2), treating mud cakes, discharging filtrate to an intermittent reaction tank, and circularly carrying out the evaporation and solid-liquid separation processes in the steps (1) to (2) until all wastewater in the intermittent reaction tank is evaporated to be solid;
(4) distilled water pretreatment and anaerobic tower:
adding alkali into the distilled water evaporated in the step (2) to adjust the pH value of the distilled water to be neutral, and supplementing proper nitrogen sources, phosphorus sources and/or domestic sewage to meet the requirements of microorganisms on N, P nutrients;
(5) the distilled water with the water quality adjusted in the step (4) is lifted to an anaerobic tower to carry out anaerobic biogas production reaction; the effluent of the anaerobic tower enters an aerobic biological reaction tank; the effluent of the aerobic biological tank enters a secondary sedimentation tank or an MBR membrane tank for sludge-water separation; discharging the clear liquid after reaching the standard, and dewatering the sludge in a solid-liquid separation device.
The COD of the used oil/lubricating oil regenerative distillation wastewater is more than or equal to 30 ten thousand mg/L, the ammonia nitrogen is more than or equal to 5000mg/L, and the total nitrogen is more than or equal to 10000mg/L, TDS and more than or equal to 20 percent.
In the step (1), dilute sulfuric acid with the concentration of 15-70 wt.% is added into a batch reaction tank to adjust the pH of the wastewater to 2-5;
in the step (2), the low-temperature evaporator evaporates and reduces the weight of the wastewater, and the evaporation temperature is controlled between 40 and 75 ℃.
In the step (2), the COD of the distilled water obtained by the treatment of the low-temperature evaporation equipment is less than or equal to 5 ten thousand mg/L, the ammonia nitrogen is less than or equal to 1mg/L, and the total nitrogen is less than or equal to 5mg/L, TDS and less than or equal to 100 mg/L.
In the step (2), the solid-liquid separation device comprises a jacketed reactor, a frame-type stirrer, a solid powder dosing device and a plate-and-frame filter press, wherein the solid powder dosing device is used for adding a solid powder medicament into the concentrated solution in the reactor, and after stirring by the frame-type stirrer, solid-liquid separation treatment is carried out by the plate-and-frame filter press; the solid powder medicament is one or more of diatomite, activated carbon, activated coke and clinoptilolite.
In the step (2), the heat source of the low-temperature evaporation equipment is from the waste heat of the waste oil distillation equipment and the methane hot water boiler of the anaerobic tower.
In the step (4), the alkali for adjusting the pH to neutral is sodium carbonate or sodium bicarbonate, and the pH of the distilled water is adjusted to 7 to 9.
In the step (4), the nitrogen source is urea, and the phosphorus source is potassium dihydrogen phosphate.
In the step (5), the anaerobic tower adopts a form of effluent dilution to reduce the COD load of the anaerobic tower, and the COD of the effluent is less than or equal to 3000 mg/L.
In the step (5), the COD of the effluent of the anaerobic tower is less than or equal to 3000mg/L, the COD of the effluent of the aerobic biological tank is less than or equal to 200mg/L, and the total nitrogen is less than or equal to 15 mg/L.
The design principle and the beneficial effects of the invention are as follows:
1) the invention adopts the mode of combining the low-temperature evaporation technology, the anaerobic tower technology and the aerobic biochemical technology to treat the waste machine oil/lubricating oil regenerative distillation wastewater.
Evaporating the waste machine oil/lubricating oil regeneration distillation wastewater under an acidic condition by using low-temperature evaporation equipment (the equipment structure can refer to patent 201721247624.9), wherein ammonia nitrogen and organic nitrogen in raw water exist in the form of ammonium salt and are remained in evaporation concentrated solution or crystallized, and the ammonia nitrogen concentration and the total nitrogen concentration in distilled water are very low and are basically controlled to be below 5 mg/L;
(2) the waste heat of the waste engine oil distillation equipment and the anaerobic tower methane boiler are used as heat sources to evaporate the waste water without fresh steam or a steam compressor, so that the evaporation cost of the waste water is controlled within 10 yuan/ton, and the waste water treatment cost is greatly reduced; and (3) reducing the amount of the wastewater by 70-80% after low-temperature evaporation, returning clear liquid to low-temperature evaporation equipment for further evaporation and concentration after solid-liquid separation of concentrated solution, and performing cyclic operation until all wastewater is evaporated to be solid. Compared with the traditional evaporator, the low-temperature evaporation equipment has no residual mother liquor, and the waste liquid can be evaporated to solid by matching with a solid-liquid separation device, so that the disposal cost of the mother liquor is greatly saved;
(3) according to the invention, the wastewater is evaporated under an acidic condition, the concentration of ammonia nitrogen and total nitrogen in the distilled water is very low, a subsequent complex denitrification process route is not needed, and the investment cost is saved; only nutrient elements such as N, P and the like need to be supplemented additionally, and the domestic sewage of the plant area can be used for supplementing, so that the operation cost of the wastewater facility is reduced; the anaerobic tower is adopted to treat the COD of the distilled water, the COD can be reduced to below 3000mg/L, simultaneously the biogas is recovered and used for a hot water boiler, and the generated hot water is used for low-temperature evaporation equipment, so that the energy recovery is realized; COD of the effluent of the anaerobic tower is less than 3000mg/L, and the concentration of N, P is lower than the discharge standard of the nano-tube, so that the effluent of the anaerobic tower is treated by adopting an aerobic biological method to reduce the COD to be below 200 mg/L.
(4) In a batch reaction tank, dilute sulfuric acid with the concentration of 15-70 wt.% is added to adjust the pH of the wastewater to 2-5; the operation of using concentrated sulfuric acid in this process has safe risk, uses hydrochloric acid easily volatile and chloride ion corrosion equipment, and nitric acid easily volatile just has the risk of introducing total nitrogen in the waste water, and phosphoric acid is higher in price and has the risk of introducing total phosphorus in the waste water.
(5) In the solid-liquid separation equipment, the jacket reactor, the frame type stirrer and the solid powder dosing device are used for forming colloidal viscous high-organic matters and powdery crystalline salt in the evaporated concentrated solution into large granular solids, so that the large granular solids can be conveniently dehydrated and separated by a plate-and-frame filter press.
(6) Compared with the prior art, the method for treating the waste machine oil/lubricating oil regeneration distillation wastewater provided by the invention does not need a complex denitrification process route, is extremely low in operation cost, free of extra waste liquid, simple in operation and maintenance of process equipment, convenient and fast to operate, free of secondary pollutants in the whole process and stable in effect.
Drawings
FIG. 1 is a schematic flow chart of the method for treating waste oil/lubricating oil regeneration distillation wastewater according to the present invention.
Detailed Description
For a further understanding of the present invention, the following description is given in conjunction with the examples which are set forth to illustrate, but are not to be construed to limit the present invention, features and advantages.
Example 1:
in this example, the used oil/lubricant oil regenerated distillation wastewater is treated as shown in FIG. 1, and the COD of the used oil/lubricant oil regenerated distillation wastewater is more than or equal to 30 ten thousand mg/L, ammonia nitrogen is more than or equal to 5000mg/L, and total nitrogen is more than or equal to 10000mg/L, TDS and more than or equal to 20%. The treatment process is as follows:
(1) raw water pretreatment and evaporation:
pumping the waste oil/lubricating oil regeneration distillation wastewater into an intermittent reaction tank, and adding sulfuric acid (30 wt.%) into the intermittent reaction tank to adjust the pH of the wastewater to 2-5;
(2) wastewater enters a low-temperature evaporator in a sequencing batch mode to be evaporated at a low temperature, and a heat source of low-temperature evaporation equipment is from waste heat of waste engine oil distillation equipment and an anaerobic tower biogas hot water boiler. After evaporation weight loss is 70-80%, the evaporated distilled water is discharged to a distilled water collecting barrel; discharging the concentrated solution obtained after evaporation to a solid-liquid separation device for solid-liquid separation;
(3) treating mud cakes obtained after solid-liquid separation, returning the obtained filtrate to the batch reaction tank, adjusting the pH to 2-5, and circularly evaporating until all the wastewater in the batch reaction tank is evaporated to be solid;
(4) distilled water pretreatment and anaerobic tower:
the COD of the distilled water evaporated in the step (2) is less than or equal to 5 ten thousand mg/L, the ammonia nitrogen is less than or equal to 1mg/L, and the total nitrogen is less than or equal to 5mg/L, TDS and less than or equal to 100 mg/L. Adding sodium carbonate or sodium bicarbonate to adjust the pH value to 7-9, and supplementing proper nitrogen source urea and phosphorus source potassium dihydrogen phosphate to meet the demand of the microorganism on N, P nutrients;
(5) the distilled water with the water quality adjusted in the step (4) is lifted to an anaerobic tower to carry out anaerobic biogas production reaction; COD of the effluent of the anaerobic tower is less than or equal to 3000mg/L, and the effluent enters an aerobic biological reaction tank; the effluent of the aerobic biological tank enters a secondary sedimentation tank or an MBR membrane tank for sludge-water separation, the COD of the effluent is less than or equal to 200mg/L, and the total nitrogen is less than or equal to 15 mg/L; discharging the clear liquid after reaching the standard, and dewatering the sludge in a solid-liquid separation device.
Claims (10)
1. A treatment method of waste oil/lubricating oil regeneration distillation wastewater is characterized by comprising the following steps: the method comprises the following steps:
(1) raw water pretreatment and evaporation:
pumping the waste engine oil/lubricating oil regeneration distillation wastewater into an intermittent reaction tank, and adding sulfuric acid to adjust the pH value of the wastewater to acidity;
(2) performing low-temperature evaporation on the wastewater of which the pH is adjusted in the step (1) in batches by using a low-temperature evaporator, discharging the obtained concentrated solution to a solid-liquid separation device for solid-liquid separation after evaporation weight loss is 70-80%, and discharging distilled water generated by evaporation of the low-temperature evaporator to a distilled water collecting barrel;
(3) carrying out solid-liquid separation on the concentrated solution obtained in the step (2), treating mud cakes, discharging filtrate to an intermittent reaction tank, and circularly carrying out the evaporation and solid-liquid separation processes in the steps (1) to (2) until all wastewater in the intermittent reaction tank is evaporated to be solid;
(4) distilled water pretreatment and anaerobic tower:
adding alkali into the distilled water evaporated in the step (2) to adjust the pH value of the distilled water to be neutral, and supplementing proper nitrogen sources, phosphorus sources and/or domestic sewage to meet the requirements of microorganisms on N, P nutrients;
(5) the distilled water with the water quality adjusted in the step (4) is lifted to an anaerobic tower to carry out anaerobic biogas production reaction; the effluent of the anaerobic tower enters an aerobic biological reaction tank; the effluent of the aerobic biological tank enters a secondary sedimentation tank or an MBR membrane tank for sludge-water separation; discharging the clear liquid after reaching the standard, and dewatering the sludge in a solid-liquid separation device.
2. The method for treating the used oil/lubricant oil regenerative distillation wastewater according to claim 1, wherein: the COD of the used oil/lubricating oil regenerative distillation wastewater is more than or equal to 30 ten thousand mg/L, the ammonia nitrogen is more than or equal to 5000mg/L, and the total nitrogen is more than or equal to 10000mg/L, TDS and more than or equal to 20 percent.
3. The method for treating the used oil/lubricant oil regenerative distillation wastewater according to claim 1, wherein: in the step (1), dilute sulfuric acid with the concentration of 15-70 wt.% is added into a batch reaction tank to adjust the pH of the wastewater to 2-5.
4. The method for treating the used oil/lubricant oil regenerative distillation wastewater according to claim 1, wherein: in the step (2), the low-temperature evaporator evaporates and reduces the weight of the wastewater, and the evaporation temperature is controlled between 40 and 75 ℃.
5. The method for treating the used oil/lubricant oil regenerative distillation wastewater according to claim 1, wherein: in the step (2), the solid-liquid separation device comprises a jacketed reactor, a frame type stirrer, a solid powder dosing device and a plate-and-frame filter press, wherein a solid powder dosing device is adopted to add a solid powder medicament into the concentrated solution in the reactor, and after the concentrated solution is stirred by the frame type stirrer, the solid-liquid separation treatment is carried out by the plate-and-frame filter press; the solid powder medicament is one or more of diatomite, activated carbon, activated coke and clinoptilolite.
6. The method for treating the used oil/lubricant oil regenerative distillation wastewater according to claim 1, wherein: in the step (2), the heat source of the low-temperature evaporation equipment is from waste heat of waste oil distillation equipment and a biogas hot water boiler of an anaerobic tower.
7. The method for treating the used oil/lubricant oil regenerative distillation wastewater according to claim 1, wherein: in the step (2), the COD of the distilled water obtained by the treatment of the low-temperature evaporation equipment is less than or equal to 5 ten thousand mg/L, the ammonia nitrogen is less than or equal to 1mg/L, and the total nitrogen is less than or equal to 5mg/L, TDS and less than or equal to 100 mg/L.
8. The method for treating the used oil/lubricant oil regenerative distillation wastewater according to claim 1, wherein: in the step (4), the alkali for adjusting the pH to neutral is sodium carbonate or sodium bicarbonate, and the pH of the distilled water is adjusted to 7-9.
9. The method for treating the used oil/lubricant oil regenerative distillation wastewater according to claim 1, wherein: in the step (4), the nitrogen source is urea, and the phosphorus source is potassium dihydrogen phosphate.
10. The method for treating the used oil/lubricant oil regenerative distillation wastewater according to claim 1, wherein: in the step (5), the COD of the effluent of the anaerobic tower is less than or equal to 3000mg/L, the COD of the effluent of the aerobic biological tank is less than or equal to 200mg/L, and the total nitrogen is less than or equal to 15 mg/L.
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