CN115109614A - Anti-coking and anti-pinch belt process method for waste mineral oil regenerated base oil - Google Patents
Anti-coking and anti-pinch belt process method for waste mineral oil regenerated base oil Download PDFInfo
- Publication number
- CN115109614A CN115109614A CN202110309724.4A CN202110309724A CN115109614A CN 115109614 A CN115109614 A CN 115109614A CN 202110309724 A CN202110309724 A CN 202110309724A CN 115109614 A CN115109614 A CN 115109614A
- Authority
- CN
- China
- Prior art keywords
- oil
- unit
- line
- enters
- solvent
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000002199 base oil Substances 0.000 title claims abstract description 34
- 239000002699 waste material Substances 0.000 title claims abstract description 28
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000002480 mineral oil Substances 0.000 title claims abstract description 20
- 235000010446 mineral oil Nutrition 0.000 title claims abstract description 20
- 238000004939 coking Methods 0.000 title claims abstract description 13
- 239000003921 oil Substances 0.000 claims abstract description 85
- 239000002904 solvent Substances 0.000 claims abstract description 29
- 238000002309 gasification Methods 0.000 claims abstract description 14
- 238000010438 heat treatment Methods 0.000 claims abstract description 14
- 238000004821 distillation Methods 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims abstract description 8
- 238000003763 carbonization Methods 0.000 claims abstract description 6
- 230000018044 dehydration Effects 0.000 claims abstract description 6
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 6
- 238000004519 manufacturing process Methods 0.000 claims abstract description 6
- 238000011084 recovery Methods 0.000 claims abstract description 6
- 239000003513 alkali Substances 0.000 claims abstract description 5
- 238000002156 mixing Methods 0.000 claims abstract description 5
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 3
- 238000000638 solvent extraction Methods 0.000 claims abstract description 3
- 238000000926 separation method Methods 0.000 claims description 27
- 238000005086 pumping Methods 0.000 claims description 15
- 238000003860 storage Methods 0.000 claims description 15
- 238000001816 cooling Methods 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 5
- 230000008020 evaporation Effects 0.000 claims description 5
- 239000000295 fuel oil Substances 0.000 claims description 5
- 238000004064 recycling Methods 0.000 claims description 4
- 239000000243 solution Substances 0.000 claims description 4
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 3
- 239000006229 carbon black Substances 0.000 claims description 3
- 239000010724 circulating oil Substances 0.000 claims description 3
- 230000003647 oxidation Effects 0.000 claims description 3
- 238000007254 oxidation reaction Methods 0.000 claims description 3
- 239000012047 saturated solution Substances 0.000 claims description 3
- 230000003068 static effect Effects 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 2
- 238000002485 combustion reaction Methods 0.000 claims description 2
- 239000010913 used oil Substances 0.000 claims 1
- 239000010705 motor oil Substances 0.000 abstract description 9
- 238000009835 boiling Methods 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000000463 material Substances 0.000 abstract 1
- 239000010687 lubricating oil Substances 0.000 description 8
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000010408 film Substances 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 230000007547 defect Effects 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000010409 thin film Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000007859 condensation product Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
- C10G2300/1007—Used oils
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a process method for preventing coking and preventing belt clamping of waste mineral oil regenerated base oil, which comprises the following steps: (1) an alkali solution neutralization waste engine oil mixing unit; (2) a waste mineral oil heating vacuum dehydration unit; (3) the O-shaped tube furnace-normal pressure kettle high-speed circulating heating system provides a heat unit for the three-line-reduction high-vacuum cyclone gasification distillation unit; (4) a light component oil removing unit; (5) a second-line-reduced vacuum cyclone gasification distillation unit; (6) a three-line-reducing high vacuum cyclone gasification distillation unit; (7) a residue carbonization unit; (8) a base oil solvent extraction unit; (9) an extract oil solvent recovery unit; (10) a refined liquid raffinate oil recovery unit; (11) a non-condensable gas processing unit. The waste engine oil of the invention circulates at low temperature and high speed, completely avoids the problems of equipment coking and high boiling point materials carried by oil gas, has no secondary pollution, is green and environment-friendly, reduces energy consumption, has high oil yield, less equipment investment and safe and reliable production.
Description
Technical Field
The invention relates to the field of waste mineral oil regeneration treatment technology and waste mineral oil solvent refining regenerated lubricating oil base oil technology, in particular to a waste mineral oil regenerated base oil anti-coking and anti-pinch belt process method.
Background
When the lubricating oil contacts with the air and the metal surface in the using process, the lubricating oil is at a local high temperature or a certain temperature condition, the water content of the lubricating oil is increased, the lubricating oil is degraded at a high temperature, oil products are oxidized to generate polar substances, such as acid, aldehyde, ketone and condensation products, which are dissolved in the oil to corrode the metal friction surface, and the polar substances are deposited after the solubility of the lubricating oil is gradually saturated or the temperature is reduced to form oil sludge, so that the viscosity of the lubricating oil is increased, the friction coefficient is increased, and the use instruction of machine equipment is greatly influenced. Therefore, lubricating oil needs to be replaced regularly, the existing technology for improving the replaced waste oil has some defects and process defects, the production temperature (maximum 320 ℃) is insufficient by adopting heat conduction oil to heat in the regeneration process of the existing waste mineral oil, and the heating of a tubular furnace can generate a local overheating cracking phenomenon to cause technical process problems of equipment system coking, entrainment and the like in the regeneration and utilization process of the waste mineral oil.
Disclosure of Invention
The invention aims to provide an anti-coking and anti-pinch process method for regenerating base oil from waste mineral oil, which adopts a falling film rectification process, recovers different distillate oil in distillation units with different temperatures, and separates oxide, colloid and aromatic hydrocarbon components through solvent refining to prepare II-type base oil reaching the standard, can completely eliminate the problems of equipment coking and oil gas entrainment of high-boiling residues, has no secondary pollution, is green and environment-friendly, reduces energy consumption, has high oil yield, less equipment investment, and is safe and reliable in production.
In order to solve the technical problems, the invention adopts the following technical scheme:
the invention provides a process method for preventing coking and preventing belt clamping of waste mineral oil regenerated base oil, which is characterized by comprising the following specific steps of:
(1) an alkali solution neutralization waste engine oil mixing unit: waste mineral oil enters a prestoring tank, is added with 0.3 to 0.5 percent alkali saturated solution and is uniformly stirred, enters a second-reduction and third-reduction oil-gas separation tank condenser for convective heat exchange, and enters a pressure reduction dehydration unit;
(2) waste mineral oil heating vacuum dehydration unit: entering a condenser of an oil-gas separation tank for reducing two and three for heat convection, controlling the temperature at 150 ℃, performing vacuum flash evaporation gasification to pull out water in oil, and pumping the oil into a tubular furnace for normal-pressure high-speed circulation heating of an atmospheric and vacuum unit;
(3) the O-shaped tube furnace-normal pressure kettle high-speed circulating heating system provides heat for the three-line reduction high-vacuum cyclone gasification distillation unit; the dehydrated waste mineral oil is circularly heated at a high speed by a tubular furnace and a normal-pressure reaction kettle, and the temperature is controlled at 350 ℃;
(4) light component oil removing unit: normal-pressure reduction high-temperature circulating oil is heated to 350 ℃, the oil enters a first-line reduction cyclone oil-gas separation tank for flash evaporation gasification separation of light component oil, the vacuum degree is controlled at 50KPa, and the heavy component oil enters a second-line reduction oil-gas separation unit;
(5) two-line-reduced high-vacuum cyclone gasification distillation unit: heavy component oil of the first-line-reduced cyclone oil-gas separation tank enters the second-line-reduced cyclone oil-gas separation tank, the vacuum degree is controlled to be 2KPa, the second-line base oil component is separated out and enters a second-line-reduced oil receiving tank for temporary storage, and the heavy component oil enters a third-line-reduced oil-gas separation unit;
(6) three-line-reducing high-vacuum cyclone gasification distillation unit: separating heavy component oil after two-line oil reduction, feeding the heavy component oil into a three-line cyclone oil-gas separation tank, circularly heating the bottom of the tank and an atmospheric kettle, controlling the vacuum degree below 500Pa, separating out three-line base oil components, feeding the three-line base oil components into a three-line oil reduction receiving tank for temporary storage, and feeding the heavy residual oil into a residual oil receiving tank for temporary storage;
(7) residual oil carbonization unit: the heavy component residual oil enters a high-temperature rotary furnace, the temperature is controlled at 450 ℃ for carbonization, the produced fuel oil is cooled and then enters a fuel oil prestoring tank, and the carbon black is subjected to harmless treatment;
(8) a base oil solvent extraction unit: reducing two, respectively carrying out ozone oxidation on the three-line base oil, then feeding the three-line base oil into a heat exchanger for convective heat exchange, controlling the temperature to be 70 ℃, feeding the three-line base oil into a static mixer for mixing with a solvent, then feeding the mixture into a disk centrifuge for centrifugal separation, and respectively obtaining refined liquid raffinate oil and extract oil, wherein the temperature of the solvent is controlled to be 60 ℃;
(9) an extract oil solvent recovery unit: pumping the extract oil into an evaporator, gasifying and drawing out a light component as a solvent, cooling and then feeding the solvent into a receiving tank, pumping the rest heavy component into a film evaporator, controlling the temperature at 150 ℃, gasifying and drawing out a small amount of the light component solvent, cooling and then feeding the solvent into the receiving tank, pumping the heavy component as extract oil into a storage tank through a pump;
(10) refined liquid raffinate oil recovery unit: pumping the refined liquid into a double-effect film evaporator to gasify and pull out light components as a solvent, controlling the temperature at 130 ℃, cooling the solvent, then feeding the cooled solvent into a receiving tank, pumping the rest components as base oil into a storage tank for storage, and recycling the recovered solvent for recycling;
(11) a noncondensable gas treatment unit: the non-condensable gas generated in the production process enters a combustion chamber for incineration through a water seal.
The invention has the beneficial effects that: the waste engine oil circulates at a low temperature and a high speed, the problems of equipment coking and oil gas carrying high-boiling residues are completely solved, secondary pollution is avoided, the environment is protected, the energy consumption is reduced, the oil yield is high, the equipment investment is low, and the production is safe and reliable.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a flow chart of the process method for preventing coking and preventing belt clamping of the waste mineral oil regenerated base oil provided by the invention.
Detailed Description
The technical solutions of the present invention will be described clearly and completely in the following embodiments of the present invention, and it should be understood that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
As shown in figure 1, the anti-coking and anti-pinch process method for the waste mineral oil regenerated base oil comprises the following specific steps:
(1) pumping 10 tons of used engine oil and 0.03 ton of potassium hydroxide saturated solution into a used engine oil stirring tank and uniformly stirring;
(2) heating the waste engine oil to 150 ℃, entering a cyclone flash tower for vacuum dehydration and light oil, wherein the vacuum degree is 100pa, and obtaining 9.9 tons of anhydrous pretreatment waste engine oil; 0.1 ton of water;
(3) pumping the anhydrous waste engine oil into an O-shaped tube furnace-normal pressure kettle heating system to circularly heat to 350 ℃ at a high speed (3.3m/s), and providing heat for a three-way reducing distillation unit;
(4) the normal-pressure and high-temperature circulating oil is heated to 350 ℃, enters a first-line reduction cyclone oil-gas separation tank for flash evaporation, gasification and separation of light component oil, the vacuum degree is controlled to be 50KPa, and the heavy component oil enters a second-line reduction oil-gas separation unit; separating light component oil by 0.4 ton;
(5) heavy component oil in the first-line-reduced cyclone oil-gas separation tank enters the second-line-reduced cyclone oil-gas separation tank, the vacuum degree is controlled to be 2KPa, the two-line base oil component is separated out and enters the second-line-reduced oil receiving tank for temporary storage, 6 tons of SN150 component oil are separated, and the heavy component oil enters the third-line-reduced oil-gas separation unit;
(6) separating heavy component oil after two-line oil reduction, feeding the heavy component oil into a three-line reduction cyclone oil-gas separation tank, circularly heating the bottom of the tank and a normal pressure kettle, controlling the vacuum degree at 300Pa, separating out three-line base oil components, feeding the three-line reduction cyclone oil-gas separation tank for temporary storage, and feeding the heavy residual oil into a residual oil receiving tank for temporary storage; 2 tons of component oil with SN above 250 and 1.5 tons of tower bottom oil are separated;
(7) pumping the tower bottom oil into a rotary kiln for carbonization treatment to produce 1.1 ton of fuel oil and 0.3 ton of carbon black, controlling the temperature to be 450 ℃, and controlling the quantity of non-condensable gas to be 0.1 ton;
(8) respectively carrying out ozone oxidation on the three-line base oil, then feeding the base oil into a heat exchanger for heat convection, feeding the base oil into a static mixer for mixing with a solvent, then feeding the mixture into a disc centrifuge for three-stage convection extraction, and respectively obtaining refined liquid raffinate oil and extract oil to separate extract oil and raffinate oil; the agent-oil ratio is 1:1, the temperature of a heat exchanger is controlled at 70 ℃, and the solvent is NMP;
(9) the extract oil passes through a reboiler, and the solvent and the bottom oil of the tower are recovered by a film evaporator by 0.48 ton; controlling the temperature to be 150 ℃;
(10) 7.52 tons of base oil and solvent are recovered from raffinate oil by a double-effect thin film evaporator, the temperature is controlled to be 130 ℃, a vacuum pump is utilized to vacuumize a distillation system of the thin film evaporator, the vacuum degree is 300pa, and the solvent is recycled.
It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (1)
1. The anti-coking and anti-pinch belt-preventing process method for the regenerated base oil of the waste mineral oil is characterized by comprising the following specific steps of:
(1) alkali solution neutralization used oil mixing unit: waste mineral oil enters a prestoring tank, is added with 0.3 to 0.5 percent alkali saturated solution and is uniformly stirred, enters a second-reduction and third-reduction oil-gas separation tank condenser for convective heat exchange, and enters a pressure reduction dehydration unit;
(2) waste mineral oil heating vacuum dehydration unit: entering a condenser of an oil-gas separation tank for reducing two and three for heat convection, controlling the temperature at 150 ℃, performing vacuum flash evaporation gasification to pull out water in oil, and pumping the oil into a tubular furnace for normal-pressure high-speed circulation heating of an atmospheric and vacuum unit;
(3) the O-shaped tube furnace-normal pressure kettle high-speed circulating heating system provides a heat unit for the three-line-reduction high-vacuum cyclone gasification distillation unit; the dehydrated waste mineral oil is circularly heated at a high speed by a tubular furnace and a normal-pressure reaction kettle, and the temperature is controlled at 350 ℃;
(4) a light component oil removing unit: the normal-pressure and high-temperature circulating oil is heated to 350 ℃, enters a first-line reduction cyclone oil-gas separation tank for flash evaporation, gasification and separation of light component oil, the vacuum degree is controlled to be 50KPa, and the heavy component oil enters a second-line reduction oil-gas separation unit;
(5) a second-line reduction vacuum cyclone gasification distillation unit: the first-line-reduced heavy component oil enters a first-line-reduced cyclone oil-gas separation tank, the vacuum degree is controlled to be 2KPa, the second-line base oil component is separated out and enters a second-line-reduced oil receiving tank for temporary storage, and the heavy component oil enters a third-line-reduced oil-gas separation unit;
(6) three-line-reducing high-vacuum cyclone gasification distillation unit: separating heavy component oil after two-line oil reduction, feeding the heavy component oil into a three-line cyclone oil-gas separation tank, circularly heating the bottom of the tank and an atmospheric kettle, controlling the vacuum degree below 500Pa, separating out three-line base oil components, feeding the three-line base oil components into a three-line oil reduction receiving tank for temporary storage, and feeding the heavy residual oil into a residual oil receiving tank for temporary storage;
(7) residual oil carbonization unit: the heavy component residual oil enters a high-temperature rotary furnace, the temperature is controlled at 450 ℃ for carbonization, the produced fuel oil is cooled and then enters a fuel oil prestoring tank, and the carbon black is subjected to harmless treatment;
(8) a base oil solvent extraction unit: reducing two, after ozone oxidation, the three-line base oil enters a heat exchanger for convective heat exchange, the temperature is controlled at 70 ℃, the three-line base oil enters a static mixer to be mixed with a solvent, the temperature of the solvent is controlled at 60 ℃, and then the three-line base oil enters a disc centrifuge for centrifugal separation to respectively obtain refined liquid raffinate oil and extract oil;
(9) an extract oil solvent recovery unit: pumping the extract oil into an evaporator, gasifying and drawing out a light component as a solvent, cooling and then feeding the solvent into a receiving tank, pumping the rest heavy component into a film evaporator, controlling the temperature at 150 ℃, gasifying and drawing out a small amount of the light component solvent, cooling and then feeding the solvent into the receiving tank, cooling the heavy component into extract oil, and pumping the extract oil into a storage tank by a pump;
(10) a refined liquid raffinate oil recovery unit: pumping the refined liquid into a double-effect film evaporator, gasifying and drawing out light components as a solvent, controlling the temperature at 130 ℃, cooling and then feeding the solvent into a receiving tank, pumping the rest components as base oil into a storage tank for storage through a pump, and recycling the solvent for recycling;
(11) a noncondensable gas treatment unit: the non-condensable gas generated in the production process enters a combustion chamber for incineration through a water seal.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110309724.4A CN115109614B (en) | 2021-03-23 | 2021-03-23 | Process method for coking and entrainment prevention of waste mineral oil regenerated base oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110309724.4A CN115109614B (en) | 2021-03-23 | 2021-03-23 | Process method for coking and entrainment prevention of waste mineral oil regenerated base oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115109614A true CN115109614A (en) | 2022-09-27 |
| CN115109614B CN115109614B (en) | 2023-11-17 |
Family
ID=83324181
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110309724.4A Active CN115109614B (en) | 2021-03-23 | 2021-03-23 | Process method for coking and entrainment prevention of waste mineral oil regenerated base oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115109614B (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ES2199697A1 (en) * | 2003-09-23 | 2004-02-16 | Sener Grupo De Ingenieria Sa | Method for regenerating used oils by demetallization and distillation |
| CA2783608A1 (en) * | 2012-07-23 | 2014-01-23 | Lucie Wheeler | Environmental process to transform contaminated or uncontaminated feed materials into useful products, uses of the process, products thereby obtained and uses thereof, manufacturing of the corresponding plant |
| CN107312568A (en) * | 2017-06-27 | 2017-11-03 | 爱润森德（天津）能源科技有限公司 | A kind of waste mineral oil catalytic pyrolysis utilization system and its processing technology |
| CN108203594A (en) * | 2018-03-21 | 2018-06-26 | 云南新昊环保科技有限公司 | A kind of method of waste mineral oil production fuel oil and lube base oil |
| CN111394123A (en) * | 2020-04-21 | 2020-07-10 | 云南新昊环保科技有限公司 | Process for refining regenerated base oil of lubricating oil from waste mineral oil solvent |
-
2021
- 2021-03-23 CN CN202110309724.4A patent/CN115109614B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ES2199697A1 (en) * | 2003-09-23 | 2004-02-16 | Sener Grupo De Ingenieria Sa | Method for regenerating used oils by demetallization and distillation |
| CA2783608A1 (en) * | 2012-07-23 | 2014-01-23 | Lucie Wheeler | Environmental process to transform contaminated or uncontaminated feed materials into useful products, uses of the process, products thereby obtained and uses thereof, manufacturing of the corresponding plant |
| CN107312568A (en) * | 2017-06-27 | 2017-11-03 | 爱润森德（天津）能源科技有限公司 | A kind of waste mineral oil catalytic pyrolysis utilization system and its processing technology |
| CN108203594A (en) * | 2018-03-21 | 2018-06-26 | 云南新昊环保科技有限公司 | A kind of method of waste mineral oil production fuel oil and lube base oil |
| CN111394123A (en) * | 2020-04-21 | 2020-07-10 | 云南新昊环保科技有限公司 | Process for refining regenerated base oil of lubricating oil from waste mineral oil solvent |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115109614B (en) | 2023-11-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110484345B (en) | Regeneration method of waste lubricating oil | |
| CN107574012A (en) | A kind of preparation method of producing base oil by regenerating waste lubricating oil | |
| CN108587766A (en) | A kind of free of contamination waste lubricating oil cyclic regeneration pretreating process | |
| CN110590087B (en) | Treatment method of oily sludge | |
| CN111394123A (en) | Process for refining regenerated base oil of lubricating oil from waste mineral oil solvent | |
| CN111718749A (en) | Waste mineral oil separation treatment method and system | |
| CN104445815A (en) | Technological method and device for semi-coke production wastewater resource utilization | |
| CN102260583B (en) | Combined process for refining base oil through recycle of waste machine oil | |
| CN105036507A (en) | Pyrolysis oil-gas-water synchronous condensing and oil-water separation recovery system and method | |
| CN115109614B (en) | Process method for coking and entrainment prevention of waste mineral oil regenerated base oil | |
| CN109423318B (en) | Coal tar deep processing technology for directly extracting industrial naphthalene by adding alkali after atmospheric and vacuum distillation | |
| CN110669549A (en) | Waste mineral oil regeneration and recovery treatment method | |
| CN101818096A (en) | Recovery system for reclaimed lubricating distillate oil and recovery processing method | |
| CN111821821A (en) | Fusel oil recycling device and method in methanol production | |
| CN101619230A (en) | Method for recycling organic compounds from caustic sludge generated in coal tar oil light end alkali cleaning | |
| CN208346102U (en) | The pretreatment of raw material solvent extraction system of needle coke industrialized production | |
| CN116040896A (en) | Recycling method for machining oil sludge | |
| CN112175743A (en) | Comprehensive treatment method for waste carclazyte after grease decolorization | |
| CN112499605A (en) | Integrated device and method for yellow phosphorus rinsing system and mud phosphorus continuous recovery | |
| CN111876197A (en) | Pretreatment process for treating waste lubricating oil by chemical refining method | |
| CN111547914A (en) | Method for recovering phenol from semi-coke wastewater | |
| CN112573784A (en) | Method for treating oily sludge by utilizing atmospheric and vacuum distillation/cracking device | |
| CN221093985U (en) | Device for recycling crude phenol from semi-coke wastewater and refining crude phenol | |
| JPS63139984A (en) | Equipment for recovery of shale oil from oil shale | |
| CN114395429B (en) | Low-rank coal dry distillation gas separation device and process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |