GB2521131A - Waste fuel oil recovery method and related ionic liquid recovery process - Google Patents

Waste fuel oil recovery method and related ionic liquid recovery process Download PDF

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Publication number
GB2521131A
GB2521131A GB1321773.2A GB201321773A GB2521131A GB 2521131 A GB2521131 A GB 2521131A GB 201321773 A GB201321773 A GB 201321773A GB 2521131 A GB2521131 A GB 2521131A
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Prior art keywords
recovery process
fuel oil
ionic liquid
short path
liquid recovery
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GB201321773D0 (en
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Wei-Ming Chang
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    • 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
    • C10G27/00—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation
    • C10G27/04—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation with oxygen or compounds generating oxygen
    • C10G27/14—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation with oxygen or compounds generating oxygen with ozone-containing gases
    • 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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/08—Inorganic compounds only
    • 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
    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
    • C10G53/14—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one oxidation step
    • 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
    • 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
    • C10M175/005—Working-up used lubricants to recover useful products ; Cleaning using extraction processes; apparatus therefor
    • 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
    • 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
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1062—Lubricating oils

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

A method for desulfurization and aromatic compounds removal of a fuel oil being recovered from waste lubricating oil with the use of ozone as an extracting agent, including a fuel oil extraction process for mixing fuel oil with ozone and performing the extraction process of desulfurization and aromatics removal, a high speed centrifuge separation process using a high speed disc separator to separate sulfide and aromatics from the produced fluid mixture so as to obtain a mixture of fuel oil and extracts, a fuel oil recovery process for performing a core operation of short path distillation to recovery fuel oil, an ionic liquid recovery process for performing a core operation of short path distillation to recover ionic liquid and a utility facility process using a cooling tower and a chiller to generate and circulate a chilled water for circulating through the fuel oil recovery process short path evaporator and the ionic liquid recovery process short path evaporator and related external cold wells for condensing the recovered fuel oil and ionic liquid.

Description

WASTE FUEL OIL RECOVERY METHOD AND RELATED
IONIC LIQUID RECOVERY PROCESS
BACKGROUND OF THE INVENTION
1. Field of the Invention:
The present inyention relates to fuel oil extraction technology, and more particularly to a method for desulfurization and aromatic compounds removal of fuel oil that is recovered from waste lubricating oil. The invention relates also to the recovery of ionic liquid.
2. Description of the Related Art:
Al the present time, hydrodesulfurization techniques are most commonly used for recovering fuel oil. After deep desulfurization during application of the hydrodesulfurization technique, the sulfur content in the recovered fuel oil is about S0ppm. Unless improving the catalyst reaction rate and increasing the working pressure and the reaction temperature, the conventional desulfurization techniques cannot achieve the expected desulfurization result to satisfy market demands for fuel oil of low sulfur content below l0ppm.
Based on technical natures, the currently developing technologies can he broadly divided into the following five kinds.
1. Solvent extraction desulfurization technology: This technology uses specific solvents as extractants, however these specific solvents are volatile and toxic and can cause environmental pollution.
2. Oxidative Desulfurization Process: This process needs to oxidize oil with a strong oxidizing agent, such as 11202, Ozone (0), ultraviolet or peroxyacid peracid, and then to start extraction separation by using a polar solvent, such as ACN (acetonitrile), DMSO (dimethysufoxide), DMF (N,N-dimethyformamide), however these polar solvents are highly volatile and flammable, easily leading to fires and explosions.
3. Desulfurization of Oil by Adsorption Technology: This techn&ogy adds an adsorbent in the desulfurization process to absorb suffides in the fuel ofl and then to perform a desuffurization reaction by hydrodesulfurization. The main problem of this technology is that its poor adsorption capability relative to DBT (dibenzothiophene).
4. Microbial desulfurization technology: This technology achieves desulfurization by using microbial metabolic enzymes as a catalyst to produce catalytic desulfurization reaction, however, this technology has the drawbacks of low reaction rate, low efficiency and high desulfurization strains culturing cost.
5. Desulfurization and Denitrogenation of Oil Streams by Extraction/Oxidation in Room Temperature Ionic Liquid System: This method is substantially similar to the aforesaid solvent extraction desulfurization technology with the exception that it
I
uses a non-toxic room temperature ionic liquid as an extractant to improve the reaction rate. Further, this method adds an oxidant, for example, H202 and a catalyst, for example, ethanoic acid (CH1COOH).
formic acid (HCOOH) or trifluoroacetic acid (CF3COOII) to accelerate desulfurization reaction; the reaction mixture is then allowed to stand for precipitation. After precipitation, the supernatant of purified fuel oH and the thwer ayer of ionic liquid, oxidant and catalyst mixture are separated by a centrifuge separator. The separated supernaant of purified Fuel oH is then processed into a low sulfur fuel oil through a dehydration and distillation process.
The separated tower layer of ionic Hquid, oxidant and cata'yst mixture is then processed through a back-extraction process using an anti-extractant such as hexane (C6H14) or N-methylpyrrolidone (NMP), enabling aromatic compounds to be extracted from the mixture. Thereafter, the ionic fluid and hexane (or NMP) are separated through a centrifuge separator for reuse.
However, adding a high concentration of hydrogen peroxide (H20,) or other oxidizing agent to enhance the reaction rate can cause a violent chemical reaction and instantaneously generate heat when encountered water-soluble ionic liquid, resulting in an ionic liquid hydr&ysis reaction. When this condition occurs, ionic liquid recycling becomes impossible. Using an oxidant that does not cause a violent reaction or ionic Uquid hydrcdysis reaction is possible way for improvement, however, this method can cause a quality change in the produced ionic liquid, and the produced ionic liquid will be not recyclable or can only be partially recycled.
SUMMARY OF THE INVENTION
The present invention has been accomplished under the circumstances in view. It is therefore the main object of the present invention to provide a method for desulfurizing fuel oil and removing aromatic compounds from fuel oil that is recovered from waste lubricating oil without using any white acid clay as commonly applied in the conventional waste lubricating oil recover techniques, lowering the chroma of the fuel oil and increasing the flash point and viscosity index of the fuel oil so as to improve the quality of the fuel oil. This method is more safety and more efficient than conventional techniques. and can greatly reduce virgin base oil loss and energy consumption and the processing cost and obtain high quality fuel oil. As the method of the invention eliminates the use of acid white clay as an adsorption filter media, the method of the invention prevents generation of environmentally harmful waste acid soil.
To achieve these and other objects of the present invention, method for desulfurizing fuel oil and removing aromatic compounds from fuel oil that is recovered from waste lubricating oil in accordance with the present invention uses an ionic liquid as
I-
an extracting agent, comprising a fuel oil extraction process. an oxidation process, a high speed centrifuge separation process, a fuel oil recovery process, an ionic liquid recovery process and a utility facility process.
The oxidation process uses ozone (03) as an oxidant to substitute for H202 that is commonly used in conventional methods for desulfurizing fuel oil and removing aromatic compounds from fuel oil. The use of ozone (03) as an oxidant effectively enhances the reaction rate of oxidation and extraction without causing any change in the material (ionic liquid or aromatics) properties.
The fuel oil recovery process and the ionic liquid recovery process respectively employ a fuel oil recovery process short path evaporator to recover fuel oil of low sulfur and low nitrogen content and ionic liquid.
The utility facility process is adapted to provide chilled water to the condenser of the fuel oil recovery process short path evaporator and the condenser of the ionic liquid recovery process short path evaporator for condensing.
Thus, the method of the present invention is capable of desulfurizing fuel oil and removing aromatic compounds from fuel oil that is recovered from waste lubricating oil. This method enables the fuel oil refining process to he performed under a high vacuum (low pressure) and low temperature working environment, preventing a secondary pollution, assuring a high level of safety, saving energy consumption and reducing the processing cost.
Further, this method is capable of recovering ionic liquid.
Other advantages and features of the present invention will be fully understood by reference to the following specification in conjunction with the accompanying drawings, in which like reference signs denote like components of structure.
BRIEF DESCRIPTION OF THE DRAWINGS
FIG. I is a system block diagram for the performance of fuel oil extraction process, oxidation process and high speed centrifuge separation process of a fuel oil recovery method in accordance with the present invention.
FIG. 2 is a system block diagram for the performance of the fuel oil recovery process of the fuel oil recovery method in accordance with the present invention.
FIG. 3 is a system block diagram for the performance of the ionic liquid recovery process of the fuel oil recovery method in accordance with the present invention.
FIG. 4 is a system block diagram for the performance of the utility facility process of the fuel oil recovery method in accordance with the present invention.
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT
Referring to FIGS. 1-4, the invention provides a waste fuel oil recovery method, which includes the steps of: fuel oil extraction process 10, an oxidation process 20, a high speed centrifuge separation process 30, a fuel oil recovery process 40, an ionic liquid recovery process 50, and a utility facility process 40.
Referring to FIG. 1 again, the fuel oil extraction process 10 is to mix waste fuel oil with an ionic liquid and then to perform an extraction process of desulfurization and aromatics removal.
Performing the fuel oil extraction process 10 needs the equipments of one fuel oil reconcile heating tank 11, a plurality of material delivery pumps 121/122/131/132, one room temperature ionic liquid storage tank 14 having stored therein an ionic liquid, OMIM BF4 or BMIMFeCI4 at room temperature, one centrifug& extractor 15, and one fuel oH and extract buffer tank 16.
When starting the fuel oil extraction process 10, heat the fuel oil reconcile heating tank 11 to 70°C and keep it at this temperature level when the prepared fuel oil is being continuously supplied. When the temperature of the fuel oil reconcile heating tank 11 reached the predetermined value, start the material delivery pumps 121/122/131/132 synchronously. At this time, the material delivery pumps 121/122/131/132 synchronously and respectively pump the prepared fuel oil and ionic liquid at a predetermined feed ratio to the centrifugal extractor 15 for desulfurization and aromatic compound removaL After extraction through the centrifuga' extractor 15, the mixture is delivered to the fuel oil and extract buffer tank 16 for continuous extraction reaction.
The predetermined feed ration between the fuel oil and the ionic liquid is determined subject to the characteristics and sulfide content of the fuel oil. Based on the actual operational verification. the feed ratio between the fuel oil and the ionic liquid is preferably within the range of 3:1-4:3.5.
The feed ratio between the fuel oil and the ionic liquid is adjustable subject to the concentration of DBTs and the actual working temperature during the extraction process.
Performing the oxidation process 20 requires a plurality of material delivery pumps 211/212/221/222, an air compressor 231, a high pressure gas impurity screening program, an ozone generator assembly 23 with an ozone generator 233, a venturi ejector 24, a buffer mixture mixing tank 25 with a ventilator 251, an exhaust blower 26, an activated carbon absorption tank 27, and an accelerator tank 28.
When starting the oxidation process 20, start the ozone generator 233 to generate ozone and to store the generated ozone in a steel cylinder under the pressure of 2-3kg/cm2. When the fuel oil and ionic liquid mixture in the fuel oil and extract buffer tank 16 reaches a predetermined high level, the material delivery pumps 211/212 are started to pump the fluid mixture out of the centrifugal extractor 15 into the venture ejector 24.
and at the same time, a flow of compressed ozone is sucked through a bypass entrance into the venture ejector 24. When the intake flow of ozone passed through the throat of the venture ejector 24, the flowing speed of the flow of ozone is enhanced, causing generation of ozone bubbles in the fluid
S
mixture that is being delivered through the venture ejector 24 to enhance the reaction rate of oxidation and extraction without causing any change in the material (ionic liquid or aromatics) properties. The gas fluid mixture is then guided into the buffer mixture mixing tank 25 for reaction while gases released from the gas fluid mixture and oxygen produced after decay of ozone rise and are accumulated in he ventilator 251. At this time, the exhaust Hower 26 is started to pump gases through the activated carbon absorption tank 27 into the atmosphere. This process absorbs pollutants from discharged gases, avoiding air poflution. The extraction reaction of the fluid mixture being guided into the buffer mixture mixing tank 25 is ongoing. When the fluid in the buffer mixture mixing tank 25 reaches a predetermined high eve, the materia' deilvery pumps 221/222 are started to pump the fluid mixture out of the buffer mixture mixing tank 25 into the accelerator tank 28 for continuous reaction and further processing.
The high speed centrifuge separation process 30 is adapted to separate the fluid mixture obtained through the oxidation process 20 into an ionic liquid and extract mixture and a fuel oil and extract mixture.
Running the high speed centrifuge separation process 30 requires the equipments of a plurality of material delivery pumps 311/312, one high speed disc separator 32, one ionic liquid buffer tank 33, and one fud ofl buffer tank 34.
When starting the high speed centrifuge separation process 30, the fuel oil and ionic liquid mixture is kept in the accelerator tank 28 for a predetermined length of time to complete the extraction reaction.
Thereafter, start the material delivery pumps 311/312 to pump the fluid mixture out of the accelerator tank 28 into the high speed disc separator 32 where the fluid mixture is separated into an ionic liquid containing a small amount of extracts, which is guided through a respective pipeline into the ionic liquid buffer tank 3 for further treatment 3. and a fuel oil containing a small amount of extracts, which is guided through a respective pipeline into the fuel oil buffer tank 34 for further treatment.
The specific gravity of the aforesaid ionic liquid of OMIM BF4 is 1.10kg/liter; the specific gravity of the aforesaid ionic liquid of BMIMFeCI4 is I.365kg/liter; the specific gravity of the fuel oil is determined subject to its composition. for example, about 0.73-0.76kg/liter for gasoline, about 0.83-0.86kg/liter for high speed diesel, about 0.85-0.87kg/liter for marine diesel, about 0.75-0.8kg/liter for jet fuel, about 0.86-0.991kg/liter for IFO-180-IFO-380 or 1-6 heavy fuel oils.
When compared with ionic liquids, there is a significant difference in specific gravity between ionic liquids and fuel oils. High speed centrifuge separation is capable of separating the ionic liquid mixture and the fuel oil mixture.
Referring to FIG. 2, the fuel oil recovery process 40 is adapted to perform the core operation of short path distillation subject to the following characteristics: a) Prepare fuel oil recovery process 40 equipments. comprising a plurality of fuel oil recovery process material delivery pump 411/412/421/422/431/432, one fuel oil recovery process pre-heater 44.
one fuel oil recovery process short path evaporator 45, one fuel oil recovery process thermal oil expansion tank 46, one fuel oil recovery process thermal oil heating furnace 47, a plurality of fuel oil recovery process thermal oil delivery pumps 481/482, one fuel oil finished product deposit tank 491, one fuel oil recovery process by-product deposit tank 492, one fuel oil recovery process vacuum buffer tank 493, one fuel oil recovery process gas-liquid separator 494, one fuel oil recovery process vacuum pump system 495, one fuel oil finished product storage tank 496, and one by-product storage tank 497.
b) In actual operation of the fuel oil recovery process 40, initiate the fuel oil recovery process thermal oil heating furnace 47 and the fuel oil recovery process thermal oil delivery pumps 481/482 where one flow of thermal oil is being circulate through the fuel oil recovery process thermal oil heating furnace 47 via a fluid passage in the cylinder wall of the fuel oil recovery process short path evaporator 45 and a fluid passage in the heating layer of the fuel oil recovery process pre-heater 44 another flow of thermal oil is being delivered through a sub piping to the fuel oil recovery process thermal oil expansion tank 46 and then hack to the fuel oil recovery process thermal oil delivery pumps 481/482 and then to the fuel oil recovery process thermal oil heating furnace 47; this pre-heating process is continued till the temperature of the cylinder wall of the fuel oil recovery process short path evaporator 45 and the temperature of the heating layer of the fuel oil recovery process pre-heater 44 reach the predetermined working temperature level; the fuel oil recovery process thermal oil heating furnace 47 will stop heating after reached the predetermined working temperature, and will start to heat again when the temperature of the returned thermal oil dropped below the predetermined temperature level, i.e., the fuel oil recovery process thermal oil heating furnace 47 will he intermittently started to maintain the desired system working temperature; the control of the heating power and temperature of the fuel oil recovery process thermal oil heating furnace 47 is performed through a diode based heating fluid controller (not shown).
c) During operation of the thermal oil heating system of the fuel oil recovery process 40, the fuel oil recovery process vacuum pump system 495 is simultaneously started to pump air out of the fuel oil recovery process short path evaporator 45, the fuel oil finished product deposit tank 491 and the fuel oil recovery process by-product deposit tank 492 via the fuel oil recovery process vacuum buffer tank 493 and fuel oil recovery process gas-liquid separator 494. The fuel oil recovery process vacuum pump system 495 stops pumping immediately after the vacuum pressure in the related piping reaches the predetermined working pressure. Thereafter, material feeding is started, causing rise in the internal working pressure of the fuel oil recovery process short path evaporator 45. When the internal working pressure rises, the fuel oil recovery process vacuum pump system 495 is started again, i.e., the fuel oil recovery process vacuum pump system 395 works intermittently to maintain the system working pressure. This operation manner enables the internal working pressure of the fuel oil recovery process short path evaporator 45 of the fuel oil recovery process to be maintained within the predelermined range, assuring a high level of system stability.
d) The operation is started when system preparation is done. When the fluid level in the fuel oil buffer tank 34 of the high speed centrifuge separation process 30 reaches a predetermined high level position, the fuel oil recovery process material delivery pumps 411/412 are started to pump the mixture of fuel oil and extract through the fuel oil recovery process pre-heater 34 for indirect heating; the fluid material passing through the fuel oil recovery process pre-heater 44 for indirect heating is delivered to a distribution panel at a top side inside the fuel oil recovery process short path evaporator 45, and then guided by a discharge gap, which is disposed in a diagonal relationship with the vacuum exhaust port, downwardly along a cylinder into the fuel oil recovery process short path evaporator 45; the fuel oil recovery process short path evaporator 45 has a scrapper module mounted therein and rotatable by a top-sided motor 451 through a gear speed reducer 452 at a speed about 160-180r.p.m. with spring-loaded front blades thereof stopped against the internal cylinder wall of the fuel oil recovery process short path evaporator 45 to spread downward falling fuel oil onto the internal cylinder wall of the fuel oil recovery process short path evaporator 45 so that a thin film of fuel oil of a predetermined thickness can be formed on the internal cylinder wall of the fuel oil recovery process short path evaporator 35; when the material is being distributed through the distribution panel into the inside of the cylinder wall of the fuel oil recovery process short path evaporator 45, the cylinder wall of the Fuel oil recovery process short path evaporator 45 is being continuously pre-heated, the internal working pressure and temperature are locked, enabling the re-fined base oil to he optimaUy evaporated and refined; thus, when the re-Fined base oil is being distributed into ihe inside of the cylinder wall of the fuel oil recovery process shon path evaporator 45 and spread by the graphite blades of the scraper modu'e to form an oil fflm on the interna' cylinder wall of the fuel oil recovery process short path evaporator 45. it will be heated to release out fuel oil molecules for free traveling, enabling the fuel oil molecules to enter the internal condenser (not shown) in the fuel oil recovery process short path evaporator 45 subject to the pumping effect of the fuel oil recovery process vacuum pump system 495, thus, the molecules of the transiently heated target thin film of fuel oil are immediately evaporated and released out; the continuous pumping operation of the fuel oil recovery process vacuum pump system 495 causes formation of a r&atively low pressure ifflet for the passing of the molecuks; however, because the fuel oil recovery process short path evaporator 45 has the condenser (not shown) verticafly disposed therein at the center, the fu& oil molecules will touch the condenser coils of the condenser before passing through the condenser to the exhaust port; because the condenser coils has a cooling water flowing therethrough, the fuel oil molecules are immediately cooled down and condensed into a liquid state to flow into the beneath fuel oil finished product deposit tank 491; when the fluid in the beneath fuel oil finished product deposit tank 491 reaches a high level, the fuel oil recovery process material delivery pumps 421/422 are automatically started to pump the cumulated fuel oil out of the fuel oil finished product deposit tank 491 to the fuel oil finished product storage tank 496 and then pumped out of the fuel oil finished product storage tank 496 by fuel oil recovery process finished product outlet pumps 497 for delivery and further application.
e) During the fuel oil recovery process 40. the minor amount of extracts that are adhered to the fuel oil and contain impurities such as sulfur and aromatics are synchronously delivered to the fuel oil recovery process short path evaporator 45, however because the internal working pressure and working temperature in the fuel oil recovery process short path evaporator 45 are still below the predetermined values, the minor amount of extracts in the mixture will not be evaporated into molecules and will be maintained in the form of a suspension and guided along the internal cylinder wall into an oblique hopper at the bottom side of the fuel oil recovery process short path evaporator 45 and then discharged into the fuel oil recovery process by-product deposit tank 492; when the fluid in the fuel oil recovery process by-product deposit tank 492 reaches a predetermined high level, the fuel oil recovery process material delivery pump 431/432 are automatically started to pump this by-product into the fuel oil recovery process by-product storage tank 497 for storage and further delivery.
Referring to FIG. 3, the ionic liquid recovery process 50 is adapted to perform the core operation of short path distillation subject to the following characteristics: a) The ionic liquid recovery process 50 needs to use the equipments of: a plurality of ionic liquid recovery process material delivery pumps 511/512/521/522/531/532, one ionic liquid recovery process pre-heater 54. one ionic liquid recovery process short path evaporator 55.
one ionic liquid recovery process thermal oil expansion tank 56, one ionic liquid recovery process thermal oil heating furnace 57, one ionic liquid recovery process thermal oil delivery pumps 581/582, one ionic liquid buffer tank 591. one ionic liquid recovery process by-product deposit tank 592, one ionic liquid recovery process vacuum buffer tank 593, one ionic liquid recovery process gas-liquid separator 594. one ionic liquid recovery process vacuum pump system 595, one ionic liquid recovery process storage tank 596, and one ionic liquid recovery process by-product storage tank 597.
h) During operation of the ionic liquid recovery process 50, start the ionic liquid recovery process thermal oil heating furnace 57 and the ionic liquid recovery process thermal oil delivery pumps 581/582 to pump a thermal oil through the cylinder jacket of the ionic liquid recovery process short path evaporator 55 and the thermal oil heating jacket of the ionic liquid recovery process pre-heater 54 and then back to the ionic liquid recovery process thermal oil heating furnace 57; another flow of thermal oil is delivered through a branch pipeline to the ionic liquid recovery process thermal oil expansion tank 56 and the ionic liquid recovery process thermal oil delivery pumps 581/582 and then hack to the ionic liquid recovery process thermal oil heating furnace 57; the pre-heating operation keeps going till that the temperature of the cylinder jacket of the ionic liquid recovery process short path evaporator 55 and the temperature of the thermal oil heating jacket of the ionic liquid recovery process pre-heater 54 reach the predetermined working temperature, and the ionic liquid recovery process thermal oil heating furnace 57 is stopped from heating when the predetermined working temperature is obtained, or started again when the temperature of the returned thermal oil drops below the predetermined working temperature; the heater power and heating temperature of the ionic liquid recovery process thermal oil heating furnace 57 are controlled by a diode-based heating fluid controller and a programmable logic controller (not shown).
c) During the operation of the thermal oil heating system of the ionic liquid recovery process 50, the ionic liquid recovery process vacuum pump system 595 is simultaneously started to draw air out of the ionic liquid recovery process short path evaporator 55, the NMP buffer tank 591 and the ionic liquid recovery process by-product deposit tank 592 via the ionic liquid recovery process vacuum buffer tank 593 and the ionic liquid recovery process gas-liquid separator 594. and the ionic liquid recovery process vacuum pump system 595 is stopped from pumping when the pressure in the entire pipeline system reaches a predetermined working pressure, and then material feeding is started, and the ionic liquid recovery process vacuum pump system 595 wifl he started again as the intern& working pressure of the ionic liquid recovery process short path evaporator rises, i.e., the ionic liquid recovery process vacuum pump system 595 works intermittently to maintain the internal working pressure of the ionic liquid recovery process short path evaporator 55 within the set range, assuring system operation stability.
d) After system preparation is done, the ionic liquid recovery processing process is started; if the fluid mixture of the ionic liquid and extracts in the ionic liquid buffer tank 33 of the ionic liquid extraction process 30 reaches the predetermined high level, the ionic liquid recovery process material delivery pumps 511/512 are started to pump the fluid mixture of the ionic liquid and extracts through the ionic liquid recovery process pre-heater 54 for indirect heating; the fluid material being heated by the ionic liquid recovery process pre-heater 54 is guided by a discharge gap in a diagon& relationship with the vacuum exhaust port downwardly along a cylinder into the to the internal distribution panel of the ionic liquid recovery process short path evaporator 55; the interna' distribution pand of the ionic liquid recovery process short path evaporator 55 has a scrapper module mounted therein and rotatable by a top-sided motor 551 through a gear speed reducer 552 at a speed about 160-ASOr.pm. with spring-loaded front blades thereof stopped against the internal cylinder wall of the ionic liquid recovery process short path evaporator 55 to spread downward falling ionic liquid onto the internal cylinder wall of the ionic liquid recovery process short path evaporator 55 so that a thin film of ionic liquid of a predetermined thickness can he formed on the internal cylinder wall of the ionic liquid recovery process short path evaporator 55; when the material is being distributed through the distribution panel into the inside of the cylinder wall of the ionic liquid recovery process short path evaporator 55, the cylinder wall of the ionic liquid recovery process short path evaporator 55 is being continuously pre-heated, the internal working pressure and temperature are locked, enabling the ionic liquid to be optimally evaporated and refined; thus, when the ionic liquid is being distributed into the inside of the cylinder wall of the ionic liquid recovery process short path evaporator 55 and spread by the graphite blades of the scraper module to form an ionic liquid film on the internal cylinder wall of the ionic liquid recovery process short path evaporator 55. it will be heated to release out ionic liquid molecules for free traveling, enabling the ionic liquid molecules to enter the internal condenser (not shown) in the ionic liquid recovery process short path evaporator 55 subject to the pumping effect of the ionic liquid recovery process vacuum pump system 595, thus, the molecules of the transiently heated target thin film of fuel oil are immediately evaporated and released out; the continuous pumping operation of the ionic liquid recovery process vacuum pump system 595 causes formation of a relatively low pressure inlet for the passing of the molecules; however, because the ionic liquid recovery process short path evaporator 55 has the condenser (not shown) vertically disposed therein at the center, the fuel oil molecules will touch the condenser coils of the condenser before passing through the condenser to the exhaust port; thus, when the re-fined hase oil is being distributed into the inside of the cylinder wall of the ionic liquid recovery process short path evaporator 55 and spread hy the graphite hlades of the scraper module to form an oil film on the internal cylinder wall of the ionic liquid recovery process short path evaporator 55, it will be heated to release out fuel oil molecules for free traveling, enabling the fuel oil molecules to enter the internal condenser (not shown) in the ionic liquid recovery process short path evaporator 55 subject to the pumping effect of the ionic liquid recovery process vacuum pump system 595. thus, the molecules of the transiently heated target thin film of ionic liquid are immediately evaporated and released out; the continuous pumping operation of the ionic liquid recovery process vacuum pump system 595 causes formation of a relatively low pressure inlet for the passing of the molecules; however, because the ionic liquid recovery process short path evaporator 55 has the condenser (not shown) vertically disposed therein at the center, the ionic liquid molecules will touch the condenser coils of the condenser before passing through the condenser to the exhaust port; because the condenser coils has a cooling water flowing therethrough, the ionic liquid molecules are immediately cooled down and condensed into a liquid state to flow into the ionic liquid buffer tank 591; when the fluid in the ionic liquid buffer tank 591 reaches a high level, the ionic liquid recovery process material delivery pumps 511/512 are automatically started to pump the cumulated fuel oil out of the ionic liquid buffer tank 591 to the ionic liquid recovery process storage tank 596 for further delivery.
e) During the ionic liquid recovery process 50, the minor amount of extracts that are adhered o the fuel oil and contain impurities such as sulfur and aromatics are synchronously delivered to the ionic liquid recovery process short path evaporator 55. however because the internal working pressure and working temperature in the ionic liquid recovery process short path evaporator 55 are still below the predetermined values, the minor amount of extracts in the mixture will not be evaporated into molecules and will be maintained in the form of a suspension and guided along the internal cylinder wall into an oblique hopper at the bottom side of the ionic liquid recovery process short path evaporator 55 and then discharged into the ionic liquid recovery process by-product deposit tank 592; when the fluid in the ionic liquid recovery process by-product deposit tank 592 reaches a predetermined high level, the ionic liquid recovery process material delivery pumps 531/532 are automatically started to pump this by-product into the ionic liquid recovery process by-product storage tank 597 for storage and further delivery.
Referring to FIG. 4, the utility facility process 60 is adapted to provide cooling water and chilled water to the internal condenser of the fuel oil recovery process short path evaporator 45 and its linked external cold well 453 and the internal condenser of the ionic liquid recovery process short path evaporator 55 of the ionic liquid recovery process 50 and its linked external cold well 553.
The utflity facUlty process 60 provides a coohng tower 61, a chiller 62, a plurality of chilled water delivery pumps 631/632, a cooling water recycling pump 641/642, and coohng water d&ivery pumps 651/652/661/662.
When starting the utility facility process 60, all the equipments of the utility facility process 60 are turned on, enabling chilled water and cooling water to be pumped by the chilled water delivery pumps 631/632 and the cooling water delivery pumps 651/652/661/662 to the target equipments, i.e., the fuel oil recovery process short path evaporator 45 and the cooling water inlet pipeline of the ionic liquid recovery process short path evaporator 55, and then delivered by the cooling water recycling pump 641/642 through recycling pipelines to the cooling tower 61 for cooling, and thus, the recyded cooflng water is kept at the predetermined working temperature level; subject to system requirements, the temperature of the delivered cooling waler is about 25-28°C, the temperature of the recycled cooling water is about 30-33 CC, and the temperature difference between these two flows of water is about 5°C; therefore, the heat dissipation capacity of the cooling tower 61, the working pressure and flow rate of each individual cooling water delivery pump and other related parameters are determined subject to individu& conditions and requirements of the operating system to satisfy actual requirements.
In one appilcation exampk of the present invention, the internal working pressure of the fuel oil recovery process short path evaporator 45 is set at 2O-25Pa (Pascal).
In one application example of the present invention, the internal working temperature of the fuel oil recovery process short path evaporator is set at i3OiS0°C.
In one application example of the present invention, the graphite blades of the scraper module in the fuel oil recovery process 40 is adapted to spread the supplied mixture of fuel oil and extracts on the internal cylinder wall of the fuel oil recovery process short path evaporator 45 to form an oil film of thickness less then 1mm.
In one application example of the present invention, the internal working pressure of the ionic liquid recovery process short path evaporator 55 is set at 20-25Pa (Pascal).
In one appilcation examp'e of the present invention, the internal working temperature of the ionic liquid recovery process short path evaporator 55 is set at 1 10-130t.
In one application example of the present invention, the graphite blades of the scraper module in the fuel oil recovery process 40 is adapted to spread the supplied mixture of fuel oil and extracts on the internal cylinder wall of the fuel oil recovery process short path evaporator 45 to form an oil film of thickness less then 1mm. In one application example of the present invention, the fuel oil recovery process short path evaporator 45 in the fuel oil recovery process 40 has connected thereto a cooling well 453, a fuel oil recovery process material delivery pump 454, and a material storage tank 455; in the evaporation operation of the fuel oil recovery process short path evaporator 45, there are some light hydrocarbons such as C710H1622 and the molecular weights of these light hydrocarbons are lower than the fuel oil to he recycled and the mean free paths of these light hydrocarbons are longer than the fuel oil to be recycled; during the operation, these minor amount of light hydrocarbons will be simultaneously evaporated and released out of the internal condenser of the fuel oil recovery process short path evaporator 45 into the exhaust passageway and then trapped by the cold well 453; the light hydrocarbons contain volatile gases and the predetermined working temperature is as high as 150°C-480°C, and therefore, in order to prevent the light hydrocarbons from entering the pipeline of the vacuum system to damage the fuel oil recovery process vacuum pump system 495, a condensing coil is provided in the utility facility process 60 for continuously guiding 5°C chilled waler into the cold well 453 to condense the light hydrocarbons in the cold well 453; thereafter, as soon as the fluid in the cold well 453 reaches a predetermined high level, the fuel oil recovery process material delivery pump 454 is started to pump the fluid material out of the cold well 453 into the material storage tank 455 for further delivery; the chilled water for this condensing system is provided by the chiller 62 of the utility facility process 60; during operation. the 5°C chilled water generated by the chifler 62 is pumped by the interna' pump of the chifler 62 to the cold wefl 453 for condensing, enabling the condensed water to he sent back to the chiller 62 for chilling, enabling the chilled 5°C water to be further delivered to the cold well 453 again; further, in order to prevent overheat of the lubricant of the gear speed reducer 452 of the fuel oil recovery process short path evaporator 45 and further gear speed reducer damage due to continuous tong period operation, a branch pipeBne is provided to guide a part of the generated chilled water from the chiller 62 to the axle seals of the fu& ofl recovery process short path evaporator 45 to cool down the ax'e seals, and the used cooling water is then delivered with the discharged condensed water of the cold wefl 453 hack to the water chifler 62 by a cooling water circulating pipeline.
In one application example of the present invention, the graphite blades of the scraper module in the ionic liquid recovery process 50 is adapted to spread the supphed mixture of fud oil and extracts on the internal cylinder wall of the ionic liquid recovery process short path evaporator 55 to form an oil mm of thickness tess then lmm.In one application example of the present invention, the ionic liquid recovery process short path evaporator 55 in the ionic liquid recovery process 50 has connected thereto a cooling well 553, an ionic liquid recovery process material delivery pump 554, and a material storage tank 555; in the evaporation operation of the ionic liquid recovery process short path evaporator 55, there are some light hydrocarbons such as C7)H1622 and the molecular weights of these light hydrocarbons are lower than the fuel oil to he recycled and the mean free paths of these light hydrocarbons are longer than the fuel oil to he recycled; during the operation, these minor amount of light hydrocarbons will he simultaneously evaporated and released out of the internal condenser of the ionic liquid recovery process short path evaporator 55 into the exhaust passageway and then trapped by the cold well 553; the light hydrocarbons contain volatile gases and the predetermined working temperature is as high as 1 10°C-130°C. and therefore, in order to prevent the light hydrocarbons from entering the pipeline of the vacuum system to damage the fuel oil recovery process vacuum pump system 595, a condensing coil is provided in the utility facility process 60 for continuously guiding 5°C chilled water into the cold well 553 to condense the light hydrocarbons in the cold well 553; thereafter, as soon as the fluid in the cold well 553 reaches a predetermined high level, the fuel oil recovery process material delivery pump 554 is started to pump the fluid material out of the cold well 553 into the material storage tank 555 for further delivery; the chilled water for this condensing system is provided by the chiller 62 of the utility facility process 60; during operation, the 5°C chilled water generated by the chiller 62 is pumped by the internal pump of the chiller 62 to the cold well 553 for condensing, enabling the condensed water to be sent back to the chiller 62 for chilling, enabling the chilled 5°C water to he further delivered to the cold well 553 again; further, in order to prevent overheat of the lubricant of the gear speed reducer 552 of the fuel oil recovery process short path evaporator 55 and further gear speed reducer damage due to continuous long period operation, a branch pipeline is provided to guide a part of the generated chilled water from the chiller 62 to the axle seals of the fuel oil recovery process short path evaporator 55 to cool down the axle seals, and the used cooling water is then delivered with the discharged condensed water of the cold well 553 back to the water chiller 62 by a cooling water circulating pipeline.
Although a particular embodiment of the invention has been described in detail for purposes of illustration, various modifications and enhancements may be made without departing from the spirit and scope of ihe invention. Accordingly, the invention is not to be limited except as by the appended claims.

Claims (9)

  1. What the invention claimed is: 1. A method for desulfurization and aromatic compounds removal of a fuel oil being recovered from waste lubricating oil with the use of ozone as an extracting agent, the method comprising: (1) a fuel oil extraction process for mixing said fuel oil with ozone and performing the extraction process of desulfurization and aromatics removal; (2) an oxidation process, comprising: a) a set of equipments comprising a plurality of oxidation process material delivery pumps, an air compressor, a high pressure gas impurity screening program, an ozone generator assembly with an ozone generator, a venture ejector, a buffer mixture mixing tank with a ventilator, an exhaust blower, an activated carbon absorption tank and an accelerator tank; b) enabling said ozone generator assembly to provide generated ozone into said venture ejector and simultaneously driving one said oxidation process material delivery pump to pump the fluid mixture obtained through said fuel oil extraction process into said venturi ejector for mixing with the provided ozone to form a fuel oil and ozone mixture; and c) guiding said fuel oil and ozone mixture from said venture ejector into said buffer mixture mixing tank for reaction, enabling released ozone to be accumulated in said ventilator and then blown by said exhaust blower through said activated carbon absorption tank into the atmosphere, and then starting another said oxidation process material delivery pump to pump the mixture out of said buffer mixture mixing tank into said accelerator tank for continuous reaction when the mixture in said buffer mixture mixing tank reaches a predetermined high level; (3) a high speed centrifuge separation process using a high speed disc separator to separate sulfide and aromatics from the fluid mixture obtained from step (2) so as to obtain a fuel oil mixture and an ionic liquid mixture; (4) a fuel oil recovery process for performing a core operation of short path distillation, said fuel oil recovery process comprising: a) a set of equipments comprising a fuel oil recovery process material delivery pump, a fuel oil recovery process pre-heater. a fuel oil recovery process short path evaporator, a fuel oil recovery process thermal oil expansion tank, a fuel oil recovery process thermal oil heating furnace, a plurality of fuel oil recovery process thermal oil delivery pumps, a fuel oil finished product deposit tank, a fuel oil recovery process by-product deposit tank, a fuel oil recovery process vacuum buffer tank, a fuel oil recovery process gas-liquid separator, a fuel oil recovery process vacuum pump system, a fuel oil finished product storage tank, and a fuel oil recovery process by-product storage tank; b) driving said fuel oil recovery process thermal oil heating furnace and said fuel oil recovery process thermal oil delivery pump to circulate a thermal oil through a cylinder jacket of said fuel oil recovery process short path evaporator and a heating jacket of said fuel oil recovery process pre-heater and said fuel oil recovery process thermal oil heating furnace and to deliver another flow of said thermal oil through said fuel oil recovery process thermal oil expansion tank and then back to said fuel oil recovery process thermal oil heating furnace to the extent that the temperature of said cylinder jacket of said fuel oil recovery process short path evaporator and the temperature of said heating jacket of said fuel oil recovery process pre-heater reaches a predetermined working temperature, and then intermittently running said fuel oil recovery process thermal oil heating furnace to maintain the predetermined temperature level; c) starting said fuel oil recovery process vacuum pump system to pump air out of said fuel oil recovery process short path evaporator, said fuel oil finished product deposit tank and said fuel oil recovery process by-product deposit tank via said fuel oil recovery process vacuum buffer tank and said fuel oil recovery process gas-liquid separator till that the internal pressure of said fuel oil recovery process short path evaporator, said fuel oil finished product deposit tank and said fuel oil recovery process by-product deposit tank reaches a predetermined working pressure level, and then intermittently running said fuel oil recovery process vacuum pump system to maintain the predetermined d) driving one said fuel oil recovery process material delivery pump to pump the fluid mixture of fuel oil and extracts produced in said high speed centrifuge separation process through said fuel oil recovery process pre-heater for heating and to continuously pump the fluid mixture to said fuel oil recovery process short path evaporator, enabling the fluid mixture to be spread by graphite blades of an internal scraper of said fuel oil recovery process short path evaporator onto an internal cylinder wall of said fuel oil recovery process short path evaporator to form an oil film of a predetermined thickness, said oil film being further evaporated by the heat of said cylinder jacket of said fuel oil recovery process short path evaporator to release out fuel oil molecules for free travel, the released said fuel oil molecules being pumped by said fuel oil recovery process vacuum pump system to an internal condenser of said fuel oil recovery process short path evaporator and then condensed into a fuel oil that is then delivered into said fuel oil finished product deposit tank and then said fuel oil finished product storage tank; and e) the extracts left in said fuel oil recovery process short path evaporator in a fluid state being guided into said fuel oil recovery process by-product deposit tank and said fuel oil recovery process by-product storage tank; (5) an ionic liquid recovery process for performing a core operation of short path distillation, said ionic liquid recovery process comprising: a) a set of equipments comprising a plurality of ionic liquid recovery process material delivery pumps. an ionic liquid recovery process pre-heater, an ionic liquid recovery process short path evaporator, an ionic liquid recovery process thermal oil expansion tank, an ionic liquid recovery process thermal oil heating furnace, a plurality of ionic liquid recovery process thermal oil delivery pumps, an ionic liquid buffer tank, an ionic liquid recovery process by-product deposit tank. an ionic liquid recovery process vacuum buffer tank, an ionic liquid recovery process gas-liquid separator, an ionic liquid recovery process vacuum pump system, an ionic liquid recovery process storage tank and an ionic liquid recovery process by-product storage tank; h) driving said ionic liquid recovery process thermal oil heating furnace and said ionic liquid recovery process thermal oil delivery pumps to circulate a thermal oil through a cylinder jacket of said ionic liquid recovery process short path evaporator and a heating jacket of said ionic liquid recovery process pre-heater and said ionic liquid recovery process thermal oil heating furnace and to deliver another flow of said thermal oil through said ionic liquid recovery process thermal oil expansion tank and then back to said ionic liquid recovery process thermal oil heating furnace to the extent that the temperature of said cylinder jacket of said ionic liquid recovery process short path evaporator and the temperature of said heating jacket of said ionic liquid recovery process pre-heater reaches a predetermined working temperature, and then intermittently running said ionic liquid recovery process thermal oil heating furnace to maintain the predetermined temperature level; c) starting said ionic liquid recovery process vacuum pump system to pump air out of said ionic liquid recovery process short path evaporator, said ionic liquid finished product deposit tank and said ionic liquid recovery process by-product deposit tank via said ionic liquid recovery process vacuum buffer tank and said ionic liquid recovery process gas-liquid separator till that the internal pressure of said ionic liquid recovery process short path evaporator, said ionic liquid finished product deposit tank and said ionic liquid recovery process by-product deposit tank reaches a predetermined working pressure level, and then intermittently running said ionic liquid recovery process vacuum pump system to maintain the predetermined working pressure; d) driving one said ionic liquid recovery process material delivery pump to pump the fluid mixture of ionic liquid and extracts produced in said high speed centrifuge separation process through said ionic liquid recovery process pre-heater for heating and to continuously pump the fluid mixture to said ionic liquid recovery process short path evaporator, enabling the fluid mixture to be spread by graphite blades of an internal scraper of said ionic liquid recovery process short path evaporator onto an internal cylinder wall of said ionic liquid recovery process short path evaporator to form an ionic liquid film of a predetermined thickness, said ionic liquid film being further evaporated by the heat of the cylinder jacket of said ionic liquid recovery process short path evaporator to release out ionic liquid molecules for free travel, the released said ionic liquid molecules being pumped by said ionic liquid recovery process vacuum pump system to an internal condenser of said ionic liquid recovery process short path evaporator and then condensed into an ionic liquid that is then delivered into said ionic liquid buffer tank and then said ionic liquid recovery process storage tank; and e) the extracts left in said ionic liquid recovery process short path evaporator in a fluid state being guided into said ionic liquid recovery process by-product deposit tank and said ionic liquid recovery process by-product storage tank; (6) a utility facility process using a cooling tower and a chiller to generate and circulate chilled water for circulating through said fuel oil recovery process short path evaporator and said ionic oil recovery process short path evaporator and respectively linked external cold wells for condensing the produced fuel oil and ionic liquid.
  2. 2. The method as claimed in claim 1, wherein the predetermined working pressure of said fuel oil recovery process short path evaporator is in the range of 2025Pa.
  3. 3. The method as claimed in claim 1, wherein the predetermined working temperature of said fuel oil recovery process short path evaporator is in the range of 150-180°C
  4. 4. The method as claimed in claim 1, wherein the oil film formed of the fluid mixture being spread by the graphite blades of the internal scraper of said fuel oil recovery process short path evaporator onto the internal cylinder wall of said fuel oil recovery process short path evaporator has a thickness less then 1mm.
  5. 5. The method as claimed in claim 1, wherein the predetermined working pressure of said ionic liquid recovery process short path evaporator is in the range of 20-25Pa.
  6. 6. The method as claimed in claim 1, wherein the predetermined working temperature of said ionic liquid recovery process short path evaporator is in the range of ii 0-130°C
  7. 7. The method as claimed in claim 1, wherein the oil film formed of the fluid mixture being spread by the graphite blades of the internal scraper of said ionic liquid recovery process short path evaporator onto the internal cylinder wall of said ionic liquid recovery process short path evaporator has a thickness less then 1mm.
  8. 8. The method as claimed in claim 1, wherein said fuel oil recovery process short path evaporator of said fuel oil recovery process has connected thereto a fuel oil cold well, a fuel oil recovery process material delivery pump and a material storage tank, said cold well being adaNed to trap light hydrocarbons produced by said Fuel oH recovery process shon path evaporator during condensing, enabling the material being condensed in said fuel oil co'd well to he delivered to said Fue' oil recovery process material storage tank by said fuel oil recovery process material delivery pump For further defl very.
  9. 9. The method as dairned in daim I, wherein said ionic liquid recovery process short path evaporator of said ionic liquid recovery process has connected thereto a ionic liquid cold well, an ionic liquid recovery process material delivery pump and an ionic liquid material storage tank, said ionic liquid cold well being adapted to trap light hydrocarbons produced by said ionic liquid recovery process short path evaporator during condensing, enabling the material being condensed in said ionic liquid cold well to be delivered to said ionic liquid process material storage tank by said ionic liquid recovery process material deflvery pump for further delivery.
GB1321773.2A 2013-12-10 2013-12-10 Waste fuel oil recovery method and related ionic liquid recovery process Withdrawn GB2521131A (en)

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Publication number Priority date Publication date Assignee Title
CN105754635A (en) * 2016-04-21 2016-07-13 辽宁石油化工大学 Oil product oxidizing desulfurization catalyzing method based on dual-core ion liquid phosphotungstate

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Publication number Priority date Publication date Assignee Title
CN114307560B (en) * 2020-10-09 2022-11-22 中石化南京化工研究院有限公司 Method for recovering NMP in waste gas

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JP2002206093A (en) * 2000-11-10 2002-07-26 Seishiro Murakami Method for producing fuel for diesel engine
JP2005015533A (en) * 2003-06-24 2005-01-20 Mitsui Eng & Shipbuild Co Ltd Method and apparatus for oxidative desulfurization of liquid petroleum product

Patent Citations (2)

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Publication number Priority date Publication date Assignee Title
JP2002206093A (en) * 2000-11-10 2002-07-26 Seishiro Murakami Method for producing fuel for diesel engine
JP2005015533A (en) * 2003-06-24 2005-01-20 Mitsui Eng & Shipbuild Co Ltd Method and apparatus for oxidative desulfurization of liquid petroleum product

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105754635A (en) * 2016-04-21 2016-07-13 辽宁石油化工大学 Oil product oxidizing desulfurization catalyzing method based on dual-core ion liquid phosphotungstate

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