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WO2017123260A1 - Distillation d'huile moteur usagée avec des vapeurs de distillat - Google Patents

Distillation d'huile moteur usagée avec des vapeurs de distillat Download PDF

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Publication number
WO2017123260A1
WO2017123260A1 PCT/US2016/013764 US2016013764W WO2017123260A1 WO 2017123260 A1 WO2017123260 A1 WO 2017123260A1 US 2016013764 W US2016013764 W US 2016013764W WO 2017123260 A1 WO2017123260 A1 WO 2017123260A1
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Prior art keywords
ulo
feed
boiling range
oil
fraction
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Inventor
Robert H. Wombles
Timothy E. LASKA
John T. Turner
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
    • C10M175/0033—Working-up used lubricants to recover useful products ; Cleaning by thermal processes using distillation processes; devices therefor

Definitions

  • the invention relates to direct contact heating of normally liquid hydrocarbons and the like especially those which are thermally unstable or difficult to heat, e.g. processing used motor oil, to recover distillable hydrocarbons.
  • the invention also relates to a way to recover a lube blending stock or a high quality feed for a catalytic cracking unit from used motor oil.
  • Automotive and many industrial lubricating oils are usually formulated from paraffin based petroleum distillate oils or from synthetic base lubricating oils.
  • Lubricating oils are combined with additives such as soaps, extreme pressure (E.P.) agents, viscosity index (V.I.) improver, antifoamants, rust inhibitors, anti-wear agents, antioxidants, and polymeric dispersants to produce an engine lubricating oil of SAE 5 to SAE 60 viscosity.
  • additives such as soaps, extreme pressure (E.P.) agents, viscosity index (V.I.) improver, antifoamants, rust inhibitors, anti-wear agents, antioxidants, and polymeric dispersants to produce an engine lubricating oil of SAE 5 to SAE 60 viscosity.
  • This used oil is collected from truck and bus fleets, automobile service stations, and municipal recycling centers for reclaiming.
  • the collected used oil contains organo- metallic additives such as zinc dialkylthiophosphate from the original lubricating oil formulation, sludge formed in the engine, and water.
  • the used oil may also contain contaminants such as waste grease, brake fluid, transmission oil, transformer oil, railroad lubricant, crude oil, antifreeze, dry cleaning fluid, degreasing solvents such as trichloroethylene, edible fats and oils, mineral acids, soot, earth and waste of unknown origin.
  • Reclaiming waste oil is mainly carried out by small processors using various processes tailored to the available waste oil, product demands, and local environmental considerations. Such processes at a minimum include partial de-watering and coarse filtering. Some more sophisticated processors may practice chemical de-metallizing or distillation. The presence of organo-metallics in waste oils such as zinc
  • dialkylthiophosphate results in decomposition of the zinc dialkyldithiophosphate to form a carbonaceous layer rich in zinc and often other metals such as calcium, magnesium and other metals present as additives and thus difficult if not impossible to process.
  • the carbonaceous layer containing the various metals forms rapidly on heated surfaces and can develop to a thickness of more than 1mm in 24 hours. This layer not only reduces the heat transfer coefficient of tubular heaters rapidly, it also results in substantial or total occlusion of these tubes within a few days.
  • Ash content can also be reduced by heating the used lubricating oil (ULO) to decompose the organo-metallic additives.
  • ULO used lubricating oil
  • Direct contact heating of ULO with a recycled bottoms fraction was disclosed in US 5,447,628 Harrison, et al., the contents of which are incorporated herein by reference.
  • the ULO was added to a lower section of a vacuum column with an enlarged bottom section. There was enough volumetric capacity below the first tray of the column to provide "a residence time of 10 to 120 minutes.”
  • the EXAMPLE reported that a dehydrated ULO fraction was mixed with a recycled bottoms fraction in the ratio of 1 :45 with a residence time of 45 minutes and a relatively constant temperature of 660°F.
  • the problem of fouling of heated surfaces can be ameliorated to some extent by gentler heating.
  • Some processes such as the fixed bed version of catalytic cracking, the Houdry process, used a molten salt bath to provide controlled, somewhat gentle heating of vaporized liquid hydrocarbon passing through tubes of catalyst immersed in the salt bath.
  • Molten metal baths have also been used as a convenient way to heat difficult to processes substances to a control temperature, e.g. flammability of some plastics is tested by putting a flask with plastic into a bath of molten metal.
  • molten salt bath or molten metal bath, or condensing high temperature vapor could be used to reduce uneven heating of heat exchange surfaces and thereby reduce ⁇ across said metal surfaces and perhaps slow the fouling of metal surfaces in ULO service, but the additives in the ULO would still tend to decompose on the hottest surface which would be the heat exchanger tubes.
  • a vapor injection ULO process was disclosed in US 6,068,759 Process for Recovering Lube Oil Base Stocks from Used Motor Oil and US 6,447,672 Continuous Plural Stage Heated Vapor Injection Process for Recovering Lube Oil Base Stocks from Used Motor Oil.
  • the heated vapor was steam, methane, ethane, propane or mixtures.
  • Other variations on the theme of ULO vapor injection are disclosed in US 6,402,937 Pumped Recycle Vapor and US 6,402,938, Vaporization of Used Motor Oil with
  • Nonhydrogenating Recycle Vapor which are incorporated by reference.
  • This approach used a "working fluid” such as methanol or propane which was heated and mixed with ULO to vaporize lube boiling range components.
  • a lube fraction was recovered as a product and the methanol or propane working fluid either compressed or condensed and pumped through a heater to be recycled to heat incoming ULO.
  • Vacuum distillation of ULO was used by Emerald Services Inc. to produce a material similar to a virgin lube blending stock.
  • Washington State studied this material for use as a ferry fuel, with the fuel being a 50/50 blend of recycled lube oil and Ultra Low Sulfur Diesel or ULSD.
  • the Washington State Department of Transportation reported the "re-refined fuel (blend) does not comply with the EPA requirements...
  • the issue... is the sulfur content.
  • the sulfur content is five times the allowable limit for use in the Emission Control Area (EC A)." Letter of Lynne Griffith, Assistant Secretary, Ferries Division to the Senate Transportation Committee, December 9, 2014. This letter is noted to make the point that some seemingly obvious uses of re-refined ULO as fuel are not options.
  • the brute force approach vaporizes the lubricant boiling range components, but can easily degrade the lube components and contaminate them with significant amounts of the breakdown products of the additive package.
  • the recovered lube boiling range components may have significant value as fuel or cracker feed blending component, but are generally not suitable for use as lubricant blending stock, at least not without a lot of expensive hydrotreating.
  • a superheated distillate boiling range material was the ideal material to use to heat and vaporize the used lubrication oil.
  • the superheated distillate could be recovered from an effluent of the used lube oil refining process, especially if the desired product is a lube blending stock or a stream that will be treated by hydrotreating or other treatment to make a lube blending stock.
  • a lube fraction recovered from the ULO is an ideal stream when a lube blending stock is sought.
  • an "outside” distillate boiling range material to form the superheated fluid.
  • Such an "outside” material need never have been used as a lubricant fraction and preferably has a significant aromatic content, making it thermally stable.
  • the ideal superheated distillate boiling range material would be a cat cracker feedstock which was too aromatic to be an ideal FCC charge material.
  • Refiners have known for decades that aromatic material is hard to crack, and they try to limit the amount of aromatics in the fresh feed to the unit. Refiners also try to limit the amount of aromatic rich material recycled within the FCC unit. These aromatic rich streams are hard to crack in the FCC unit because the aromatics are both thermally stable and relatively refractory to the cracking catalyst.
  • Thermal stability makes aromatic rich materials ideal for use as a superheated fluid for vaporizing used motor oil because they are relatively easy to superheat without fouling the furnace.
  • aromatic rich liquids such as a cycle oil or slurry oil from an FCC unit are used for ULO re-refining
  • the resulting product is a good cracker feed, although not ideal because of the high aromatic content.
  • the multi-ring aromatics typically found in such FCC streams do not become easier to crack because they contain significant amounts of aliphatic lube components, but the mixture still has significant value as cracker feed stock.
  • a recycled, recovered lube oil fraction will always be available from a ULO recycling plant so no outside source of feed is required.
  • the only drawback to using this material is that the highly paraffinic lube stock is readily cracked, both thermally and catalytically.
  • the key feature of our process is heating the ULO with a superheated distillate vapor.
  • This material can be either a recycled product fraction, a portion of the lubricant boiling range product recovered from the used lube oil fractionator or an "outside" distillate boiling range stream.
  • a recycled product fraction is essentially free of metals and additives and could safely be heated in a heat exchanger or fired heater. With no additives, there is no fear of fouling due to additive decomposition.
  • This fraction is always available downstream of the re-refining plant. It has a high boiling point, essentially the same as the boiling point of the lubricating oil components of the ULO feed to the process.
  • This vaporized lube fraction can be readily condensed at high temperature. By virtue of its high molecular weight, it carries a lot of energy with it when heated in a furnace or heat exchanger so that undue volumetric amounts are not required to achieve the desired amount of direct contact heating of ULO feed.
  • outside distillate stream can also be used. This requires a source of outside distillate material in addition to the ULO feed, but such materials are always available. Preferably these materials have been through one or more distillation steps so that relatively clean superheated vapor is used to heat and vaporize lubricant boiling range material from the ULO.
  • the high grade energy in the resulting mix of superheated vapor and vaporized distillate boiling range material recovered from contact with raw ULO feed may be used to preheat effectively and gently incoming ULO liquid feed for energy savings.
  • the resulting cooled and perhaps partially condensed lube fraction could also be split into a net product fraction removed from the process and a recycle fraction sent through a fired heater, heat exchanger or other heating means to generate the hot vapor needed to vaporize the ULO feed.
  • the relatively hot product liquid fraction could be used for a measure of preheating of ULO to, e.g. facilitate dehydration.
  • the condensed lubricant boiling range material recovered from the product is a relatively stable material, at least far more stable than the feed ULO. This stable material may tolerate a lot of heating by heat exchange with heavy residue material withdrawn from the product fractionator, heating in a fired heater or by heat exchange with some other high temperature heat source. While the paraffinic lubricant boiling range material is subject to thermal cracking, at least the only cracking products will be those typically experienced during mild thermal cracking of relatively pure hydrocarbons, a modest amount of olefins. Such a stream is a valuable product, especially as a lubricant blending stock. With hydro-processing it can produce a premium lube blending stock or fuel.
  • the same plant may shift from one type of superheated fluid to another.
  • a recycled or ULO derived superheated fluid may be used to produce a product relatively uncontaminated with aromatics.
  • the ULO re-refining process may shift to once through operation without recycle.
  • a purchased distillate boiling range feed such as FCC cycle oil is superheated and used to lift distillable components from the ULO, but there is no recycle.
  • the present invention provides a process for re-refining a used lubricating oil (ULO) containing lubricant boiling range hydrocarbons and a thermally unstable additive package which fouls metal surfaces used to heat said ULO to vaporize said lubricant boiling range hydrocarbons comprising direct contact heating of said ULO with a superheated fluid comprising at least a majority by weight of distillate boiling range hydrocarbons to form a heated mixture of said ULO and said superheated fluid, flashing or fractionating said heated mixture to produce a vapor fraction comprising at least a majority of the lubricant boiling range hydrocarbons in said ULO feed and a residual liquid fraction comprising said thermally unstable additives and a minority by weight of said lubricant boiling range hydrocarbons in said ULO feed, and cooling and condensing at least a portion of said vapor fraction to produce a liquid product comprising at least a majority of lubricant boiling range hydrocarbons in said ULO feed.
  • ULO used lubricating oil
  • FIGURE 1 is a simplified schematic drawing of an embodiment wherein used oil is heated by direct contact heating with a heated recycle vapor stream derived from the used oil feed.
  • FIGURE 2 is similar to FIGURE 1 but shows more detail and preferred heat exchange and control elements.
  • distillate boiling range hydrocarbons is meant to include normally liquid, but distillable hydrocarbons as defined by the US Energy Information Association in their Glossary on DISTILLATE FUEL OIL. Information from this government agency is copied below. This US agency used English units, and approximate metric conversions are indicated in parenthesis.
  • No. 1 Distillate A light petroleum distillate that can be used as either a diesel fuel (see No. 1 Diesel Fuel) or a fuel oil. See No.1 Fuel Oil.
  • Diesel Fuel A light distillate fuel oil that has distillation temperatures of 550 degrees Fahrenheit (288°C) at the 90-percent point and meets the specifications defined in ASTM Specification D 975. It is used in high-speed diesel engines, such as those in city buses and similar vehicles.
  • Fuel Oil A light distillate fuel oil that has distillation temperatures of 400 degrees Fahrenheit (204°C) at the 10-percent recovery point and 550 degrees Fahrenheit (288°C) at the 90-percent point and meets the specifications defined in ASTM Specification D 396. It is used primarily as fuel for portable outdoor stoves and portable outdoor heaters.
  • No. 2 Distillate A petroleum distillate that can be used as either a diesel fuel or a fuel oil.
  • No. 2 Diesel Fuel A fuel that has a distillation temperature of 640 degrees Fahrenheit (338°C) at the 90-percent recovery point and meets the specifications defined in ASTM Specification D 975. It is used in high- speed diesel engines, such as those in railroad locomotives, trucks, and automobiles.
  • the superheated fluid can be entirely from a recycle stream as discussed below in conjunction with the review of the figures or a purchased stream such as LCO or mixture.
  • a purchased outside stream is used, it is preferably a distilled material, but it can contain some non-distillable material, e.g. a mix of LCO and slurry oil can be used, with the net effect being that some of the slurry oil will remain in the bottoms or residual fraction after contacting ULO feed, permitting a greater percentage of the lubricating oil boiling range material in the ULO feed to be removed.
  • a very effective superheated fluid is one destined for charge to a cracking unit, e.g. a gas oil or vacuum gas oil obtained from a crude unit. This material is readily available in a refinery and ideal for use when the recovered fraction of the ULO will be fed to an FCC unit. Relatively large amounts of e.g. VGO may be used to lift lubricant boiling range components from ULO, and when large amounts of superheated fluid are used relative to ULO feed, the superheated fluid does not need to be heated as much.
  • as-received Used Lube Oil flows from a feed storage system not shown through line 10 into the atmospheric flash vessel 20.
  • the ULO feed has been preheated by means not shown to a temperature sufficient to permit atmospheric flashing of water and volatile hydrocarbons and subsequent vacuum flashing as discussed later of components boiling below the lube boiling or gas oil range.
  • Water and volatile hydrocarbons or other volatile material which flashes at say atmospheric pressure and 200°C are removed from the ULO feed via line 15 as a vapor. These vapors may be incinerated, used as fuel for heating needs of the process or otherwise treated.
  • There are other modes of operation where more or less material is flashed from the ULO, but in many applications removing the materials which flash at 200°C and atmospheric pressure will be preferred.
  • Dehydrated ULO is removed from vessel 20 via line 25 and charged to vacuum flash vessel 30.
  • a pressure control valve may be used to regulate flow from vessel 20 to vessel 30.
  • vacuum flash vessel 30 the temperature is slightly lower than the temperature in the atmospheric flash vessel as some cooling occurs due to flashing of water in vessel 20 and flashing of light hydrocarbons in vessel 30.
  • a vaporized hydrocarbon stream comprising gasoline and diesel boiling range components is removed via line 35 for cooling, condensing, and further handling by means not shown.
  • the net effect of these atmospheric and vacuum flashing steps is to produce a used lube oil fraction with a significant reduction in material boiling below 300 - 330°C, though it should be remembered that one or more simple flashing steps will not produce a "clean cut" material.
  • a flash stage is basically a distillation column with a single tray and such a device can only achieve a limited split of say 300 -330°C material in the bottoms and 300 -330°C material overhead. There will be considerable overlap in boiling range of the overhead vapor stream and the bottoms liquid stream.
  • a dehydrated somewhat de-volatized ULO fraction is withdrawn from vessel 30 via line 32 and charged to the inlet of inline mixer 34.
  • a recycle fraction or an outside source of fluid may be superheated for use herein.
  • all or almost all of the superheated fluid will be a recycled lubricant boiling range fraction.
  • a hot recycle fraction from a source hereafter discussed is also charged to the inlet of inline mixer 34 to produce a heated mixture of ULO feed and a recycled stream. This heated mixture is charged via line 36 to fractionator 40.
  • Light hydrocarbons are removed via line 45 while a liquid fraction comprising a majority of the lubricant boiling range components in the feed is withdrawn via line 46.
  • a portion of this liquid is withdrawn as a product fraction via line 48 while the remainder is recycled via line 50 through heat exchanger 60 to produce the heated recycle stream charged via line 54 to in line mixer 34.
  • a vacuum fractionator such as a steam jet ej ector, pumps, condensers, and reflux lines to the column. Removed from the bottom of vacuum fractionator 40 via line 42 is a residual product, which may be cooled by conventional means not shown and sent to storage.
  • the recycled fraction is heated in heat exchange means 60.
  • a circulating fluid enters the heat exchanger via line 72, heats the recycled lubricant rich fraction and is returned via line 74 to fired heater 70.
  • fired heater 70 Although a fired heater is shown, it is possible to use an electric heater or other source of hot fluid for use in heating the recycle liquid in heat exchanger 60.
  • the recovered lubricant boiling range material When the recovered lubricant boiling range material is to be used as cracker feed, some and preferably all of the superheated fluid is derived from an outside source such as gas oil, vacuum gas oil, even slurry oil, or other similar boiling range vaporizable liquid. These streams all tend to have more aromatics than a recycled lubricant boiling range fraction and therefore are easier to heat without forming coke.
  • the same equipment used to form superheated vapor from a recycled lube fraction may thus be used to form superheated vapor from an outside source of distillate hydrocarbons.
  • the simplified representation in Figure 1 omits many conventional details such as pumps, temperature controllers and the like, but these features are conventional.
  • the vacuum distillation column or columns should multiple column operation be preferred will have the following conventional components.
  • Working from the bottom up there can be a wash bed with sufficient wetting of surfaces to prevent coking or fouling. Above this will usually be a reflux section for heavy distillate comprising chimney trays, sieve trays, mesh packing or other structured packing, along with means for adding reflux liquid.
  • a similar section, for light distillate will usually be above this.
  • a de-mister will usually be added to an upper portion of the column so that fine particles of liquid may be recovered as a liquid and retained in the vacuum column rather than being entrained out with the overhead vapor.
  • de-misters may be added to each flash vessel to remove liquid mist entrained in a vapor product.
  • FIG. 2 shows more details including extensive energy conserving features.
  • only a single heater usually a fired heater is required to satisfy the heating needs of the process.
  • This approach also uses the energy in various
  • a ULO stream is charged via line 1 10 through at least one and preferably all of three heat exchangers 112, 114 and 1 16.
  • the fresh ULO feed can be first heat exchanged against a liquid product lube boiling range fraction being removed from the process.
  • This lube product typically about 70 - 90 LV % of the feed may be at a temperature of 150 - 260°C, typically about 200°C. It should be cooled prior to storage for safety reasons.
  • This lube product stream is at j ust the right temperature and has just the right volume to supply most or all of the preheating needs of the nrocess.
  • the ULO feed typically at 15 - 30°C in feed storage tanks is heat exchanged against a similar volume of lube product to produce a partially or totally if desired, preheated feed in line 113.
  • Heat exchanger 112 produces a ULO stream having a temperature of say 150°C in line 113.
  • the feed may be further heated in heat exchanger 114 by heat exchange against vapors removed from the vacuum distillation column 140, as discussed hereafter.
  • the overhead vapors from the column are theoretically at about the same temperature as the temperature of the condensed liquid removed from the overhead receiver.
  • Heat exchanger 114 can be used to cool and condense the hot overhead vapors from the vacuum column.
  • the condensing overhead stream can preheat the incoming ULO feed to the desired temperature.
  • the overhead vapor stream from the vacuum column typically contains two to three times more material on a molar basis than the feed ULO. It is possible to heat the ULO feed to something approaching the temperature of the vacuum column overhead vapor to within 20 - 40 degrees.
  • the temperature of the thoroughly preheated feed removed from exchanger 114 via line 115 will be say 160 -165°C or slightly higher depending on the amount of heat exchange capacity one wants to buy and the amount of pressure drop that can be tolerated getting vacuum column overhead vapors through the heat exchanger.
  • the use of heat exchangers in refinery processing is conventional, but what is unusual and beneficial is the use of selected streams for preheating that are unlikely to do any damage in the sense of decomposing the ULO feed.
  • the ULO feed is stable at temperatures encountered in a typical automobile engine and can easily tolerate temperatures of 200°C for extended periods and even higher for short periods.
  • the lube fractions recovered from the vacuum tower 140 are always below the temperature at which lube decomposition starts. If there are minor upsets, flow rate and even temperature of heat exchange liquid to heat exchangers 112 and 114 may fluctuate some, but the temperature in these exchangers should never be high enough to cause significant additive decomposition. This is in marked contrast to what happens if a fired heater is used for preheating.
  • a high temperature can be reached due to a temperature controller malfunction or some portion of the fired heater can have a hot spot or a stagnant region where tube wall temperatures increase. Flow slows, fouling starts and progresses and will soon lead to complete plugging of a fired heater.
  • This residual stream may also be used to preheat the ULO feed or a fraction thereof.
  • a ULO feed fraction is preheated by heat exchange against the column bottoms stream, some additive breakdown in the incoming ULO feed may occur and can be tolerated, especially if flow conditions are sufficiently vigorous so that "hot spots" do not develop and flow is fast enough to keep ULO feed moving rapidly through the exchanger.
  • the advantage of use of residual liquid as a heating medium is that it may be used to heat the incoming ULO feed to a higher temperature than can be achieved using only overhead product vapor or overhead product liquid.
  • the preheated ULO feed is charged via line 117 into atmospheric flash vessel 120 where water vapor and other light hydrocarbons are removed via line 119.
  • This material may be burned to supply heat needs of the process or incinerated to destroy contaminants that may be present.
  • Dehydrated ULO is then charged via line 125 to an optional in-line mixer 200 where the dehydrated ULO can optionally be further heated by direct contact heating with an outside superheated distillate stream, a superheated recycle product stream, or both as discussed in more detail hereafter.
  • the ULO is charged via line 127 to vacuum flash 130.
  • Reduced pressure in vessel 130 allows most hydrocarbons boiling below the lube oil boiling range to flash and be removed via line 135. This material may be burned as fuel for the re-refining process, incinerated or further processed and recovered as a product after conventional cooling and condensing.
  • the dehydrated less volatized used lube oil is withdrawn as a liquid from vacuum flash 130 and charged via line 132 to mix with a heated recycle product stream 174.
  • the two streams, ULO and the superheated vapor merge either in or immediately upstream of optional inline mixer 210.
  • the inline mixer is a preferred conventional device available from several manufacturers. It is optional since careful control of pipe sizing and flow can and preferably does generate fully developed turbulent flow, which does a good job of mixing two highly miscible fluids such as ULO and a superheated distillate boiling range fraction. Turbulent flow also keeps the pipe walls wet and somewhat "scrubbed" lessening the chance of fouling or plugging of pipe walls.
  • the mixture of ULO and added superheated vapor will generally be discharged as two phases, vapor and liquid, into vacuum fractionator 136.
  • This material will generally be at a temperature of 260 -400°C, preferably 290 - 345°C, ideally 300 - 330°C.
  • This mixture should be at a temperature sufficient to vaporize in the conditions existing in the vacuum fractionator, at least 60 -90, and preferably about 80 mole % of the lubricant boiling range components in the incoming ULO feed. It is possible using pumps and a pressure reducing valve to keep the material largely or perhaps entirely in the liquid phase, but it will usually be at enough pressure to get the combined liquid stream of. ULO and recycled product through the piping and mixer if used and into the vacuum column 140.
  • Vacuum column 140 is preferably a conventional distillation column with enough trays or internal packing material to help separate lube oil boiling range materials from heavy materials.
  • the primary and preferably the sole means of heat input into the column is the high temperature of the feed stream to the column.
  • the mixture of ULO and injected superheated vapor whether recycled or fresh should be heated by the injection of superheated fluid to a temperature sufficient to achieve the desired amount of vaporization in the vacuum column. There must be enough heat in the feed stream to vaporize entirely the recycled lube stream used for heat input and the desired amount of lube oil components to be recovered from the ULO.
  • lube boiling range materials typically, 50 to 90 %, preferably 70 to 85 %, and ideally 70 % of the lube boiling components in the ULO will be recovered as a product. If not enough energy is added to the column in the form of a hot feed mixture, less lubricant boiling range material will be recovered with overproduction of the generally less valuable residual fraction. There is an upper limit on feed vaporization because it is important to leave some lubricant boiling range materials in the bottoms product to permit its withdrawal as a liquid and facilitate further handling. This material has value as an asphalt extender, addition to coker feed, or other uses. Vaporized lubricant boiling range materials are withdrawn overhead from vacuum fractionator 140 via line 145. Although it is possible to use conventional methods of handling this material, e.g.
  • vaporized lube boiling range hydrocarbons for heat exchange in this process.
  • the temperature of the overhead vapor generally 150 - 200°C, typically 175 - 180°C, makes it ideal for preheating of fresh ULO feed.
  • the moderate temperature of the vaporized lube boiling range material is ideal for preheating ULO feed without decomposing it.
  • hot overhead vapor is charged via line 145 to heat exchanger 114 as previously discussed, to heat incoming fresh ULO feed. This heat exchange may condense enough overhead vapor to permit recovery of the desired amount of liquid for column reflux, product recovery and for use as a recycled heating medium in in-line mixer 210. If the amount of heat exchange in exchanger 114 is not sufficient to produce enough condensed liquid, then additional cooling may be done by heat exchange with water, not shown, or use of fin fan coolers 214 with the condensed liquid charged via line 216 to overhead receiver 250.
  • Preferably essentially all overhead vapor removed from the vacuum column is condensed since the lighter materials will usually have been removed either by the atmospheric flash 120 or vacuum flash 130. Some light ends may remain, and these will be removed from the process via line 255, connective with a conventional vacuum means such as a steam jet ejector, not shown. Depending on how "hard” the process is run, there may be some breakdown of additive package components or thermal cracking of the lubricant boiling range hydrocarbons.
  • the vacuum system should be sized large enough to handle these low boiling materials.
  • the cooled and condensed lubricant boiling range materials are collected in overhead receiver 250.
  • the desired amount of reflux is charged via line 260 back to the vacuum column and the remainder passes via line 265 for product recovery and recycle.
  • the net production of lubricating oil boiling range materials is withdrawn as a liquid via line 270.
  • This liquid is usually still hot as the condensing system preferably removes just enough heat to condense the overhead vapor and not to cool it further.
  • the recovered lube product should be cooled before storage.
  • This stream is typically 60 - 90 Liquid Volume % (LV %) of the dehydrated ULO feed, preferably about 80 %, and is an ideal stream for charging via line 270 for heat exchange with incoming ULO feed in exchanger 112.
  • the product is a liquid so a compact L/L heat exchanger may be used.
  • the product liquid in line 270 is one of the "coolest" streams in the plant though considerably warmer than the ULO feed so it may be safely used to heat incoming ULO with little or no risk of thermally degrading the feed.
  • the net production of lubricating oil boiling range hydrocarbons is removed from the plant via line 271 and charged to storage tanks, not shown.
  • the remaining portion of lubricant boiling range hydrocarbons is charged as a liquid via line 272 for superheating and reuse in the process to vaporize distillable components from the feed ULO.
  • To that end recycled product must pass through a heater such as fired heater 170 to produce a superheated stream charged via lines 172 and 174 to mix with the dehydrated ULO feed in line 132 withdrawn from vacuum flash vessel 130.
  • the recycle product is first heat exchanged against bottoms fraction withdrawn from vacuum column 140, namely the residual fraction 142.
  • This residual fraction representing perhaps 10 - 40% and preferably about 20 LV % of the ULO is withdrawn as a liquid from the bottom of the column usually at a temperature near that of the feed temperature entering the column.
  • the bottoms product withdrawn from the vacuum column 140 may also be used to achieve additional preheating of ULO feed by heat exchange against ULO feed in exchanger 116.
  • heat exchange of the unstable ULO feed is done only when the column bottoms fraction has been cooled to some extent by heat exchange or other cooling so that the bottoms fraction is at a temperature below that which will cause thermal cracking or degradation of ULO feed. After such optional heat exchange and further cooling or energy recovery by means not shown, the bottoms fraction is recovered as a heavy product of the process and charged via line 212 to product storage not shown.
  • the heated recycle material withdrawn from the furnace 170 via line 172 may also be charged via line 176 to mix with liquid withdrawn from the atmospheric flash vessel 120. This may be done when e.g. the feed ULO contains a relatively large amount of gasoline or other lighter boiling components which are to be recovered in the vacuum flash vessel 130. If higher temperatures are needed in vacuum flash 130, mixing ULO with some heated recycle product is an easy way to achieve such heating. Mixing may occur simply by in line mixing as the fluid flows through the pipes or preferably in-line mixer 200 may be used to facilitate rapid mixing. DESCRIPTION OF PREFERRED EMBODIMENTS
  • Any feed containing a normally liquid hydrocarbon can be heated using the process of the present invention.
  • the normally liquid hydrocarbons include C5 and heavier hydrocarbons e.g. naphtha boiling range up through residual fractions.
  • Heavy feeds are contemplated for use herein including those which are so heavy that they are not liquid at room temperature e.g. grease, wax, petrolatum or indeed any hydrocarbon having a high melting point may be used as feed. These materials will upon heating form liquids and may be used as feed.
  • Treatment of solids is outside the scope of the present invention i.e. treatment of coal or dirt contaminated with oil. What is essential for the practice of the present invention is that the feed have at least some distillable components boiling above the gasoline boiling range and direct contact heating of the feed by mixing with a superheated stream comprising e.g. lubricant or gas oil boiling range hydrocarbons.
  • ULO is the feed contemplated for primary use herein.
  • the ULO will frequently contain both light and heavy contaminants and large amounts of paraffinic hydrocarbons in the CI 6 to C50 range.
  • Light contaminants include water, naphtha and some impurities introduced during the ULO collection process.
  • Heavy contaminants include the additive package.
  • the economic incentive is usually to vaporize as much ULO feed as possible. This can create a problem as the residue will not flow when too much of the feed is vaporized. About 60 - 90% vaporization of the dry used oil will usually be the target, with 80 LV % vaporization of dehydrated ULO feed giving good results.
  • ULO is the most difficult to re-refine of industrial waste oils, but other waste or low value oil containing liquids may be treated as well.
  • fluids which may be treated include cutting oils, crude oil emulsions, tank bottoms and any of the myriad other materials mentioned in the voluminous art discussed above on re- refining of used lubricating oil, all of which are incorporated herein by reference.
  • the process can tolerate some sediment and solids provided the plant is built so that large sized particles can be filtered and small sized particles can be carried out with the residual liquid fraction without clogging the plant.
  • This step will usually be run at a temperature above 90 - 100°C, preferably above 150°C and most preferably at 200°C or more.
  • the pressure will usually be atmospheric to simplify construction and operation, but it may be operated under vacuum when desired.
  • the temperature and pressure should be sufficient to remove at least a maj ority and preferably at least 90 mole % of the water in the feed.
  • this step removes a maj ority of the gasoline and lighter boiling range components although in some circumstances it may be beneficial to have a first flash that removes water and light naphtha and other light materials that may be present, followed by a second flash at lower pressure or higher temperature to remove gasoline boiling range components, say those boiling below 200 - 210°C.
  • This preferred but not essential step removes those molecules from the ULO which can be flashed at relatively mild conditions. This will include some gasoline components and some lubricant boiling range components.
  • the vacuum flash will typically be at the same or a higher temperature than the initial dehydration treatment. The vacuum flash will be at a lower pressure to facilitate flashing of molecules boiling below the lube oil boiling range. This flash will usually be a simple flash in a flash drum equivalent to a one theoretical tray distillation column. Where desired a conventional vacuum distillation column may be used, but for most purposes a simnle flash drum will be sufficient and will be all that is used.
  • the vacuum flash removes a poorly defined fraction comprising heavy gasoline and lighter lubricant boiling range components. This material will usually have significant value as a fuel for use in the re-refining process or for sale.
  • the temperature in the vacuum flash will typically be 150 - 350°C, preferably 200 - 315°C, and ideally about 200 - 210°C.
  • the pressure will typically be 5 to 250 mm Hg, preferably 10 to 200 mm Hg, ideally about 20 - 50 mm Hg. Temperature and pressure are related. When a relatively clean feed with little in the way of light ends is being processed or when a robust vacuum system is available, it is possible to run the vacuum flash at the lower range of temperature and with a higher vacuum. If the feed is heavily contaminated or if for some reason light ends are being generated due to thermal cracking in the system, or if the vacuum system is not working well, then higher temperatures will be required to remove the desired amount of distillable hydrocarbons in the vacuum flash.
  • the main function of the vacuum flash is to recover as much as possible in the way of distillable liquids from the ULO feed at conditions which cause no or only modest amounts of thermal cracking of ULO feed or decomposition of thermally decomposable materials in the ULO feed such as the additive package.
  • the vacuum flash preferably removes most or all of the materials which are recoverable from a ULO feed using conventional technology. There is no need to use a superheated fluid to remove gasoline when simple heating of the ULO by conventional means will suffice.
  • re-refiners can omit the flash and just send the ULO feed through one or more preheating steps, one or more conventional fired heaters and charge sufficient superheated distillate to lift the desired amount of material from the ULO feed.
  • Such a simple plant will usually be cheaper to build and this approach may be satisfactory when the distillate boiling range portion of the product can profitably be sold as a crude component or blended into the feed to an FCC unit.
  • Thermal cracking of hydrocarbons is a function of time and temperature and the nature of the hydrocarbon.
  • the earliest cracking processes e.g. the Dubbs process subjected a heavy crude oil fraction to high temperatures cracking some of the larger molecules to form some light ends and other lighter molecules.
  • the formation of smaller molecules from bigger ones meant that the product contained not only viscous, heavy, long-chain feed molecules but some lighter ones as well that were less viscous.
  • Refiners could make a low viscosity product by cracking a heavy feed sufficiently so that the feed made its own cutter stock hence the name "visbreaking" for one type of early cracking process.
  • Thermal cracking is not all bad, but in most instances we prefer that our plant be run to minimize thermal cracking. Thermal cracking is an important parameter and frequently a limiting factor on severity so it is reviewed below.
  • reaction rate doubles for every 12 to 13°C increase in temperature.
  • 60 seconds of residence time at 427°C is equivalent to 60 ERT, and increasing the temperature to 456°C would make the operation five times as severe i.e. 300 ERT.
  • 300 seconds at 427°C is equivalent to 60 seconds at 456°C, and the same product mix and distribution should be obtained under either set of conditions.
  • the visbreaking process conditions which may be used, or which can be tolerated, depend to some extent on the amount of thermal cracking of ULO components which can be tolerated.
  • processing severities are typically in the range of an Equivalent Reaction Time of 250 to 1500 ERT seconds. In general terms, this is about an order of magnitude more cracking than is desired or required for ULO re- refining.
  • ERT Equivalent Reaction Time
  • the recovered lube product is destined for reuse as a lube blending stock, it will be beneficial to limit ERT to 25 or less, with an ERT of 2 - 10 being most preferred.
  • ERT is a significant constraint or at least a guideline for the operation of the heater, the mixing zone and the vacuum flash. ERT in effect can be an upper limit on severity. Another constraint is operating the vacuum column at a temperature and pressure sufficient to vaporize the desired amount lubricant boiling range hydrocarbons in the ULO feed. Distillation is a function of temperature and pressure alone, save for any thermal cracking of lube or degradation of additive materials which may occur in the vacuum column. Successful recovery of a desired amount of lube product requires a minimum temperature, while limiting thermal cracking involves time and temperature. The heater, mixing zone and vacuum column should be operated to keep the ERT severity at a relatively low level.
  • ZDDP zinc dialkyldithiophosphates
  • the vacuum column must run hot enough and at a low enough pressure to allow vaporization of the desired amount of lubricant boiling range material.
  • the ULO feed should not be subjected to excessive reaction severity since this severity will produce extended thermal cracking and some downstream additive degradation, primarily in the bottoms of the vacuum column. Finally, the additive material should not be exposed to hot metal surfaces, lest these start fouling.
  • a superheated fluid of distillate or a recycled lubricant boiling range stream as the heating medium to heat the ULO feed solves the most significant problem which is additive induced fouling of metal surfaces.
  • the hottest thing to which the ULO feed is exposed is a completely miscible material i.e. a superheated fluid of either vaporized outside distillate hydrocarbons or recycled lubricant boiling range material derived from the ULO feed.
  • a superheated fluid of either vaporized outside distillate hydrocarbons or recycled lubricant boiling range material derived from the ULO feed.
  • Some additives may decompose, but they will not preferentially deposit upon hot metal surfaces since the metal surfaces are cooler than the fluid contained or flowing in them. Small amounts of additive decomposition are not desired but can be tolerated.
  • the lubricant boiling range material recovered as a product of the process is a distilled material.
  • refiners knew that the catalysts and technology available could not tolerate the "heavy ends" of the feed usually because of metals content.
  • the metal problems were left behind in the crude column used to prepare cat cracker feed.
  • the troublesome additives are left behind in the vacuum column so the recovered product is essentially free of metals.
  • gas oil recovered from a crude column in the early days of refining our gas oil recovered from vacuum distillation of ULO is free of metals.
  • Thermal cracking of the recycled lubricant boiling range fraction during heating, or superheating may be minimized in several ways.
  • a fired heater it is possible to reduce the residence time of the recycled gas oil by sizing the heater for high superficial velocities in the tubes and designing the heater to minimize high tube wall temperatures.
  • coker heaters it was reported that great variability in heater performance or run length was observed. The author reported that some heaters had coil outlet temperatures of 399 - 405°C (750 - 760°F) and low flux rates, but could run for only 2 years, while others had higher outlet temperatures and flux rates and ran for four years. Different techniques were discussed which could be used to reduce residence time of oil feed in the furnace, both overall and at high temperature.
  • the temperature required to vaporize lube oil boiling range hydrocarbons is less than that required for efficient operation of a coker, but the principle is the same. Careful furnace design can minimize high temperature experienced by the oil in the furnace.
  • a fired heater can produce a high temperature fluid, and this can be heat exchanged against a recycled gas oil fraction.
  • the tubes in a fired heater can easily be 30 - 55°C higher than the target discharge temperature so oil being heated can start to coke.
  • a fluid such as a thermally stable heat transfer fluid which is hotter than the recycled gas oil but not nearly as hot as the radiant or convection section of a fired heater. It is possible to operate with a heat transfer fluid having a temperature of say 400°C when heating a recycled gas oil fraction to 385°C. The highest temperature the recycled gas oil will experience is that of the heat transfer fluid at 400°C. Had a fired heater been used, the recycled gas oil could easily see a tube wall temperature of 425 - 430°C or higher.
  • Suitable heat exchangers include the Sulzer SMXL multitube or monotube.
  • an "outside” material When an "outside" material is used for the superheated fluid rather than a recycled one, it should be a relatively clean stock preferably obtained by distillation. These will heat the ULO feed, but the residual streams will end up in the residue of the ULO re- refining process. Distilled materials form a superheated fluid generally free of metals so the recovered lubricant boiling range material lifted from the ULO feed will also be metal free and an ideal feed for an FCC or other refinery processing unit. Various refinery streams may be used to form the superheated fluid, such as kerosene, jet fuel, gas oil, vacuum gas oil and many others. At least a majority by weight of the "outside” material should boil above 175 - 200°C and below 535 - 565°C.
  • LCO Light Cycle Oil
  • an aromatic rich material which is one of the products of the FCC process. If the distillate product recovered from the ULO will be sold as an FCC feedstock, there is some penalty because highly aromatic light cycle oil is not a desirable material for an FCC because it is difficult to crack.
  • Our process may be unique in permitting recovery of up to 90 to 95% of the lubricating oil boiling range hydrocarbons in the ULO by distillation and recovery of a pumpable ULO residue product.
  • Sufficient superheated fluid should be injected to "lift” or vaporize at least a majority by weight of lubricant boiling range hydrocarbons in the ULO feed.
  • a feed preparation step is conducted before contact with superheated fluid, dehydration and/or an initial flashing step is practiced, which will remove some lubricant boiling range hydrocarbons.
  • the ULO may be treated either "raw” or as received or after one or more feed preparation steps, and some lubricant boiling range material removal may occur prior to contact with superheated fluid.
  • This portion of the process mixes directly the superheated distillate vapors whether recycled lubricant boiling range hydrocarbons recovered from the product or outside distillate boiling range hydrocarbons with the incoming ULO feed.
  • the superheated fluid should be used at a temperature and in amount sufficient to achieve the desired temperature and desired amount of product uplift, in the vacuum column.
  • direct contact heating can occur in a simple length of pipe.
  • the fluids will be flowing at high velocity in fully developed turbulent flow which is an effective method of mixing ULO feed with superheated lubricant boiling range hydrocarbons.
  • ULO feed and recycled superheated fluid using an in-line mixer such as the Sulzer Compax.
  • This device if used may be placed near the heater or heat exchanger outlet but is preferably placed near the inlet of the vacuum flash vessel for mixing of the superheated recycled hydrocarbons with ULO feed.
  • multiple mixing elements create turbulent flow and good mixing. Uniform mixing can be achieved within three pipe diameters downstream of the injection point.
  • Other in-line mixing devices may be used, if desired.
  • the process of the present invention using a superheated distillate material to heat ULO, is a breakthrough in ULO processing. Quite a lot of heat or energy is added via the superheated fluid, enough to vaporize the desired amount of lubricant boiling range material in the ULO feed and to maintain most, preferably all, of the added superheated fluid in the vapor phase. Using this approach, the ULO feed need never be exposed to heated metal surfaces. The hottest thing the ULO "sees" is a superheated fluid which is generally compatible with the ULO feed. The heat needs of the process are met by heating either a relatively clean distilled product, the lubricant boiling range hydrocarbons recovered from the ULO feed, or by heating an outside distillate material.
  • Thermal cracking of the superheated material can be reduced by selection of a stable material and/or by careful design of any fired furnace used for heating thereof.
  • the material destined for superheating may be gently preheated by heat exchange, thus limiting the amount of heating or superheating to be done in a furnace.
  • Further reduction in thermal cracking of superheated material may be achieved by incorporating into the tubes, whether used in the heater or a heat exchanger, in line mixers or wall wipers that move oil from the metal tube walls to central portions of the tube, thereby reducing extended exposure of oil to high temperatures at the tube wall.
  • the ULO feed is efficiently mixed with the superheated fluid by direct contact in a pipe operating with turbulent conditions and/or using an in-line mixer.
  • the process will be run to maximize production of this stream. If a lubricant product is desired, it may be beneficial to flash and/or fractionate enough lighter hydrocarbons to minimize the amount of distillation required for the lubricant product.
  • the plant can consist of a heater, a length of pipe and a vacuum flash.
  • the heater can be a simple fired or electric heater to superheat the distillate.
  • a length of pipe will suffice as a contacting zone where fresh ULO feed and superheated fluid are mixed.
  • the mixture can be discharged from a pipe or across a valve into a vacuum flash where most of the ULO feed by weight is removed as an overhead vapor along with most and preferably all of the injected superheated fluid. In such a simple plant the separation between lubricant boiling range components and the residue fraction will be poor.
  • a fired heater or electric heater may be used to superheat the fluid charged to the ULO vaporizer and when a material such as LCO is used a simple design is possible for the heater as LCO is tolerant of rough heating.
  • the residual liquid remaining after processing is a source of high grade heat which may be used to preheat the ULO feed or, preferably, the superheated fluid.
  • the liquid residue additive concentration has been significantly increased due to the "lift" of the lubricant boiling range components from the ULO so it should be removed from the process and cooled relatively quickly.
  • a hybrid approach on superheated fluid can also be used when desired. For example, some heating can be achieved with recycled superheated lubricant fluid followed by heating taken to completion with superheated LCO or the like. In some circumstances it may be beneficial to use a blended superheated fluid or a mix of recycled lubricant boiling range materials and purchased distillate.
  • the residue fraction resulting from ULO processing should contain enough normally liquid hydrocarbons to permit handling of this material. Because the "lift" of lubricant boiling range hydrocarbons from the ULO can be done quickly, it is possible to run the process with greatly reduced breakdown of the additive package. This can be beneficial when some portion of the ULO residual has value in other products e.g. the polymer viscosity modifier can be a valuable blending component in asphalt. Minimizing additive breakdown will also improve the quality of lubricant boiling range hydrocarbons recovered as a product which may be of minor or major importance depending on the use of this product. The residue fraction must have enough normally liquid hydrocarbon to flow out of the vessels and to permit pumping and conventional handling.
  • the lubricating boiling range fraction recovered by our process has exceptional value as an FCC stock. This is important for several reasons. There are hundreds of FCC units in the USA and over 400 worldwide so there are many markets for recovered lube boiling range product. Although it will typically be a small part of the feed blend to an FCC, refiners know that gasoline yields are strongly affected by hydrogen content of the feed. Increasing the hydrogen content of the feed from 11.1 to 13.1 increased gasoline yields from a typical FCC unit from under 52 LV % to over 69 LV %.
  • Typical used lube oil fractions have a hydrogen content of 13 - 14 wt % so the lube boiling range material recovered by our process will also be hydrogen rich. A recovered lubricant boiling range material can be a very important even if relatively small part of the feed to an FCC.
  • Our recovered lube boiling range product will also have value as a fuel or blending stock, but the requirement to use ultralow sulfur fuels or other fuel quality regulations may prohibit its use as fuel in many areas. There will usually be some sulfur in our product as sulfur compounds are an important part of lubricating oil. Such modest sulfur amounts are not a hindrance to use of our product as FCC feed.
  • the residual liquid product of our process can be used as an asphalt extender.
  • the exceptional low severity processing that lifts the lubricating oil boiling range molecules from the ULO feed preserves most and preferably essentially all of the polymer rich additive package. This material will have little or no smell either at ambient or at temperatures required during construction of asphalt roads. We smelled the cooled material produced in our laboratory work, and it had no smell.
  • US6270657B 1 which used steam to lift lube oil from ULO, our material should have even less of an odor concern when used in an asphalt blend. Steam can be a reactive material at the temperatures needed to vaporize lubricant boiling range hydrocarbons, and our hydrocarbon material will have no or greatly reduced reactivity with ULO.
  • Our process provides a cost effective way to recycle ULO.
  • a relatively large plant can be used for central collection and re-refining.
  • a working plant can be made with a single superheater for distillate, a pipe for contacting of ULO with superheated distillate and a vacuum flash for separation of lubricant boiling range vapors from a residual liquid phase.
  • Such a small plant will not be as enersv efficient as a larger one which can take advantage of multiple heat exchange steps, but in some locations recycling ULO at low cost and with a low capital investment is more important than doing so with optimum energy efficiency. Because of the simplicity of our process, it may be skid or truck mounted permitting small mobile units to process the ULO where it may be found.

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Abstract

L'invention concerne un procédé et un appareil pour le reraffinage d'huile lubrifiante usagée (HLU) présentant des additifs thermiquement instables tels que des composés de zinc. L'HLU est mélangée avec une vapeur de distillat surchauffée, un flux de recyclage, un flux extérieur ou une combinaison puis chargée sur un dispositif d'évaporation instantanée et/ou une colonne de fractionnement pour produire une vapeur de tête et une fraction résiduelle comprenant les additifs et/ou des produits de décomposition correspondants. La vapeur de tête est condensée pour obtenir un produit liquide d'hydrocarbures à ébullition lubrifiante qui peuvent être recyclés. La surchauffe peut avoir lieu dans un dispositif de chauffage à combustible. Le mélange du fluide surchauffé et de l'HLU peut avoir lieu dans une conduite, de préférence en écoulement turbulent, et peut utiliser un mélangeur en ligne. Le rendement énergétique est amélioré par échange de chaleur de l'alimentation en HLU avec des produits liquides ou sous forme de vapeur. Un flux riche en aromatiques thermiquement stable, tel que du gasoil ou une huile légère recyclée (light cycle oil - LCO) de CCF, peut être surchauffé. Le produit récupéré peut être utilisé comme carburant, huile lubrifiante ou charge d'alimentation de CCF.
PCT/US2016/013764 2016-01-17 2016-01-17 Distillation d'huile moteur usagée avec des vapeurs de distillat Ceased WO2017123260A1 (fr)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114195312A (zh) * 2021-12-17 2022-03-18 湖北润驰环保科技有限公司 一种废润滑油废水净化工艺

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS4870659A (fr) * 1971-12-25 1973-09-25
US4406743A (en) * 1981-06-15 1983-09-27 Phillips Petroleum Company Fractionation column for reclaiming used lubricating oil
US6106699A (en) * 1997-04-29 2000-08-22 Probex Process for de-chlorinating and de-fouling oil
WO2001090283A1 (fr) * 2000-05-22 2001-11-29 Marathon Ashland Petroleum Llc Rupture d'emulsion par condensation

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS4870659A (fr) * 1971-12-25 1973-09-25
US4406743A (en) * 1981-06-15 1983-09-27 Phillips Petroleum Company Fractionation column for reclaiming used lubricating oil
US6106699A (en) * 1997-04-29 2000-08-22 Probex Process for de-chlorinating and de-fouling oil
WO2001090283A1 (fr) * 2000-05-22 2001-11-29 Marathon Ashland Petroleum Llc Rupture d'emulsion par condensation

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114195312A (zh) * 2021-12-17 2022-03-18 湖北润驰环保科技有限公司 一种废润滑油废水净化工艺

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