[go: up one dir, main page]

WO2001090283A1 - Rupture d'emulsion par condensation - Google Patents

Rupture d'emulsion par condensation Download PDF

Info

Publication number
WO2001090283A1
WO2001090283A1 PCT/US2000/013990 US0013990W WO0190283A1 WO 2001090283 A1 WO2001090283 A1 WO 2001090283A1 US 0013990 W US0013990 W US 0013990W WO 0190283 A1 WO0190283 A1 WO 0190283A1
Authority
WO
WIPO (PCT)
Prior art keywords
umo
vapor
water
boiling range
phase
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/US2000/013990
Other languages
English (en)
Inventor
Howard F. Moore
Donald P. Malone
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Marathon Petroleum Corp
Original Assignee
Marathon Ashland Petroleum LLC
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Marathon Ashland Petroleum LLC filed Critical Marathon Ashland Petroleum LLC
Priority to AU2000252800A priority Critical patent/AU2000252800A1/en
Priority to PCT/US2000/013990 priority patent/WO2001090283A1/fr
Priority to CA002406985A priority patent/CA2406985C/fr
Priority to MXPA02011615A priority patent/MXPA02011615A/es
Priority to EP00937657A priority patent/EP1309668A4/fr
Publication of WO2001090283A1 publication Critical patent/WO2001090283A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • 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
    • C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
    • C10G31/06—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment
    • 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
    • C10G33/00—Dewatering or demulsification of hydrocarbon oils
    • 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
    • C10M175/04—Working-up used lubricants to recover useful products ; Cleaning aqueous emulsion based

Definitions

  • the invention generally relates to the reprocessing of Used Motor Oil (UMO) and specifically to selective condensation of steam and hydrocarbon vapors derived from such a process.
  • UEO Used Motor Oil
  • WFE Wiped Film Evaporators
  • Some re-refiners used filtration and/or solvent extraction, some with pretreatment with acids or bases.
  • the present invention deals with a troublesome, vapor product stream which can be generated by some UMO processes, i.e. a vapor phase stream comprising significant amounts of water vapor, vaporized normally liquid hydrocarbons boiling in the lube oil range and polymer and/or other surface active agents added to the virgin lubricating oil.
  • This UMO vapor phase may also contain gasoline boiling range components and/or solvents.
  • the UMO processing reactor or fractionator is run at sufficient temperature to recover significant portions of the lubricating oil boiling range components present in the UMO, then large amounts of surface active materials end up in the overhead vapor phase. If this vapor is condensed, the surfactants and/or other vaporized additives and the native water or steam added during UMO processing form a stable emulsion with the lubricating oil boiling range components. Used oil and water can mix and form a stable emulsion in the presence of the robust surfactants in modern motor oils. This emulsified product of UMO processing can be as troublesome to work with as the
  • the present invention provides a process for refining UMO feed comprising 0-50 wt.% water, 0-15 wt.% gasoline and lighter, normally liquid hydrocarbon components, at least 50 wt.% lube oil boiling range components, and a sufficient amount of vaporizable detergents and/or surface active agents (surfactants) to form an oil/water emulsion when vaporized lube oil boiling range components are condensed in the presence of steam or water comprising heating and partially vaporizing said UMO feed to produce a UMO overhead vapor phase comprising essentially all of the gasoline boiling range components which may be present, at least a majority of the lubricating oil boiling range components in the UMO feed, and a sufficient amount of detergents and/or surfactants to produce an overhead vapor fraction which can be condensed to form an emulsion of oil and water; cooling to a temperature above the boiling point of water and partially condensing from said UMO 75 overhead vapor at least a majority of said gasoline boiling range components,
  • the present invention provides a process for reprocessing a UMO and water emulsion comprising surface active agents, gasoline boiling range components, lube oil boiling range components, and surfactant additives comprising heating said UMO at least in part by the direct injection of steam in an 5 amount, and at a temperature, sufficient to vaporize essentially all of said gasoline, essentially all of said water, at least a majority of said lube boiling range components, and at least sufficient surfactants to produce a UMO reactor overhead vapor stream which will form an oil/water emulsion if cooled to the dew point to produce liquid water; cooling, partially condensing and separating said UMO reactor overhead vapor
  • FIG. 1 is a simplified process flow diagram of a preferred embodiment of the invention.
  • UMO in line 1 is charged to thermal reactor or vaporizer 10.
  • the UMO is heated by direct injection of superheated steam from line 5.
  • the UMO is typically preheated by one or more indirect heat exchange means not shown with various hot effluent streams created by the UMO plant or that may be found in a refinery or other nearby process unit.
  • Thermal reactor 10 may be insulated but need not be heated and preferably does not have a fired heater associated therewith.
  • UMO overhead (OH) vapors are removed via line 17, pass through heat exchange means 20 and charged to hot separator 30.
  • Hot separator 30 operates at a temperature low enough to condense essentially all of the diesel and/or lubricating oil boiling range components, all or almost all of the gasoline boiling range components, but essentially no liquid water.
  • the condensed liquid hydrocarbon phase will contain significant amounts of volatile surface active materials, polymer, and the like present in the UMO charge.
  • the surfactants will be present in an amount sufficient to form an emulsion if the UMO vapor stream was cooled enough to produce liquid water.
  • the careful, partial, condensation of hot UMO reactor vapors ensures that a dry, liquid hydrocarbon stream is produced, which is removed via line 35.
  • Hot separator overhead vapors essentially steam or other injected superheated vapors
  • conditions upstream in the UMO vaporizer 10 and in hot separator 30 are adjusted so that only a water phase forms in receiver 50. This water phase will contain a modest amount of dissolved hydrocarbons and may be discharged via line 55 into sewer means 64 for further conventional wastewater treatment.
  • Figure 2 is a more detailed process flow diagram of a steam heated UMO process using emulsion breaking by condensation.
  • UMO feed in line 101 is heat exchanged in heat exchanger 1-99-E-4 and 1-99- E-l to produce a pre-heated feed which is discharged into pre-flash drum 1-99-F-l.
  • a pre-flash drum overhead vapor stream is removed via line 2 and charged into the hot- flash separator.
  • the flashed feed is removed from the pre-flash drum and pumped via line 3 into one of four thermal swing reactors, 1-99-D-l, 1-99-D-2, 1-99-D-3, or 1-99- D-4.
  • Hot UMO OH vapors are removed from the #2 thermal reactor, 1-99-D-2, and quenched by heat exchange with boiler feed water, then heat exchanged against UMO feed and then charged to hot flash separator 1-99-F-2.
  • a hot vapor phase is removed at 300°F, cooled in fin-fan cooler 1-99-E-5 and charged via line 6 to wastewater treatment.
  • a liquid hydrocarbon, gas oil product phase is removed from the hot flash separator and charged via line 7 as a gas oil product phase.
  • gasoline boiling range means hydrocarbons having the boiling range of conventional gasoline fuels.
  • distillate or lube oil boiling range hydrocarbons means normally liquid hydrocarbons boiling above the gasoline boiling range, above 300°F, typically above 350 or even 400°F. Most distillates present will boil in the range of 400-650°F.
  • the UMO is preheated by heat exchange with process streams or steam so it has a temperature of at least 300°F. Mild preheating in a fired heater is also possible. Preheating above 400°F should be avoided because at such temperatures fouling of heat exchange surfaces can occur. Fouling will occur rapidly above 500°F. If a refiner does not mind frequent shutdowns for removal of heat exchange deposits, it is possible to have even higher preheat temperatures. More heat exchange is thermally beneficial, though in commercial practice it is believed that the benefits of more preheat will not be offset by the aggravation of more downtime for maintenance.
  • UMO UMO
  • a pre-flash step it may be beneficial to subject the UMO to a pre-flash step to remove some of the light ends, water, solvents and the like that may be present.
  • This can partially, or completely, dehydrate UMO feed to the thermal reactors. Removal of the gasoline boiling range hydrocarbons and a minor amount, say the lightest 2-20 wt.%, of the distillate boiling range oil present in a UMO feed allows water, solvent, gasoline and some distillate to be removed using low grade energy. This increases the effective capacity of the thermal reactors.
  • Such pre-flash stripping if practiced, can occur at vacuum or under a few atmospheres pressure at temperatures from roughly 200°F- 400°F or even higher.
  • the pre-flash vapors are eventually commingled with the vapor phase from the hot separator so that only a single vapor handling means is necessary for the plant.
  • a heat exchange method is used which simultaneously ensures: no water phase forms during condensation of distillates in UMO OH vapor, and no portion of the UMO feed is exposed to unduly high temperatures during preheating.
  • This approach ensures that the UMO feed does not get too hot (which causes coking/deposit formation) and that the UMO vapors from the thermal reactor or UMO vaporizer do not get too cold (which could cause liquid water and an emulsion to form).
  • the "Goldilocks" heat exchange like the porridge of Goldilocks and the three bears, is not too hot and not too cold. Goldilocks heat exchange is just right for our UMO process.
  • a UMO feed is charged via line 301 to optional conventional indirect heat exchange means 305 to heat exchanger 310.
  • the UMO feed is heated to any desired temperature by heat exchange with condensing steam, in this case 150 psig steam.
  • This condensing steam heats the UMO to a temperature approaching, but never exceeding, the temperature of the condensing steam. It is possible to have very high preheat temperatures by using high pressure or superheated steam, but allowing the steam to condense in the heat exchanger to form liquid water sets an upper limit on temperature in the condensing side of the heat exchanger, arbitrarily shown as the shell side in the
  • This tempered preheat step is essential, but only l A of the Goldilocks process.
  • the preheated UMO is then charged via line 315 to thermal reactor 330 wherein the preheated UMO is vaporized by direct injection of steam.
  • the UMO is heated to a temperature sufficient to vaporize the desired amount of distillate boiling range material and surfactants.
  • the UMO overhead vapor is usually above 500°F, hot enough to cause additive decomposition of UMO feed.
  • Such UMO OH vapor is a somewhat dangerous stream to use for preheating the feed as decomposition or fouling may start in one portion of a heat exchanger and eventually foul the exchanger.
  • the UMO overhead (OH) vapor may be quenched or heat exchanged against a non-coking substance, which could be water or some other refinery stream, in optional heat exchange means 340 to produce a quenched UMO OH vapor which is charged via line 341 to heat exchanger means 350.
  • a cooled fraction preferably condensate water from exchanger 310, is heated by indirect heat exchange against hot UMO vapors exiting thermal reactor 330.
  • the temperature of the "cooling" liquid, condensate in line 313, will be, in this example, close to that of the temperature at which 150 psig steam condenses, or 366°F.
  • the condensate will be vaporized and superheated to a temperature approaching that of the UMO vapor, or typically 10-50°F cooler to provide ample delta T to reduce the amount of surface area needed for heat exchange.
  • the UMO OH vapor is cooled by the heat exchange, but not below the temperature of the incoming condensate water, which will have a temperature near that of condensing 150 psig steam.
  • thermal reactor 330 operates at near atmospheric pressure, no water phase can form in the cooled UMO OH vapor.
  • the cooled UMO OH vapor then passes through optional heat exchange means 355 into receiver 360 via line 356.
  • a condensed distillate product which is essentially free of liquid water is withdrawn via line 361.
  • a vapor phase stream, essentially steam, perhaps with a minor amount of vaporized, normally gasoline boiling range components or solvent, if present, is cooled in either conventional heat exchanger 370 or fin-fan cooler 380 to produce condensate which is discharged via line 381 into condensate receiver 390.
  • An oily water stream is withdrawn via line 391 and will usually be sent to conventional water treatment facilities.
  • the heat input to vessel 330 will usually be supplemented by additional superheated steam which may be added via line 315.
  • additional superheated steam which may be added via line 315.
  • An alternative, or supplement, is to rely entirely on steam added via line 314 and add more heat to this steam, using, e.g., a fired heater or other high grade heat source not shown to superheat the steam in line 314 to any desired temperature.
  • Vessel 330 may be batch or continuous. If a batch process is used, multiple swing reactors or vaporizers should be used to ensure the process operates reasonably continuously overall.
  • heat exchangers may be desirable to limit the number and/or size of heat exchangers. If capital costs are high and energy readily available, as by burning some of the UMO product, the optimum plant design may require only exchangers 310 and 350. If maximum energy savings is desired, then additional heat exchangers, such as 305, 355 and 370, may be used.
  • the process of the present invention does not require any special type of reactor, per se.
  • Conventional techniques can be used to heat/vaporize the UMO, e.g. use of a fired heater to supply some or all of the heat input to the vaporization vessel holding the UMO.
  • a UMO fraction containing a large amount, e.g. 10- 15 wt.%) water can be charged to a fractionator vessel with a fired heater reboiler.
  • the reboiler will coke up quickly and have to be shut down frequently to have deposits removed from inside the heater tubes, but the vapor produced will contain more steam than distillate (on a molar basis) and enough surfactants to form an emulsion.
  • a WFE may be used to heat a water containing UMO feed, or steam may be added to the WFE to aid in removal of distillable distillate from the UMO, and produce a UMO vapor phase with sufficient surfactant and steam to form an emulsion upon cooling.
  • steam may be added to the WFE to aid in removal of distillable distillate from the UMO, and produce a UMO vapor phase with sufficient surfactant and steam to form an emulsion upon cooling.
  • UMO vaporization means may be used, but are not preferred, to form a hot UMO vapor fraction which the process of the present invention can treat to avoid the formation of an emulsion.
  • the process of the present invention is especially beneficial when the preferred, direct steam heating method is used for vaporization of the UMO.
  • a preferred embodiment includes the batch, steam heating method disclosed in Figure 2, which is reviewed next.
  • thermal reactors are preferred for the practice of the present invention.
  • a plurality of thermal reactors, each operating in batch mode, work together so that the feed rate to the plant is constant, the product production rate is constant and the only changes in operation are internal as reactors fill and empty.
  • the essence of a thermal batch reactor is thermal processing of UMO by direct contact heat exchange with a heating vapor.
  • the feed can be preheated or not. Lack of pre-heat means that more heating vapor is required to reach the desired end temperature.
  • the UMO feed can be dry or contain large amounts of water.
  • the heating vapor is preferably steam, but any high heat capacity, condensable or recyclable vapor can be used.
  • UMO is charged to a vessel during a fill cycle until a desired liquid level is obtained, typically half-full.
  • a desired liquid level typically half-full.
  • superheated steam is added continuously during filling to ensure the steam line remains open, but this is not essential from a process point of view.
  • superheated vapor injection preferably steam
  • a stirring means may be present, but usually the energy of the entering hot vapors is sufficient to agitate the UMO liquid.
  • Hot vapor injection continues until the desired degree of lift is achieved.
  • more than 30%) of the lube oil boiling range components will be vaporized.
  • more than 50 wt.% of the lube oil boiling range components will be vaporized, or even more, such as 70-80%> "lift".
  • thermal processing or UMO vaporization is complete and the thermal reactor would go into a drain cycle where no steam or UMO would be added, save for minor amounts of steam to ensure that the steam inlets do not clog.
  • the thermal reactors can operate under vacuum or modest pressure, e.g. from 14 atmosphere to 5 or 10 atmospheres absolute. In practice, atmospheric pressure operation works well with the only additional pressure being that required to move fluids through the system. Typically the product receivers will operate at about atmospheric pressure while the thermal reactor will operate at this pressure plus the pressure drop needed to pass the UMO OH vapor through various heat exchangers, vessels and piping.
  • the process lends itself to operation under a mild vacuum, especially as it can be run to condense in the hot separator 90 + %>, and preferably essentially all, of the gasoline boiling range components with the condensed, dry, distillate fraction. This means that the vapor charge from the hot separator is essentially all steam and may be condensed. If the hot flash separator UMO OH receiver is somewhat elevated, it is possible to use a barometric leg to remove the water phase without a pump and a small steam jet ejector or other vacuum means to remove the small amount of non- condensibles that may be present in the UMO feed or leak into the plant.
  • Thermal reactor vapors are removed and preferably quenched or rapidly cooled by heat exchange with a non-reactive medium such as water. Heat exchange of UMO feed against hot thermal reactor vapor effluent is likely to cause fouling. If a refiner has a lot of spare heat exchanger capacity, or does not mind frequent shutdowns, there is no problem with using UMO reactor feed to quench or cool, by indirect heat exchange, UMO thermal reactor vapors.
  • a refiner has a lot of spare heat exchanger capacity, or does not mind frequent shutdowns, there is no problem with using UMO reactor feed to quench or cool, by indirect heat exchange, UMO thermal reactor vapors.
  • boiler feed water, or other non- coking fluid is used in the quench exchanger.
  • the quenched thermal reactor vapors are preferably further heat exchanged against boiler feed water and/or UMO feed to produce partially condensed vapors that are charged to the hot separator.
  • the partially cooled vapors will typically be at a temperature of 250-350°F, depending on pressure, UMO feed properties and % vaporization.
  • This partially condensed vapor/liquid stream consisting essentially of large amounts of steam and condensed, normally liquid, hydrocarbon product, is charged to a hot separator from which a gas oil product is recovered. Hot separator vapors may then be subjected to further heat exchange or simply cooled in a fin-fan cooler, or by heat exchange against cooling water, to produce an oily wastewater stream which may be sent to a conventional wastewater treatment plant.
  • Any conventional or hereafter developed UMO process can be used ranging from the simple to the complex. Common to any system used will be the following features: • Heating the UMO sufficiently to vaporize essentially all of the water present in the UMO or added in the form of super heated steam.
  • the condensation step will condense most, and preferably at least 90 + %, and most preferably, essentially all of the lubricating oil boiling range fractions, but without condensing any water.
  • the overhead (OH) vapor from the UMO reactor is cooled sufficiently to condense most, or all, of the lube boiling range hydrocarbons but never cooled sufficiently to form liquid water. Some water may be dissolved in the liquid hydrocarbon, but no liquid water condenses.
  • the vapor from partial condensation is then further cooled to condense most, or
  • the UMO process preferably operates at a pressure ranging from 14 to 10 atmospheres, absolute, more preferably 1 to 3 atmospheres, absolute.
  • the UMO process operates at essentially atmospheric pressure or slightly above to permit venting of vapor streams to the atmosphere, or to a flare, if either venting or flaring is desired.
  • the UMO recovery process preferably operates with the addition of steam, preferably more steam than UMO is present, on a molar basis. Preferably there is more steam than UMO on a weight basis.
  • the examples that follow are based upon computer simulations, using computer programs that have proven reliable for predicting the performance of various refinery units in the past.
  • the computer simulations are consistent with, but not directly comparable to, a limited amount of laboratory test work done with steam.
  • the computer simulation predicts an end of run thermal reactor temperature a few degrees different than an actual test result. The difference is not believed significant and probably is due to the difficulty of maintaining relatively small pilot plant size equipment at a high temperature in a cold room.
  • This computer simulation is reliable and is used to design refinery fractionation towers, etc. and a commercial scale UMO plant.
  • the computer simulations that follow are side-by-side comparisons of different working fluids and different approaches (recycling a vapor by compressing it versus once through operation or pumped recycle vapor).
  • Fin-fan coolers then cooled and condensed the lubricating oil boiling range components in the UMO vaporizer overhead vapors, leaving most, and preferably essentially all, of the injected vapor in the vapor phase.
  • Condensed hydrocarbon liquid was recovered in a hot separator operating at a temperature of 300°F for this exercise. Hot separator liquid was then heat exchanged against incoming, ambient temperature UMO feed to provide a measure of preheat of the UMO feed prior to heat exchange of UMO feed with hot UMO vaporizer vapors.
  • ULO (or UMO) Cold Feed is the filtered, raw used motor oil feed to the plant.
  • Pre-flash Drum Vapor refers to the overhead vapors from the pre-flash.
  • the pre- flash preferably removes at least 80% of the water, chlorinated solvents, and gasoline boiling range components from the UMO feed.
  • Hot ULO Charge to Reactors refers to the pre-heated feed to each vaporizing vessel.
  • Thermal Reactor Vapor refers to the overhead vapors from each vaporizing reactor. The numbers reported are averaged over the entire heat cycle.
  • Residue Product refers to the bottoms fraction remaining in each vaporization reactor after completion of a heat cycle.
  • Gas Oil Rec.Napor refers to the overhead vapor fraction from the hot separator
  • Gas Oil Product refers to the liquid fraction removed from the hot separator. It contains essentially all of the lubricating oil boiling range components and is similar to, and may be substituted for or blended with, gas oil charge to an FCC unit. Oily Wastewater Product is the liquid water phase resulting when pre-flash overhead vapors and injected steam in the gas oil rec. vapor are cooled and condensed.
  • S.H. Steam-to-Reactors refers to the amount of SuperHeated steam (or other working fluid as the case may be) charged to each vaporization reactor during a heat cycle.

Landscapes

  • 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)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne de retraitement par vaporisation et condensation partielle d'huile à moteur usagée. La fraction vapeur de l'huile à moteur usagée provenant du réacteur (10) thermique peut contenir de l'essence et des solvants chlorés. et contiendra des composants volatils présentant le même intervalle d'ébullition que l'huile lubrifiante et des tensioactifs ou d'autres additifs, en quantité suffisante pour produire une émulsion si la vapeur d'huile usagée est condensée à une température suffisante pour produire une phase aqueuse liquide. Un refroidissement partiel de la vapeur dans des moyens (20) échangeurs de chaleur, à une température située en dessus du point d'ébullition de l'eau, permet d'assurer l'obtention d'un produit hydrocarbure liquide déshydraté, non émulsionné. La phase vapeur qui subsiste après la condensation des hydrocarbures présentant le même intervalle d'ébullition que l'huile lubrifiante, dans le séparateur (30) à chaud, est ensuite condensée pour être transformée en une phase liquide qui peut être traitée dans des installations de traitement d'eaux usées conventionnelles. Ce procédé permet une régénération des huiles à moteur usagées par vaporisation, sans dégazage ou brûlage des vapeurs directement dérivées du traitement des huiles à moteur usagées.
PCT/US2000/013990 2000-05-22 2000-05-22 Rupture d'emulsion par condensation Ceased WO2001090283A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
AU2000252800A AU2000252800A1 (en) 2000-05-22 2000-05-22 Emulsion breaking by condensation
PCT/US2000/013990 WO2001090283A1 (fr) 2000-05-22 2000-05-22 Rupture d'emulsion par condensation
CA002406985A CA2406985C (fr) 2000-05-22 2000-05-22 Rupture d'emulsion par condensation
MXPA02011615A MXPA02011615A (es) 2000-05-22 2000-05-22 Ruptura de emulsion por medio de condensacion.
EP00937657A EP1309668A4 (fr) 2000-05-22 2000-05-22 Rupture d'emulsion par condensation

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/US2000/013990 WO2001090283A1 (fr) 2000-05-22 2000-05-22 Rupture d'emulsion par condensation

Publications (1)

Publication Number Publication Date
WO2001090283A1 true WO2001090283A1 (fr) 2001-11-29

Family

ID=21741404

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2000/013990 Ceased WO2001090283A1 (fr) 2000-05-22 2000-05-22 Rupture d'emulsion par condensation

Country Status (5)

Country Link
EP (1) EP1309668A4 (fr)
AU (1) AU2000252800A1 (fr)
CA (1) CA2406985C (fr)
MX (1) MXPA02011615A (fr)
WO (1) WO2001090283A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2017123260A1 (fr) * 2016-01-17 2017-07-20 Stone, Richard Distillation d'huile moteur usagée avec des vapeurs de distillat

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2065619A (en) * 1931-02-14 1936-12-29 Motol Inc Oil purification and fractionation and apparatus for same
US3791965A (en) * 1972-04-07 1974-02-12 Petrocon Corp Process for re-refining used petroleum products

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2065619A (en) * 1931-02-14 1936-12-29 Motol Inc Oil purification and fractionation and apparatus for same
US3791965A (en) * 1972-04-07 1974-02-12 Petrocon Corp Process for re-refining used petroleum products

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP1309668A4 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2017123260A1 (fr) * 2016-01-17 2017-07-20 Stone, Richard Distillation d'huile moteur usagée avec des vapeurs de distillat

Also Published As

Publication number Publication date
CA2406985A1 (fr) 2001-11-29
MXPA02011615A (es) 2004-05-17
EP1309668A4 (fr) 2004-09-08
EP1309668A1 (fr) 2003-05-14
AU2000252800A1 (en) 2001-12-03
CA2406985C (fr) 2007-12-04

Similar Documents

Publication Publication Date Title
US5976361A (en) Method of and means for upgrading hydrocarbons containing metals and asphaltenes
CN104685033B (zh) 用来将受污或非受污碳氢化合物材料分离和转化成有用产品的混合热处理工艺、工艺的使用、相应系统和设备的制造
US4874505A (en) Recycle of oily refinery wastes
KR0171501B1 (ko) 폐유 재생 장치 및 방법
US10280371B2 (en) Distillation of used motor oil with distillate vapors
WO1991004307A1 (fr) Recyclage de dechets de raffinage du type huileux
CA2242742C (fr) Procede et dispositif pour le traitement des huiles usees
RU2100403C1 (ru) Способ фракционирования нефти и установка для его осуществления
US9243191B1 (en) Re-refining used motor oil
NO314042B1 (no) Fremgangsmåte og anlegg for reraffinering av brukt olje, og syklonvakuumfordamper for behandling av oljen
CN101198674B (zh) 部分脱盐的烃原料的蒸汽裂化
EP2174697A1 (fr) Procédé et unité de recyclage des résidus du pétrole
US6132596A (en) Process and apparatus for the treatment of waste oils
US6402937B1 (en) “Pumped” recycle vapor
US6402938B1 (en) Vaporization of used motor oil with non-hydrogenating recycle vapor
US20040173504A1 (en) Coker operation without recycle
CA2406985C (fr) Rupture d'emulsion par condensation
US5223152A (en) Recovered oil dewatering process and apparatus with water vaporizing in blowdown drum
US9150470B2 (en) Process for contacting one or more contaminated hydrocarbons
EP0348707A1 (fr) Procédé de traitement des boues d'huiles
Hsu et al. Petroleum Distillation
RU2581584C1 (ru) Способ обезвоживания высокоустойчивых водо-углеводородных эмульсий природного и техногенного происхождения и устройство для его реализации
WO2017123260A1 (fr) Distillation d'huile moteur usagée avec des vapeurs de distillat
AU2000250210A1 (en) Vapor phase neutralization in integrated solvent deasphalting and gasification
CN120457186A (zh) 经由具有集成气-液分离器的脱盐器和裂化炉共处理热解油以产生循环产物

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BY CA CH CN CR CU CZ DE DK DM DZ EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT TZ UA UG US UZ VN YU ZA ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE BF BJ CF CG CI CM GA GN GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
WWE Wipo information: entry into national phase

Ref document number: 2406985

Country of ref document: CA

REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

WWE Wipo information: entry into national phase

Ref document number: PA/a/2002/011615

Country of ref document: MX

WWE Wipo information: entry into national phase

Ref document number: 2000937657

Country of ref document: EP

DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
WWP Wipo information: published in national office

Ref document number: 2000937657

Country of ref document: EP

NENP Non-entry into the national phase

Ref country code: JP