EP0940466A2 - Procédé de raffinage d'huile usée - Google Patents

Procédé de raffinage d'huile usée Download PDF

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Publication number
EP0940466A2
EP0940466A2 EP99104198A EP99104198A EP0940466A2 EP 0940466 A2 EP0940466 A2 EP 0940466A2 EP 99104198 A EP99104198 A EP 99104198A EP 99104198 A EP99104198 A EP 99104198A EP 0940466 A2 EP0940466 A2 EP 0940466A2
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EP
European Patent Office
Prior art keywords
oil
aliphatic solvent
treatment vessel
waste oil
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.)
Withdrawn
Application number
EP99104198A
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German (de)
English (en)
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EP0940466A3 (fr
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.)
OLIM TECHNOLOGIES SA
Original Assignee
OLIM TECHNOLOGIES SA
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.)
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Publication date
Application filed by OLIM TECHNOLOGIES SA filed Critical OLIM TECHNOLOGIES SA
Publication of EP0940466A2 publication Critical patent/EP0940466A2/fr
Publication of EP0940466A3 publication Critical patent/EP0940466A3/fr
Withdrawn legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/28—Recovery of used solvent
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/006—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents of waste oils, e.g. PCB's containing oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/12—Organic compounds only
    • C10G21/14—Hydrocarbons

Definitions

  • Waste oil may contain many unwanted substances such as water, contaminants and additives which need to be removed before the oil can be re-used.
  • Waste or used oil however contains other unwanted substances particularly water.
  • the method described in US 2196989 cannot readily be adapted for the treatment of waste oil containing water.
  • a solvent i.e. propane is used to dissolve the oil in a static mixer.
  • the waste oil contains too much water, this has to be removed before the waste oil is refined. Also, the water is removed from the static treatment vessel with residuum and then has to be separated therefrom.
  • a method of refining waste oil containing contaminants and water comprising the steps of contacting the waste oil with an aliphatic solvent to form a waste oil/aliphatic solvent mixture, and in a treatment vessel separating the mixture into three phases, namely a bottom phase comprising predominantly water, an intermediate phase comprising predominantly residuum containing contaminants and a top phase comprising predominantly an oil/aliphatic solvent solution, and removing the three phases individually from the treatment vessel.
  • waste oil and aliphatic solvent are mixed in the treatment vessel although they may be pre-mixed if desired and fed to the treatment vessel.
  • a precipitant gas such as nitrogen, carbon dioxide, or a C 1 to C 4 alkane may be introduced into the treatment vessel to cause refluxing of the waste oil/aliphatic solvent mixture in a similar manner to that described in US 2196989.
  • the treatment vessel has a larger cross section in a lower region thereof than in an intermediate region above the lower region, refluxing occurring above the lower region and the bottom and intermediate phases collecting in the lower region of the treatment vessel.
  • the precipitant gas or other refluxing agent conveniently is introduced into an upper part of the intermediate region of the vessel and the waste oil is introduced below into the treatment vessel for mixing with the aliphatic solvent.
  • the aliphatic solvent is preferably introduced into the treatment vessel in a lower part of the intermediate region thereof, preferably below the waste oil.
  • each of the three phases may contain some entrained aliphatic solvent and so desirably each of the three phases is treated to remove aliphatic solvent therefrom.
  • the recovered aliphatic solvent is preferably recycled by mixing with further waste oil in the treatment vessel.
  • the oil from the top phase is subjected to a fractional distillation e.g. vacuum distillation to separate the oil into different fractions.
  • an apparatus for performing the method of the first aspect of the invention comprising a treatment vessel in which a waste oil/aliphatic solvent mixture is separated into three phases, namely a bottom phase comprising predominantly water, an intermediate phase comprising contaminant residuum and a top phase comprising and oil/aliphatic solvent solution, the treatment vessel having means to enable each of the three phases to be removed individually from the treatment vessel.
  • the treatment vessel may comprise a lower region having a greater cross section that an intermediate region above the lower region to enable refluxing of the waste oil/aliphatic solvent mixture in the treatment vessel above the lower region and to aid separation of the three phases.
  • the apparatus may comprise an evaporator means for evaporating from the bottom phase and/or top phase and/or intermediate phase, aliphatic solvent and may include a fractional distillation means for separating the oil from the top phase into different fractions.
  • the oil may be vaporised prior to distillation in an evaporator means comprising a vessel having passage means along which oil to be evaporated, passes as the oil is heated, the passage means being lined with a flowing film of heavy fraction obtained from the fractional distillation means.
  • an evaporating means for vaporising oil comprising passage means along which the oil passes as the oil is heated, the passage means being lined with a flowing film of heavy fraction oil.
  • an apparatus 10 for refining waste oil containing contaminants including water comprises a treatment vessel 11 parts of which are heated to a temperature of between 15° and 45°C, and into which the waste oil is introduced at point 12 from a storage vessel or the like along a disperser D1, preferably at a temperature in the range 15°C and 45°C.
  • the treatment vessel 11 comprises a tower having a lower region 14 the cross section of which is generally larger than an intermediate region 15 immediately above. At the very bottom of the lower region 14 there is a sump 16 for a purpose hereinafter explained. Point 12 is preferably in the intermediate region 15.
  • the waste oil is contacted in the treatment vessel 11 with an aliphatic solvent being propane liquid, although in another example, the waste oil and propane or other aliphatic solvent may be contacted in a separate mixing vessel before being introduced into the treatment vessel 11.
  • an aliphatic solvent being propane liquid
  • propane or other aliphatic solvent may be contacted in a separate mixing vessel before being introduced into the treatment vessel 11.
  • the propane is introduced into the treatment vessel 11 at point 18 at a lower part of the intermediate region 15, via a disperser D2 from a line 36 from a propane store (not shown).
  • the propane is heated or cooled before being introduced into the treatment vessel 11 to be at a temperature of between -5°C and 45°C.
  • propane and waste oil will form a mixture with a large proportion of the waste oil dissolved in the propane and water will tend to sink in the vessel 11 by virtue of its higher specific gravity.
  • the ratio of propane to waste oil in the mixture in the vessel 11 is preferably in the range 3:1 to 10:1.
  • a precipitant gas such as nitrogen is injected into the treatment vessel 11 preferably at a temperature of between 15°C and 45°C at point 20 being an upper part of the intermediate region 15, via a disperser D3.
  • the waste oil/propane mixture separates into three phases, namely a bottom phase I which is predominantly water with some entrained propane and other contaminants, an intermediate phase II which is predominantly waste residuum with some entrained propane and water, and a top phase III which is an oil/propane solution which collects in an upper region 39 of the treatment vessel 11.
  • the upper region 39 has a cross section greater than that of the immediately adjacent part of the intermediate region 15, but less than that of the lower region 14.
  • the bottom phase I tends to collect in the very bottom of the lower region 14 of the treatment vessel 11, in sump 16 from where the bottom phase may be removed and fed to a heating vessel 22 and hence to an evaporating means 24 which comprises in this example a flash evaporator.
  • an evaporating means 24 which comprises in this example a flash evaporator.
  • propane is removed and delivered via a line 29 to a collection line 25 from where the propane may be removed, cleaned and recycled to the treatment vessel 11.
  • the water is removed from the flash evaporator 24 via a line 26 for disposal.
  • the intermediate phase II tends to collect in the lower region 14 of the treatment vessel 11 too, and is removed via a poll 27, fed to a heating vessel 28 and hence to an atmospheric pressure propane stripper 30 where the intermediate phase is further heated to remove propane which is fed to collection line 25 via a line 32 via another heater and a flash condensate receiver so that any waste water entrained in the propane is removed.
  • the remaining residuum is removed from the stripper 30 via a port 31 and may be used for example only, when mixed with oil, as a road making material.
  • oil may be any oil having a flash point above 200°C such as for example oil from downstream in the process, from line 74 (see below).
  • the top phase III is removed from the upper region 39 of the treatment vessel 11 and fed along a line 40 to a surge vessel 41 (figure 2), so that any residuum entrained in the oil/propane solution can be removed and returned to the treatment vessel 11 along a return line 43 for further processing.
  • the residuum is preferably at a temperature of between 15°C and 45°C.
  • Any propane removed from the solution in the surge vessel 41 is fed via line 34 to collection line 25 for further treatment and recycling.
  • the remaining cleaned top phase is then fed along a line 45 to a series of heaters 46-48 where the temperature of the solution is steadily raised.
  • the hot solution is then fed along line 50 via a final heater 51, and into solvent flash column 53 where the major portion of the propane in the solution is removed, condensed in condensers 54,55 and recycled to the treatment vessel 11 via a line 36.
  • Remaining propane in the top phase solution is removed in a second (steam) stripper 58, and passes from the stripper 58 to a heater 60 and condenser 61 so that any light hydrocarbon fractions removed from the oil in the second stripper 58 can be recovered and fed to a store along line 62 for use.
  • Any water in the propane arising from steam introduced into the second stripper 58 at 59 is also condensed in condenser 61 and may be collected in a sump 65 thereof for disposal.
  • the oil separated from the propane in the second stripper 58 is then treated by fractional distillation in a vacuum distillation column 70 from where the various fractions in the oil e.g. (VGO) gas oil 66, (light) neutral oil 67 and (heavy) neutral fuel oil 68 can be separated as is well known in the art.
  • VGO vacuum distillation column 70
  • the oil Prior to introduction of the oil into the distillation column 70, the oil is preheated in a heat exchanger 71. Conventionally immediately prior to introduction into a distillation column, oil is vaporised by reducing the pressure of the oil. The pressure of the oil is however maintained in the heat exchanger 71 by means of the operation of a control valve C so that in the event of any remaining contaminants in the oil, these are not deposited in the heat exchanger 71 if the lighter oil fractions boil to dryness, which could cause a blockage and hence reduction in oil flow.
  • the hot oil from heat exchanger 71 is however vaporised in a falling film evaporator indicated at 72, prior to introduction into the distillation column 70 at line 76.
  • Any light fractions in the hot oil from heat exchanger 71 flash in a vessel 75 and by pass the evaporator 72 via a line 77 from where they are fed into line 76 to enter the distillation column 70.
  • the falling film evaporator 72 comprises a plurality of tubular passages 73 through which the oil passes as it is heated. To avoid the possibility of contaminants being deposited in the passages, the passages are lined with a flowing film of oil.
  • the oil for the film is obtained in this example from the distillation column 70 and comprises the heaviest fraction separated from the oil, known as fuel oil, which is fed to the falling film evaporator 72 via line 74 and the flash vessel 75 to which the hot oil from the heater 71 is also directed.
  • oil for the flowing film may be obtained from another source if desired.
  • At least a proportion of the heat in the fraction oil from line 74 may be introduced into the pressure propane stripper 30 via a line 78, in order to maintain constant the level of distillation bottoms in the system.
  • the line 78 may lead to a store.
  • the volume of oil flowing to provide the falling film is substantially greater, typically ten times greater than the volume of the recovered oil being heated so that an insubstantial amount of the oil of the falling film only, is evaporated, and the flowing film is relatively thin (1 mm or so) compared with the volume of the passages 73 (30-35mm diameter perhaps) lined by the flowing film.
  • the falling film effectively covers the passage walls but fills less than 10% of the passage void, more preferably 6%.
  • the recovered oil can efficiently be heated in the evaporator 72 to evaporate the oil, without risk of any contaminants remaining in the recovered oil, being deposited.
  • the falling film evaporator 72 may be used in other applications to that described herein, for example in any application where it is desired to evaporate oil.
  • a falling film evaporator 72 may be used in the place of any of the evaporating and flash vessels described above in relation to the oil refining process.
  • the treatment vessel 11 shown in the drawings is only an example of a suitable vessel in which a waste oil/propane mixture may be separated into three distinct phases. Although it is preferred that propane or other aliphatic solvent removed from the three phases is collected, treated and recycled, virgin propane or any other suitable aliphatic solvent may be used.
  • the number of and positions of heaters used in the apparatus 10 may be varied depending on the refinery layout and the positioning of each of the various vessels may be arranged to suit a particular site.
  • the treatment vessel 11 is heated to a temperature of between 15°C and 45°C by virtue of the flows into the vessel, at 12, 20 and from line 43, but ancillary heaters/coolers may be provided if desired.
  • nitrogen is introduced into the treatment vessel to facilitate refluxing
  • another precipitating/refluxing agent such as carbon dioxide, or a C1 to C4 alkane gas
  • such gas is introduced into treatment vessel 11 at pressure, typically a pressure of less than one bar above the pressure at which the propane liquid is introduced into the vessel 11.
  • the nitrogen or other gas is removed from the top vessel 11 via line 99 and recovered for re-use or is mixed with combustion air for use in heating in the apparatus.
  • other substances which facilitate precipitation of the oil and contaminants may be introduced into the treatment vessel 11 in addition to or instead of the precipitant gas, such as flocculating reagents.
  • a refluxing agent being distillation feed oil from downstream in the process, may be used.
  • Such refluxing oil may be fed from between the stripper 58 and the heating vessel 71, as indicated in dotted lines in figure 2.
  • the treatment vessel 11 may be at least partially packed as shown at P to facilitate mixing of the waste oil and propane and the effect of the refluxing agent, as well as settling out of the phases.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP99104198A 1998-03-04 1999-03-02 Procédé de raffinage d'huile usée Withdrawn EP0940466A3 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB9804481 1998-03-04
GB9804481A GB2335436B (en) 1998-03-04 1998-03-04 Method of refining waste oil

Publications (2)

Publication Number Publication Date
EP0940466A2 true EP0940466A2 (fr) 1999-09-08
EP0940466A3 EP0940466A3 (fr) 2000-09-06

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ID=10827897

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EP99104198A Withdrawn EP0940466A3 (fr) 1998-03-04 1999-03-02 Procédé de raffinage d'huile usée

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EP (1) EP0940466A3 (fr)
GB (1) GB2335436B (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2947281A1 (fr) * 2009-06-26 2010-12-31 Total Sa Procede de traitement d'hydrocarbures
US7976699B2 (en) 2006-06-16 2011-07-12 Kesler Michael L Distillation apparatus and method of use

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2196989A (en) * 1938-07-11 1940-04-16 Phillips Petroleum Co Process for treating hydrocarbons
DE2153976A1 (de) * 1971-10-29 1973-05-03 Texaco Development Corp Verfahren zum entoelen und entwaessern von raffinerie- und oelschlamm
FR2301592A1 (fr) * 1975-02-20 1976-09-17 Inst Francais Du Petrole Procede de regeneration d'huiles lubrifiantes usagees par extraction au solvant et hydrogenation
US4502944A (en) * 1982-09-27 1985-03-05 Kerr-Mcgee Refining Corporation Fractionation of heavy hydrocarbon process material
FR2550545B1 (fr) * 1983-08-08 1986-04-11 Elf France Procede et appareil pour deshydrater, dessaler et desasphalter simultanement un melange d'hydrocarbures
FR2639649B1 (fr) * 1988-11-25 1991-01-25 Elf Aquitaine Procede d'extraction d'une charge hydrocarbonee par un solvant organique
GB9408609D0 (en) * 1994-02-15 1994-06-22 Petroleum Technology Corp Apparatus and related method for processing drain oil

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7976699B2 (en) 2006-06-16 2011-07-12 Kesler Michael L Distillation apparatus and method of use
FR2947281A1 (fr) * 2009-06-26 2010-12-31 Total Sa Procede de traitement d'hydrocarbures
WO2010150234A3 (fr) * 2009-06-26 2011-03-17 Total S.A. Procede de traitement d'hydrocarbures
GB2483039A (en) * 2009-06-26 2012-02-22 Total Sa Method for treating hydrocarbons
GB2483039B (en) * 2009-06-26 2013-07-10 Total Sa Method for treating hydrocarbons

Also Published As

Publication number Publication date
GB9804481D0 (en) 1998-04-29
GB2335436A (en) 1999-09-22
EP0940466A3 (fr) 2000-09-06
GB2335436B (en) 2002-05-15

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