EP0053535B1 - Verfahren zur Lösungsmitteldesasfaltierung von Rückstands-Kohlenwasserstoffölen - Google Patents

Verfahren zur Lösungsmitteldesasfaltierung von Rückstands-Kohlenwasserstoffölen Download PDF

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Publication number
EP0053535B1
EP0053535B1 EP81401814A EP81401814A EP0053535B1 EP 0053535 B1 EP0053535 B1 EP 0053535B1 EP 81401814 A EP81401814 A EP 81401814A EP 81401814 A EP81401814 A EP 81401814A EP 0053535 B1 EP0053535 B1 EP 0053535B1
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EP
European Patent Office
Prior art keywords
solvent
deasphalted oil
oil
process according
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.)
Expired
Application number
EP81401814A
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English (en)
French (fr)
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EP0053535A1 (de
Inventor
Pierre Auboir
Pierre Bonnefond
Larry Mank
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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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
    • C10G21/003—Solvent de-asphalting

Definitions

  • the present invention relates to the deasphalting of residual hydrocarbon oils, such as petroleum distillation residues, residues derived from shale oil or oil sands or heavy products from destructive distillation or from hydrogenation of coal.
  • residual hydrocarbon oils such as petroleum distillation residues, residues derived from shale oil or oil sands or heavy products from destructive distillation or from hydrogenation of coal.
  • Residual hydrocarbon oils which contain asphaltic materials, cannot be directly subjected to treatments such as hydrodesulfurization, hydrocracking or catalytic cracking because of their excessive content of asphalt and metals.
  • a difficulty to be overcome is that of the treatment of the asphaltic phase rejected during the deasphalting.
  • This phase contains a significant proportion of extraction solvent, but must be separated from it. This is commonly carried out by vaporization of the solvent and / or entrainment by an inert gas such as nitrogen or water vapor; the vaporization of the solvent makes it necessary to supply a significant amount of heat to the asphalt phase.
  • the asphalt phase is passed through an oven heated by a flame (US 2943050, 3423308 and 4017383) although steam can be used for propane and certain light mixtures of propane and butane (US 3627675).
  • the temperature of the oven must be higher the heavier the solvent, but the temperature is limited by the tendency of the asphalt to decompose on contact with the walls of the oven. It is assumed that a decomposition of the asphalt occurs from 310 to 330 ° C. However, it is difficult to control the temperature of the walls of an oven. Not only is it not the same at all points in the oven, but also the optimum temperature varies over time depending on the variable nature of the load to be heated.
  • the object of the present invention is to describe a process for deasphalting (demetallization) which overcomes the aforementioned drawbacks and makes it possible to treat, without difficulty of fouling and for long periods, residual oils of hydrocarbons by means of hydrocarbons having 4 to 7 carbon atoms, for example isobutane, n-butane, neo-pentane, n-pentane, iso-hexane or C 4 , C s or C 6 cuts.
  • the process comprises bringing the charge of hydrocarbons to be deasphalted into contact with a light hydrocarbon solvent in an extraction (or simple mixing) zone, the quantity of solvent, the temperature and the pressure being chosen so as to allow the formation of 2 distinct phases: a liquid solvent-deasphalted oil mixture and a solvent-asphaltic oil mixture; the phases thus formed are separated from each other, for example by decantation, and the solvent is then separated from each phase by vaporization in order to be able to be recycled.
  • the method is characterized in that a part of the deasphalted oil, substantially separated from the solvent, is passed through a zone of indirect flame heating, so as to raise its temperature, so that it is then brought into contact heat exchange with the solvent-asphalt oil mixture, so as to provide the latter with at least part of the heat necessary for the vaporization of the solvent which it contains, and in that it is finally mixed with the mixture solvent-deasphalted oil discharged from the extraction zone, to which it provides additional heat which facilitates the vaporization of the solvent.
  • the solvent vapor separated by vaporization of the deasphalted oil is brought into heat exchange contact with the solvent-deasphalted oil mixture before the latter receives the deasphalted oil which provides it with the abovementioned supplement. heat.
  • the volume ratio of light hydrocarbon / oil to be deasphalted is usually from 2 to 12, preferably 3 to 5.
  • the temperature depends on the hydrocarbon light used and is usually between 70 and 220 ° C. For example, with pentane, the temperature is usually chosen between 170 and 210 ° C, for example 205 ° C at the top and 195 ° C at the bottom.
  • the temperature to which the deasphalted oil can be brought, in the indirect heating zone by flame, can be relatively high, for example 250 to 420 ° C, preferably 350 to 400 ° C, without serious risk of fouling of said area, due to the reduced content of asphaltenes in this oil.
  • part of the deasphalted oil, heated by flame, can be used to heat the asphalt as it leaves the vaporizer (s).
  • the invention is illustrated by the attached figure.
  • the hydrocarbon charge containing asphaltenes (line 1) is received in intermediate storage 2, then is sent via line 3 in column 4, after having received light hydrocarbon coming from line 5. If desired , another portion of light hydrocarbon is introduced at the bottom of column 4 via line 6.
  • This supply system is of conventional type, just like the reheating at the top of the column by exchanger 7; an interface is established in the column.
  • a mixture of light hydrocarbon and deasphalted oil is drawn off via line 8 and it is passed through exchanger 9 and line 10 to feed the vaporization column 11.
  • the light hydrocarbon vapor is recycled to the pipes 5 and 6 via line 12, exchanger 9, condenser 13 and line 14.
  • the deasphalted oil is withdrawn from column 11 through line 15.
  • a light hydrocarbon vapor phase is obtained which joins line 14 after passing through line 26 and the condenser 27. It can however be sent, if desired, in whole or in part, to line 12 through line 28, so as to recover its heat in the exchanger 9.
  • the asphalt is withdrawn from column 21 through line 29 and is sent to the drive column 30 to be rid of the last traces of 'light hydrocarbon by means of a stream of water vapor admitted by line 31.
  • the asphalt is discharged by line 32; it can be reheated to make it fluid by passing through the exchanger 33 supplied with part of the deasphalted oil having passed through the furnace 16: this oil passes through line 34, exchanger 33 and line 35.
  • vaporized mixtures of water and light hydrocarbon are obtained. These mixtures can be treated together or separately; in the first case, taken as an example, the mixture of line 36 is combined with the mixture of line 37 to pass through the condenser 38 then into the decanter 39. The water is discharged through line 40 and the light hydrocarbon by line 41. The latter can be recycled into the installation by a pipe not shown.
  • the removal of light hydrocarbon from either deasphalted oil or asphalt can be done in a single column, for example column 11 for deasphalted oil and column 21 for asphalt. In this case columns 23 and / or 30 are not used. It is also possible, in this case, to provide a drive by steam or inert gas in the single column, that is to say in columns 11 and 21.
  • a hydrocarbon feedstock consisting of a vacuum residue whose properties are given in the attached table is treated.
  • the hydrocarbon feedstock is treated with n-pentane in a pentane / hydrocarbon volume ratio of 4, at a temperature of approximately 175 ° C. at the bottom and 195 ° C. at the head.
  • the overhead effluent (deasphalted oil + solvent) is subjected to a pressure relief and then passes through the exchanger 9 where it undergoes heating.
  • the vaporized solvent leaves at the head and passes into the exchanger 9.
  • the liquid phase of deasphalted oil leaves at 250 ° C.
  • a part is evacuated from the installation after treatment with water vapor (23).
  • Another part passes into the furnace 16, heated with fuel oil, where it is brought to 330-380 ° C., then into the exchanger 18 where it serves to bring the temperature of the asphaltic phase from approximately 150 to 300 ° C.
  • the latter is subjected to vaporization, after pressure relief, so as to recover the solvent.
  • the asphalt is entrained by water vapor, intended to remove traces of solvent, then it is removed at a temperature of approximately 300 ° C. after reheating with part of the deasphalted oil leaving the oven 16.

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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)

Claims (8)

1. Verfahren zur Entfernung von Asphalt aus einem Asphaltene enthaltenden Kohlenwasserstoffölrückstand durch Lösungsmittel, bei dem der Ölrückstand in einer Extraktionszone mit einem aus einem leichten Kohlenwasserstoff bestehenden Lösungsmittel in Kontakt gebracht wird, Entasphaltierungsbedingungen aufrecht erhalten werden, welche die Bildung einer flüssigen Phase Lösungsmittel-entasphaltiertes Öl und einer fluiden Phase Lösungsmittel-Asphalt ermöglichen, die beiden gebildeten Phasen getrennt und separat das Lösungsmittel aus jeder dieser beiden Phasen verdampft und dadurch getrennt voneinander ein entasphaltiertes Öl und ein Asphaltrückstand gewonnen werden, dadurch gekennzeichnet, daß man
a) einen Teil des entasphaltinen Öls. das praktisch frei von Lösungsmittel ist. in eine indirekte Flammheizzone leitet zur Erhöhung von dessen Temperatur,
b) das in Verfahrensstufe (a) erhaltene aufgeheizte entasphaltierte Öl in indirekten Wärmeaustauschkontakt mit der fluiden Phase Lösungsmittel-Asphalt bringt zur Zuführung mindestens eines Teils der zur Verdampfung des Lösungsmittels benötigten Wärme in diese Phase, und
c) das entasphaltierte Öl nach durchgeführten Wärmeaustausch in Verfahrensstufe (b) mit der aus der Extraktionszone stammenden flüssigen Phase Lösungsmittel-entasphaltiertes Öl mischt.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß man einen Teil des aus Verfahrensstufe (a) stammenden, aufgeheizten, entasphaltierten Öls in indirekten Wärmeaustauschkontakt mit dem Asphaltrückstand bringt zur Aufheizung und Fluidisierung desselben.
3. Verfahren nach Ansprüchen 1 oder 2, dadurch gekennzeichnet, daß man in Verfahrensstufe (a) die Temperatur des entasphaltierten Öls auf 250-420 °C bringt.
4. Verfahren nach Ansprüchen 1 oder 2, dadurch gekennzeichnet, daß man in Verfahrensstufe (a) die Temperatur des entasphaltierten Öls auf 350-400 °C bringt.
5. Verfahren nach einem der Ansprüche 1-4, dadurch gekennzeichnet, daß man den aus dem entasphaltierten Öl abgeschiedenen Lösungsmitteldampf in Wärmeaustauschkontakt mit der flüssigen Phase Lösungsmittel-entasphaltiertes Öl bringt vor deren Vermischen in Verfahrensstufe (c).
6. Verfahren nach einem der Ansprüche 1-5, dadurch gekennzeichnet, daß man als Lösungsmittel aliphatische Kohlenwasserstoffe mit 4 bis 7 Kohlenstoffatomen einsetzt.
7. Verfahren nach einem der Ansprüche 1-5, dadurch gekennzeichnet, daß man als Lösungsmittel aliphatische Kohlenwasserstoffe mit 5 bis 7 Kohlenstoffatomen einsetzt.
8. Verfahren nach einem der Ansprüche 1-7, dadurch gekennzeichnet, daß man die Menge des in Verfahrensstufe (a) eingespeisten entasphaltierten Öls in Abhängigkeit von der Wärmemenge steuert, die der fluiden Phase Lösungsmittel-Asphaltöl zuzuführen ist.
EP81401814A 1980-11-28 1981-11-18 Verfahren zur Lösungsmitteldesasfaltierung von Rückstands-Kohlenwasserstoffölen Expired EP0053535B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8025405 1980-11-28
FR8025405A FR2495177B1 (fr) 1980-11-28 1980-11-28 Procede de desasphaltage au solvant d'huiles residuelles d'hydrocarbures

Publications (2)

Publication Number Publication Date
EP0053535A1 EP0053535A1 (de) 1982-06-09
EP0053535B1 true EP0053535B1 (de) 1985-01-30

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EP81401814A Expired EP0053535B1 (de) 1980-11-28 1981-11-18 Verfahren zur Lösungsmitteldesasfaltierung von Rückstands-Kohlenwasserstoffölen

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US (1) US4395330A (de)
EP (1) EP0053535B1 (de)
DE (1) DE3168699D1 (de)
FR (1) FR2495177B1 (de)

Families Citing this family (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4548711A (en) * 1982-09-02 1985-10-22 Phillips Petroleum Company Solvent extraction
GB2134537A (en) * 1983-02-03 1984-08-15 Dravo Corp For solvent deasphalting of petroleum
US4666587A (en) * 1983-09-29 1987-05-19 Aaron Seligson Waste oil purifying process
US4572781A (en) * 1984-02-29 1986-02-25 Intevep S.A. Solvent deasphalting in solid phase
US4673485A (en) * 1984-04-06 1987-06-16 Exxon Research And Engineering Company Process for increasing deasphalted oil production from upgraded residua
US4601816A (en) * 1984-08-09 1986-07-22 Mobil Oil Corporation Upgrading heavy hydrocarbon oils using sodium hypochlorite
US4795551A (en) * 1985-07-15 1989-01-03 Lummus Crest, Inc. Solvent refining of residues
FR2588877B1 (fr) * 1985-10-17 1988-01-15 Inst Francais Du Petrole Procede de desasphaltage comportant une recuperation d'energie lors de la separation huile desasphaltee-solvant de desasphaltage
DE3609988C2 (de) * 1986-03-25 1994-08-04 Metallgesellschaft Ag Kombiniertes Verfahren zum Abtrennen und Behandeln von Asphaltenen mit hoher Erweichungstemperatur
US5914010A (en) * 1996-09-19 1999-06-22 Ormat Industries Ltd. Apparatus for solvent-deasphalting residual oil containing asphaltenes
DE19644600A1 (de) * 1996-10-26 1998-05-07 Inst Erdoel Und Erdgasforschun Halbkontinuierlich arbeitende Laborapparatur zur Entasphaltierung von Rohölen
US6043299A (en) * 1996-10-31 2000-03-28 Shell Oil Company Process for the extraction of material from multi-phase systems
RU2217475C2 (ru) * 2002-01-10 2003-11-27 Открытое акционерное общество "Славнефть-Ярославнефтеоргсинтез" Способ регенерации растворителя
US7749378B2 (en) * 2005-06-21 2010-07-06 Kellogg Brown & Root Llc Bitumen production-upgrade with common or different solvents
CA2729457C (en) 2011-01-27 2013-08-06 Fort Hills Energy L.P. Process for integration of paraffinic froth treatment hub and a bitumen ore mining and extraction facility
CA2853070C (en) 2011-02-25 2015-12-15 Fort Hills Energy L.P. Process for treating high paraffin diluted bitumen
CA2931815C (en) 2011-03-01 2020-10-27 Fort Hills Energy L.P. Process and unit for solvent recovery from solvent diluted tailings derived from bitumen froth treatment
CA2865139C (en) 2011-03-04 2015-11-17 Fort Hills Energy L.P. Process for co-directional solvent addition to bitumen froth
CA2735311C (en) 2011-03-22 2013-09-24 Fort Hills Energy L.P. Process for direct steam injection heating of oil sands bitumen froth
CA2737410C (en) 2011-04-15 2013-10-15 Fort Hills Energy L.P. Heat recovery for bitumen froth treatment plant integration with sealed closed-loop cooling circuit
CA2848254C (en) 2011-04-28 2020-08-25 Fort Hills Energy L.P. Recovery of solvent from diluted tailings by feeding a desegregated flow to nozzles
CA2857702C (en) 2011-05-04 2015-07-07 Fort Hills Energy L.P. Process for operating a bitumen froth treatment operation in turndown mode
CA2740935C (en) 2011-05-18 2013-12-31 Fort Hills Energy L.P. Enhanced temperature control of bitumen froth treatment process
US10808183B2 (en) 2012-09-12 2020-10-20 The University Of Wyoming Research Corporation Continuous destabilization of emulsions

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CA512043A (en) * 1955-04-19 G. Ditman John Propane deasphalting of crude residua of hydrocarbon oil
US2240008A (en) * 1938-12-29 1941-04-29 Process Management Co Inc Treating hydrocarbon fluids
US2611737A (en) * 1949-02-09 1952-09-23 Sinclair Refining Co Process for the preparation of hydrocarbon cracking stock for catalytic cracking
FR1111876A (fr) * 1953-11-07 1956-03-06 Edeleanu Gmbh Procédé pour la récupération de solvants à partir de mélanges en contenant
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US2847353A (en) * 1955-12-30 1958-08-12 Texas Co Treatment of residual asphaltic oils with light hydrocarbons
US2943050A (en) * 1957-12-03 1960-06-28 Texaco Inc Solvent deasphalting
FR1408708A (fr) * 1962-09-27 1965-08-20 Exxon Research Engineering Co Procédé de raffinage d'huiles lubrifiantes
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Also Published As

Publication number Publication date
DE3168699D1 (en) 1985-03-21
FR2495177A1 (fr) 1982-06-04
FR2495177B1 (fr) 1985-06-07
EP0053535A1 (de) 1982-06-09
US4395330A (en) 1983-07-26

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