EP0053535B1 - De-asphalting process with a solvent of residual hydrocarbon oils - Google Patents

De-asphalting process with a solvent of residual hydrocarbon oils 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
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EP81401814A
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German (de)
French (fr)
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EP0053535A1 (en
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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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    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G21/00Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/28Recovery of used solvent
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G21/00Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/003Solvent 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)

Description

La présente invention concerne le désasphaltage des huiles résiduelles d'hydrocarbures, telles que les résidus de distillation du pétrole, les résidus dérivés des huiles de schiste ou des sables bitumineux ou les produits lourds de la distillation destructrice ou de l'hydrogénation du charbon.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.

Les huiles résiduelles d'hydrocarbures, qui renferment des matières asphaltiques, ne peuvent être directement soumises à des traitements tels que l'hydrodésulfuration, l'hydrocracking ou le cracking catalytique du fait de leur teneur excessive en asphalte et en métaux.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.

Il a donc été proposé de les soumettre à un traitement préalable de désasphaltage au moyen d'un solvant habituellement choisi parmi les hydrocarbures aliphatiques, saturés ou oléfiniques, de bas poids moléculaire.It has therefore been proposed to subject them to a prior deasphalting treatment by means of a solvent usually chosen from aliphatic hydrocarbons, saturated or olefinic, of low molecular weight.

On sait que le rendement en huile désasphaltée est d'autant plus élevé que l'hydrocarbure utilisé comme solvant renferme davantage d'atomes de carbone, avec toutefois deux inconvénients : ce rendement accru est obtenu au détriment de la pureté de l'huile, notamment de sa teneur en métaux ; l'asphalte obtenu est d'autant plus dur et moins fusible que le solvant est plus lourd.It is known that the yield of deasphalted oil is higher the more the hydrocarbon used as solvent contains more carbon atoms, with however two drawbacks: this increased yield is obtained at the expense of the purity of the oil, in particular its metal content; the asphalt obtained is harder and less meltable the heavier the solvent.

Il en résulte que, pour des raisons pratiques et bien que l'on ait proposé d'utiliser des hydrocarbures ayant de 3 à 7 atomes de carbone, la plupart des réalisations connues opèrent avec des hydrocarbures C3, C4, mélanges C3 + C4 et plus rarement C5.As a result, for practical reasons and although it has been proposed to use hydrocarbons having from 3 to 7 carbon atoms, most of the known embodiments operate with C 3 , C 4 hydrocarbons, C 3 + mixtures C 4 and more rarely C 5 .

Une difficulté à surmonter est celle du traitement de la phase asphaltique rejetée au cours du désasphaltage. Cette phase renferme une proportion notable de solvant d'extraction, mais doit être séparée de celui-ci. Ceci est communément réalisé par vaporisation du solvant et/ou entraînement par un gaz inerte tel que l'azote ou la vapeur d'eau ; la vaporisation du solvant oblige à fournir une quantité importante de chaleur à la phase asphaltique.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.

Dans les réalisations connues, on fait passer la phase asphaltique dans un four chauffé par une flamme (US 2943050, 3423308 et 4017383) bien que l'on puisse utiliser la vapeur d'eau pour le propane et certains mélanges légers de propane et de butane (US 3627675).In known embodiments, 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).

Il est clair que la température du four doit être d'autant plus élevée que le solvant est plus lourd, mais on est limité en température par la tendance de l'asphalte à se décomposer au contact des parois du four. On admet qu'une décomposition de l'asphalte se produit dès 310 à 330 °C. Or il est difficile de contrôler la température des parois d'un four. Non seulement celle-ci n'est pas la même en tous les points du four, mais encore la température optimale varie au cours du temps en fonction de la nature elle-même variable de la charge à réchauffer.It is clear that 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.

La décomposition de l'asphalte se traduit par des dépôts qui s'opposent à une bonne transmission de la chaleur et obligent à chauffer davantage, augmentant encore les points chauds. Le rendement du four s'abaisse tellement que l'on doit procéder à un arrêt et à un nettoyage de l'installation ; parfois même c'est le bouchage des canalisations qui commande l'arrêt de l'opération.The breakdown of the asphalt results in deposits which prevent good heat transmission and force more heat, further increasing hot spots. The efficiency of the oven drops so much that the system has to be shut down and cleaned; sometimes even it is the blockage of the pipes that controls the stopping of the operation.

Cet inconvénient se manifeste déjà avec l'emploi de butane, et il est particulièrement accusé quand on emploie un hydrocarbure ayant de 5 à 7 atomes de carbone en raison du caractère de plus en plus visqueux de l'asphalte obtenu.This drawback is already manifested with the use of butane, and it is particularly pronounced when a hydrocarbon having 5 to 7 carbon atoms is used because of the increasingly viscous nature of the asphalt obtained.

L'objet de la présente invention est de décrire un procédé de désasphaltage (démétallisation) qui remédie aux inconvénients précités et permet de traiter, sans difficulté d'encrassement et pendant de longues périodes, des huiles résiduelles d'hydrocarbures au moyen d'hydrocarbures ayant 4 à 7 atomes de carbone, par exemple l'isobutane, le n-butane, le néo-pentane, le n-pentane, l'iso-hexane ou des coupes C4, Cs ou C6.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.

Le procédé comprend la mise en contact de la charge d'hydrocarbures à désasphalter avec un solvant hydrocarbure léger, dans une zone d'extraction (ou de simple mélange), la quantité de solvant, la température et la pression étant choisies de manière à permettre la formation de 2 phases distinctes : un mélange liquide solvant-huile désasphaltée et un mélange fluide solvant-huile asphaltique ; les phases ainsi formées sont séparées l'une de l'autre, par exemple par décantation, et le solvant est ensuite séparé de chaque phase par vaporisation afin de pouvoir être recyclé. Le procédé est caractérisé en ce qu'on fait passer une partie de l'huile désasphaltée, substantiellement séparée du solvant, dans une zone de chauffage indirect par flamme, de manière à élever sa température, en ce qu'on la met ensuite en contact d'échange de chaleur avec le mélange solvant-huile asphaltique, de manière à fournir à ce dernier au moins une partie de la chaleur nécessaire à la vaporisation du solvant qu'il renferme, et en ce qu'on la mélange enfin avec le mélange solvant-huile désasphaltée déchargé de la zone d'extraction, auquel elle apporte un complément de chaleur qui facilite la vaporisation du solvant.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.

Suivant un mode de réalisation préféré, la vapeur de solvant séparée par vaporisation de l'huile désasphaltée est mise en contact d'échange thermique avec le mélange solvant-huile désasphaltée avant que celui-ci reçoive l'huile désasphaltée qui lui fournit le complément précité de chaleur.According to a preferred embodiment, 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.

Les conditions opératoires du désasphaltage sont, en elles-mêmes, connues et ne seront que brièvement rappelées : le rapport en volume hydrocarbure léger/huile à désasphalter est habituellement de 2 à 12, de préférence 3 à 5. La température dépend de l'hydrocarbure léger utilisé et se situe habituellement entre 70 et 220 °C. Par exemple, avec le pentane, la température est habituellement choisie entre 170 et 210 °C, par exemple 205 °C en tête et 195 °C en fond.The operating conditions for deasphalting are in themselves known and will only be briefly recalled: 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.

La température à laquelle peut être portée l'huile désasphaltée, dans la zone de chauffage indirect par flamme, peut être relativement élevée, par exemple 250 à 420 °C, de préférence 350 à 400 °C, sans risque sérieux d'encrassement de la dite zone, en raison de la teneur réduite en asphaltènes de cette huile.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.

Comme cette huile est ensuite renvoyée en aval de la zone de vaporisation du solvant mélangé à l'huile désasphaltée, il est aisé de contrôler la quantité de chaleur fournie à la phase asphaltique, dans la zone d'échange, par simple réglage du débit de cette huile.As this oil is then returned downstream of the vaporization zone of the solvent mixed with the deasphalted oil, it is easy to control the quantity of heat supplied to the asphalt phase, in the exchange zone, by simply adjusting the flow rate of this oil.

Selon une variante du procédé, une partie de l'huile désasphaltée, chauffée par flamme, peut être utilisée pour réchauffer l'asphalte à sa sortie du (ou des) vaporiseur(s).According to a variant of the process, part of the deasphalted oil, heated by flame, can be used to heat the asphalt as it leaves the vaporizer (s).

L'invention est illustrée par la figure jointe.The invention is illustrated by the attached figure.

La charge d'hydrocarbures contenant des asphaltènes (conduite 1) est reçue dans le stockage intermédiaire 2, puis est envoyée par la conduite 3 dans la colonne 4, après avoir reçu de l'hydrocarbure léger provenant de la conduite 5. Si on le désire, une autre portion d'hydrocarbure léger est introduite au bas de la colonne 4 par la ligne 6. Ce système d'alimentation est de type conventionnel, tout comme le réchauffage en haut de colonne par l'échangeur 7 ; un interface s'établit dans la colonne. On soutire un mélange d'hydrocarbure léger et d'huile désasphaltée par la ligne 8 et on le fait passer dans l'échangeur 9 et la ligne 10 pour alimenter la colonne de vaporisation 11. La vapeur d'hydrocarbure léger est recyclée vers les conduites 5 et 6 par la ligne 12, l'échangeur 9, le condenseur 13 et la conduite 14. L'huile désasphaltée est soutirée de la colonne 11 par la conduite 15. Une partie de cette huile passe dans le four 16, la conduite 17, l'échangeur 18 et la ligne 19 pour rejoindre la conduite 10. Dans l'échangeur 18, elle cède de la chaleur au mélange d'asphalte et d'hydrocarbure léger qui quitte la colonne 4 par la conduite 20 pour être envoyé dans la colonne de vaporisation 21. Une autre partie d'huile désasphaltée est envoyée par la conduite 22 dans la colonne d'entraînement 23 où elle est traitée par un courant de vapeur d'eau (conduite 24). L'huile désasphaltée est ainsi débarrassée des dernières traces d'hydrocarbure léger et est évacuée par la ligne 25.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. Part of this oil passes through the oven 16, line 17 , the exchanger 18 and the line 19 to join the line 10. In the exchanger 18, it gives off heat to the mixture of asphalt and light hydrocarbon which leaves the column 4 via the line 20 to be sent to the vaporization column 21. Another part of deasphalted oil is sent through line 22 into the drive column 23 where it is treated by a stream of water vapor (line 24). The deasphalted oil is thus freed from the last traces of light hydrocarbon and is discharged via line 25.

Dans la colonne de vaporisation 21, on obtient une phase vapeur d'hydrocarbure léger qui rejoint la ligne 14 après passage dans la conduite 26 et le condenseur 27. On peut toutefois l'envoyer, si on le désire, en tout ou partie, vers la ligne 12 par la conduite 28, de façon à récupérer sa chaleur dans l'échangeur 9. L'asphalte est soutiré de la colonne 21 par la ligne 29 et est envoyé dans la colonne d'entraînement 30 pour être débarrassé des dernières traces d'hydrocarbure léger au moyen d'un courant de vapeur d'eau admis par la ligne 31. L'asphalte est déchargé par la ligne 32 ; on peut le réchauffer pour le fluidiser par passage dans l'échangeur 33 alimenté par une partie de l'huile désasphaltée ayant traversé le four 16 : cette huile passe dans la ligne 34, l'échangeur 33 et la ligne 35.In the vaporization column 21, 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.

En tête des colonnes 23 et 30 on obtient des mélanges vaporisés d'eau et d'hydrocarbure léger. Ces mélanges peuvent être traités ensemble ou séparément ; dans le premier cas, pris comme exemple, le mélange de la conduite 36 est réuni au mélange de la ligne 37 pour passer dans le condenseur 38 puis dans le décanteur 39. L'eau est déchargée par la ligne 40 et l'hydrocarbure léger par la ligne 41. Ce dernier peut être recyclé dans l'installation par une conduite non représentée.At the head of columns 23 and 30, 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.

De nombreuses modifications peuvent être apportées au schéma ci-dessus sans en modifier l'esprit. Par exemple, l'enlèvement de l'hydrocarbure léger à partir, soit de l'huile désasphaltée, soit de l'asphalte, peut être effectué dans une seule colonne, par exemple la colonne 11 pour l'huile désasphaltée et la colonne 21 pour l'asphalte. Dans ce cas les colonnes 23 et/ou 30 ne sont pas utilisées. On peut aussi, dans ce cas, prévoir un entraînement par vapeur d'eau ou gaz inerte dans la colonne unique, c'est-à-dire dans les colonnes 11 et 21.Many modifications can be made to the above diagram without changing the spirit. For example, 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.

Dans le schéma annexé, les compresseurs, les détendeurs et les pompes n'ont pas été représentés, dans un but de simplification. Il est toutefois entendu que l'opération de désasphaltage est effectuée le plus souvent, de manière connue, sous pression en raison de la nécessité de maintenir l'hydrocarbure léger en phase liquide à la température opératoire. Il est cependant avantageux de soumettre les effluents du désasphaltage à une détente de la pression pour favoriser l'évaporation du solvant.In the attached diagram, the compressors, the regulators and the pumps have not been shown, for the sake of simplification. It is however understood that the deasphalting operation is most often carried out, in a known manner, under pressure because of the need to keep the light hydrocarbon in the liquid phase at the operating temperature. It is however advantageous to subject the effluents from the deasphalting to a pressure relief to promote the evaporation of the solvent.

ExempleExample

On opère selon le schéma de la figure jointe.We operate according to the diagram in the attached figure.

On traite une charge d'hydrocarbures constituée par un résidu sous-vide dont les propriétés sont données dans le tableau joint.A hydrocarbon feedstock consisting of a vacuum residue whose properties are given in the attached table is treated.

La charge d'hydrocarbures est traitée par le n-pentane en rapport volume pentane/hydrocarbures de 4, à une température d'environ 175 °C en fond et 195 °C en tête. L'effluent de tête (huile désasphaltée + solvant) est soumis à une détente de pression et passe ensuite dans l'échangeur 9 où il subit un réchauffage. Dans le ballon 11, le solvant vaporisé sort en tête et passe dans l'échangeur 9. La phase liquide d'huile désasphaltée sort à 250 °C. Une partie est évacuée de l'installation après traitement par la vapeur d'eau (23). Une autre partie passe dans le four 16, chauffé au fuel, où elle est portée à 330-380 °C, puis dans l'échangeur 18 où elle sert à porter la température de la phase asphaltique d'environ 150 à 300 °C. Cette dernière est soumise à une vaporisation, après détente de la pression, de manière à récupérer le solvant. L'asphalte subit un entraînement par la vapeur d'eau, destiné à éliminer les traces de solvant puis il est évacué à une température d'environ 300 °C après réchauffage par une partie de l'huile désasphaltée sortant du four 16.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. In the flask 11, 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.

Après 6 mois de fonctionnement, on a examiné l'état de l'échangeur 18. Un dépôt goudronneux de faible épaisseur s'était formé, mais les propriétés de conduction thermique n'avaient pratiquement pas changé. Quant au four de chauffage de l'huile désasphaltée, il ne présentait aucun encrassement.

Figure imgb0001
After 6 months of operation, the state of the exchanger 18 was examined. A thin tarry deposit had formed, but the thermal conduction properties had practically not changed. As for the deasphalted oil heating furnace, it showed no fouling.
Figure imgb0001

A titre de comparaison, une unité de désasphaltage pratiquement identique, si ce n'est que l'échangeur 18 avait été remplacé par un four chauffé au fuel, a dû être arrêtée après seulement 3 mois de fonctionnement en raison d'une perte de charge excessive dans le four. Une inspection de celui-ci a montré des dépôts infusibles très durs en certains points chauds des tubes.For comparison, a practically identical deasphalting unit, except that the exchanger 18 had been replaced by an oven heated with fuel, had to be shut down after only 3 months of operation due to a pressure drop excessive in the oven. An inspection of this one showed very hard infusible deposits in certain hot spots of the tubes.

Claims (8)

1. A process for solvent deasphalting an asphaltene-containing residual hydrocarbon oil, wherein the residual oil is contacted with a light hydrocarbon solvent, in an extraction zone, deasphalting conditions are maintained to allow the formation of a liquid solvent-deasphalted oil phase and a fluid solvent-asphalt phase, the two resultant phases are separated and the solvent is separately vaporized from each of the two phases, so as to separately obtain a deasphalted oil and an asphaltic residue, characterized in
a) passing a portion of the deasphalted oil, substantially separated from the solvent, through a zone of indirect heating by flame, so as to raise its temperature,
b) contacting the reheated deasphalted oil from step (a), in indirect heat exchange relation, with the fluid solvent-asphalt phase, so as to deliver to this phase at least a part of the heat necessary to the vaporization of the solvent, and
c) admixing the deasphalted oil, after the heat exchange of step (b), with the liquid solvent-deasphalted oil phase recovered from the extraction zone.
2. A process according to claim 1, wherein a portion of the reheated deasphalted oil from step (a) is contacted, in indirect heat exchange relation, with the asphaltic residue, so as to reheat the latter and make it more fluid.
3. A process according to claim 1 or 2, wherein the temperature of the deasphalted oil is raised to 250-420 °C in step (a).
4. A process according to claim 1 or 2, wherein the temperature of the deasphalted oil is raised to 350-400 °C in step (a).
5. A process according to any of claims 1 to 4, wherein the solvent vapor separated from the deasphalted oil is contacted, in heat exchange relation, with the liquid solvent-deasphalted oil phase before subjecting the latter to the mixing of step (c).
6. A process according to any of claims 1 to 5, wherein the solvent is selected from the aliphatic hydrocarbons with 4 to 7 carbon atoms.
7. A process according to any of claims 1 to 5, wherein the solvent is selected from the aliphatic hydrocarbons with 5 to 7 carbon atoms.
8. A process according to any of claims 1 to 7, wherein the feed rate of the deasphalted oil supplied to step (a) is controlled according to the heat amount to be delivered to the fluid solvent-asphaltic oil phase.
EP81401814A 1980-11-28 1981-11-18 De-asphalting process with a solvent of residual hydrocarbon oils Expired EP0053535B1 (en)

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FR8025405A FR2495177B1 (en) 1980-11-28 1980-11-28 PROCESS FOR THE SOLVENT DEASPHALTATION OF HYDROCARBON RESIDUAL OILS
FR8025405 1980-11-28

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FR2495177A1 (en) 1982-06-04
FR2495177B1 (en) 1985-06-07

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