EP0819752A1 - Verfahren und Einrichtung zur Umwandlung einer Kohlenwasserstoffbeschickung mit zwei Wasserstoffbehandlungsreaktoren und einer einzigen Fraktionierungsanlage - Google Patents

Verfahren und Einrichtung zur Umwandlung einer Kohlenwasserstoffbeschickung mit zwei Wasserstoffbehandlungsreaktoren und einer einzigen Fraktionierungsanlage Download PDF

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Publication number
EP0819752A1
EP0819752A1 EP97401730A EP97401730A EP0819752A1 EP 0819752 A1 EP0819752 A1 EP 0819752A1 EP 97401730 A EP97401730 A EP 97401730A EP 97401730 A EP97401730 A EP 97401730A EP 0819752 A1 EP0819752 A1 EP 0819752A1
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EP
European Patent Office
Prior art keywords
reactor
effluents
fractionation unit
reactors
zone
Prior art date
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Granted
Application number
EP97401730A
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English (en)
French (fr)
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EP0819752B1 (de
Inventor
Pierre Crespin
Laurent Mariette
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.)
Total Marketing Services SA
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Total Raffinage Distribution SA
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Publication of EP0819752A1 publication Critical patent/EP0819752A1/de
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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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/10—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only cracking steps
    • 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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps

Definitions

  • the present invention relates to an improved process and device for converting a hydrocarbon feedstock, by hydrotreating in the presence of a catalyst, using two reactors and a single fractionation unit.
  • hydrotreating conversion processes aim to convert relatively inexpensive, high-boiling hydrocarbon charges into lighter, much more recoverable charges.
  • the first reactor contains a catalyst preferably selected for its strength qualities, which, while carrying out a first conversion step, makes it possible to eliminate some of these pollutants, such as sulfur and nitrogen.
  • the second reactor contains a catalyst more sensitive to pollutants, but also much more active and therefore more "converting".
  • one solution consists in providing for an intermediate fractionation between the two conversion units.
  • the US patent US Pat. is first sent to a first hydrotreatment reactor, where it is purified of its impurities.
  • the effluents from the first reactor are sent to an intermediate fractionation unit, where the lighter components formed by cracking in this first reactor are separated, while the unconverted heavy part of the feed is led to a second hydrocracking reactor called "more converting".
  • the effluents from this second stage can then either be fractionated by distillation in a second fractionation unit, or, in a much more economical manner (since only one fractionation zone is used instead of two), be recycled to the fractionation unit located between the two reactors.
  • the present invention aims to provide a conversion method which overcomes the aforementioned drawbacks.
  • the process according to the invention makes it possible to avoid mixing between the residues from the distillation of the effluents from the first reactor and the residues from the distillation of the effluents from the second reactor, which result from a much more extensive conversion and therefore contain the compounds more refractory.
  • the vaporized fractions originating from two zones of a common fractionation unit, can then either be directed to treatments such as isomerization or the reforming of gasolines, or even constitute jet fuel or diesel fuel cuts.
  • the distillation residues from the fractionation unit after undergoing a purge, can be recycled to the second reactor and, according to a characteristic of the invention, the purge can advantageously consist mainly of withdrawing the residues from the distillation of effluents from the second reactor.
  • the fraction recycled to the second reactor and the purge obtained are thus of improved quality, insofar as they consist mainly of distillation residues which have been treated in two successive passes, without using multiple fractionation units.
  • the purging of the distillation residues of the effluents from the second reactor can be carried out directly on a distillation plate of the fractionation unit located above the effluent introduction zone of the first reactor .
  • the distillation residues from said zones can be separated from one another, a vertical partitioning disposed inside the fractionation unit.
  • the invention also aims to propose a device for implementing the method described above.
  • the conversion assembly by hydrotreatment of a hydrocarbon feedstock comprises a first reactor 10, a fractionation unit 12 and a second reactor 14.
  • the charge is brought first by a line 2 within the reactor 10, where it undergoes a first conversion.
  • the effluent which results therefrom is then evacuated towards the fractionation unit 12, via the conduit 16.
  • the corresponding distillation residue is extracted from the unit 12 by drawing off at 18, then is conducted by the line 8 to the second reactor 14.
  • the effluent from the latter is recycled via line 20 to the fractionation unit 12.
  • separation means 22 which will be described in more detail below, delimit two distinct zones 24, 26 of the fractionation unit 12.
  • the supply lines 16, 20 of this unit open out and on the other side the separation means 22, so as to isolate the distillation residues from the effluents coming from each reactor 10,14.
  • the distillation residue from the effluent from the second reactor is extracted at the rack 28, the location of which is different from that of the rack 18.
  • This residue is then partly recycled to the second reactor 14 via line 30 and line 8, and partly removed from the conversion assembly via line 32, in order to constitute a purge of improved quality.
  • the vaporized fractions of the effluents from each reactor 10,14 are recondensed at level of a common area 34 and extracted from the fractionation unit 12 by various common withdrawals 36
  • FIGs 2, 3 and 4 show more precisely various types of separation means, in the fractionation unit 12, of the intake zones 24 and 26 of the effluents from the two reactors.
  • the separation means can be constituted by a vertical partition, respectively 22 or 38, which extends from the bottom 40 of the fractionation unit 12.
  • the partition 22 can be arranged along a transverse vertical plane in the unit 10 of the fractionation 12 and, in particular, along a plane passing through the axis of the latter (see FIG. 2).
  • the inlet pipes 16, 20, of the effluents from each reactor open respectively into separate zones 24, 26, located on either side of this partitioning 22.
  • the withdrawals 18, 28 of each of the distillation residues are disposed, at the bottom 40 of the unit 12, on either side of the partition 22.
  • the partition 38 can alternatively form a chimney concentric with the vertical wall 42 of the fractionation unit (see FIG. 3).
  • the inlet pipes 16, 20 of the effluents open respectively into separate zones 44, 46, located inside and outside the chimney 38.
  • the withdrawals 48, 50 of each of the residues are disposed at the bottom 40 of the reactor 12, respectively inside and outside the chimney 38.
  • the vertical partitions 22, 38 extend only over a small part of the height of the fractionation unit 12, so as to leave a zone 34 of common vaporization for each of the effluents, which includes in in addition to common withdrawals 36 recondensed vaporized fractions.
  • the separation means can be constituted by a horizontal plate 52, on either side of which open at different heights, in the fractionation unit 12, the effluents from each reactor.
  • the plate 52 is dimensioned so as to cover the entire cross section of the unit, in order to collect the distillation residue 54 of the effluent coming from the upper pipe 20.
  • the residue 56 of the effluent coming from the lower pipe 16 is collected, in the usual way, at the bottom 40 of the unit 12.
  • the distillation residues 54, 56 are extracted at different rackings, respectively 58 and 60.
  • the plate 52 is provided with a chimney 64, surmounted by a cap 66, allowing the passage of the vaporized fractions of the effluent coming from the lower zone, towards the top of the unit 12.
  • the cap 66 has a substantially conical shape , which makes it possible to direct the liquid effluents coming from the upper pipe 20 onto the separation plate 52, with a view to perfect segregation of the residues 54, 56.
  • FIG. 5 represents another conversion assembly in accordance with the invention. This assembly is similar to that shown in FIG. 1, except that the fractionation unit includes two distillation columns 72, 74.
  • the charge is brought first by line 112 to reactor 110, where it undergoes a first conversion.
  • the effluent which results therefrom is then directed to the first fractionation column 72 by the pipe 76.
  • the corresponding distillation residue is extracted at the draw-off 78, then leads to the second fractionation column 74 by the pipe 80.
  • the distillation residue obtained in this second column is extracted at rack 82, then discharged through line 112 to the second reactor 114.
  • the effluent from the latter is recycled through line 84 to the first fractionation column 72.
  • the first column 72 is provided with a separation plate 52 similar to that shown in FIG. 4, so that the respective supply lines 76, 84 (that is to say the effluents coming from the first and from the second reactor) emerge on either side of this tray, in order to isolate from each other the corresponding distillation residues.
  • the distillation residue from the effluent from the second reactor 114 is extracted by the racking 90, then directed to the second column 74 by the line 92.
  • This column 74 is also provided with a horizontal separating plate 152, on both sides. other from which open the lines 80, 92, respectively bringing the distillation residue, in the first column 72, of the effluent coming from the first reactor 110, and the distillation residue, in the first column, of the effluent coming from the second reactor, in order to isolate these residues from each other.
  • the residue from the second column 74, from the distillation of the effluent from the second reactor 114, is then extracted at the rack 98, placed immediately above the separation plate 152.
  • This residue is then partly recycled to the second reactor via line 100, and partly directed out of the conversion assembly via line 102, in order to constitute an improved quality purge.
  • the device described above is applicable to a fractionation unit including any number of columns, atmospheric or vacuum, keeping in each column the segregation between the effluents from each reactor.
  • the effluent from the first reactor is then directed to a fractionation unit, where it is separated into a gas fraction, a petrol fraction, a diesel fraction, and a residual fraction distilling above the diesel distillation range and representing approximately 40% of the total weight of the effluent.
  • the effluent from the second reactor is then returned to the fractionation unit.
  • a purge is also drawn off from the residual fraction from the fractionation.
  • the residual fraction from this fractionation is sent to a hydrocracking reactor, the operating conditions of which are the same as in the first experiment.
  • the effluent from this second reactor is directed to the fractionation, where its residual fraction is isolated so as to constitute the purge.
  • the process according to the invention makes it possible, with equal severity, to obtain products of higher quality (higher cetane number for diesel, lower viscosity and higher VI number for purging) .
  • the effluent from the first reactor is then sent to a fractionation unit, where it is separated into a gas fraction, a gasoline fraction, a diesel fraction, and a residual fraction distilling above the distillation interval. diesel and representing approximately 40% of the total weight of the effluent.
  • the effluent from the second reactor is then returned to the fractionation.
  • a purge is also drawn off from the residual fraction from the fractionation.

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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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
EP97401730A 1996-07-19 1997-07-17 Verfahren und Einrichtung zur Umwandlung einer Kohlenwasserstoffbeschickung mit zwei Wasserstoffbehandlungsreaktoren und einer einzigen Fraktionierungsanlage Expired - Lifetime EP0819752B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9609090A FR2751339B1 (fr) 1996-07-19 1996-07-19 Procede et dispositif de conversion d'une charge d'hydrocarbures, mettant en oeuvre deux reacteurs d'hydrotraitement et une seule unite de fractionnement
FR9609090 1996-07-19

Publications (2)

Publication Number Publication Date
EP0819752A1 true EP0819752A1 (de) 1998-01-21
EP0819752B1 EP0819752B1 (de) 2001-04-11

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EP97401730A Expired - Lifetime EP0819752B1 (de) 1996-07-19 1997-07-17 Verfahren und Einrichtung zur Umwandlung einer Kohlenwasserstoffbeschickung mit zwei Wasserstoffbehandlungsreaktoren und einer einzigen Fraktionierungsanlage

Country Status (5)

Country Link
EP (1) EP0819752B1 (de)
AT (1) ATE200511T1 (de)
DE (1) DE69704519T2 (de)
ES (1) ES2157537T3 (de)
FR (1) FR2751339B1 (de)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0851020A1 (de) * 1996-12-31 1998-07-01 Total Raffinage Distribution S.A. Verfahren und Einrichtung zur Wasserstoffbehandlung von Kohlenwasserstoffeinsätzen
WO2011068666A1 (en) 2009-12-01 2011-06-09 Exxonmobil Research And Engineering Company Two stage hydroprocessing with divided wall column fractionator
WO2011133829A1 (en) 2010-04-23 2011-10-27 Exxonmobil Research And Engineering Company Low pressure production of low cloud point diesel
WO2012012088A2 (en) 2010-06-30 2012-01-26 Exxonmobil Research And Engineering Company Two stage hydroprocessing with divided wall column fractionator
WO2012012091A3 (en) * 2010-06-30 2012-12-27 Exxonmobil Research And Engineering Company Integrated gas and liquid phase processing of biocomponent feedstocks
WO2013070566A1 (en) 2011-11-09 2013-05-16 Exxonmobil Research And Engineering Company Production of low cloud point distillates

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SG10201503121SA (en) 2010-06-30 2015-06-29 Exxonmobil Res & Eng Co Liquid phase distillate dewaxing
EP2588431A2 (de) 2010-06-30 2013-05-08 ExxonMobil Research and Engineering Company Gas- und flüssigphasen-hydroverarbeitung für biokomponentenrohstoffe

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB394858A (en) * 1932-03-08 1933-07-06 Lummus Co Improvements in or relating to methods of and apparatus for dividing petroleum bottoms
US3437584A (en) * 1967-08-09 1969-04-08 Universal Oil Prod Co Method for converting heavy carbonaceous materials
US4713167A (en) * 1986-06-20 1987-12-15 Uop Inc. Multiple single-stage hydrocracking process

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB394858A (en) * 1932-03-08 1933-07-06 Lummus Co Improvements in or relating to methods of and apparatus for dividing petroleum bottoms
US3437584A (en) * 1967-08-09 1969-04-08 Universal Oil Prod Co Method for converting heavy carbonaceous materials
US4713167A (en) * 1986-06-20 1987-12-15 Uop Inc. Multiple single-stage hydrocracking process

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0851020A1 (de) * 1996-12-31 1998-07-01 Total Raffinage Distribution S.A. Verfahren und Einrichtung zur Wasserstoffbehandlung von Kohlenwasserstoffeinsätzen
WO2011068666A1 (en) 2009-12-01 2011-06-09 Exxonmobil Research And Engineering Company Two stage hydroprocessing with divided wall column fractionator
WO2011133829A1 (en) 2010-04-23 2011-10-27 Exxonmobil Research And Engineering Company Low pressure production of low cloud point diesel
WO2012012088A2 (en) 2010-06-30 2012-01-26 Exxonmobil Research And Engineering Company Two stage hydroprocessing with divided wall column fractionator
WO2012012091A3 (en) * 2010-06-30 2012-12-27 Exxonmobil Research And Engineering Company Integrated gas and liquid phase processing of biocomponent feedstocks
CN102985515A (zh) * 2010-06-30 2013-03-20 埃克森美孚研究工程公司 生物组分原料的联合气相和液相加工
WO2012012088A3 (en) * 2010-06-30 2013-05-02 Exxonmobil Research And Engineering Company Two stage hydroprocessing with divided wall column fractionator
CN103370397A (zh) * 2010-06-30 2013-10-23 埃克森美孚研究工程公司 具有分隔壁塔分馏器的两段加氢操作
AU2011280064B2 (en) * 2010-06-30 2015-05-14 Exxonmobil Research And Engineering Company Two stage hydroprocessing with divided wall column fractionator
CN103370397B (zh) * 2010-06-30 2016-08-03 埃克森美孚研究工程公司 具有分隔壁塔分馏器的两段加氢操作
WO2013070566A1 (en) 2011-11-09 2013-05-16 Exxonmobil Research And Engineering Company Production of low cloud point distillates

Also Published As

Publication number Publication date
ES2157537T3 (es) 2001-08-16
DE69704519D1 (de) 2001-05-17
DE69704519T2 (de) 2001-08-09
ATE200511T1 (de) 2001-04-15
FR2751339A1 (fr) 1998-01-23
EP0819752B1 (de) 2001-04-11
FR2751339B1 (fr) 2003-08-08

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