EP0819752B1 - 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
EP0819752B1
EP0819752B1 EP97401730A EP97401730A EP0819752B1 EP 0819752 B1 EP0819752 B1 EP 0819752B1 EP 97401730 A EP97401730 A EP 97401730A EP 97401730 A EP97401730 A EP 97401730A EP 0819752 B1 EP0819752 B1 EP 0819752B1
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EP
European Patent Office
Prior art keywords
reactor
reactors
effluents
fractionating unit
zone
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Expired - Lifetime
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EP97401730A
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English (en)
French (fr)
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EP0819752A1 (de
Inventor
Pierre Crespin
Laurent Mariette
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Total Marketing Services SA
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Total Raffinage Distribution SA
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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 a method and a improved charge conversion device of hydrocarbons, by hydrotreating in the presence of a catalyst, using two reactors and one fractionation unit.
  • the first reactor contains a catalyst preferably selected for its resistance qualities, which, while carrying out a first conversion step, eliminates 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 a intermediate fractionation between the two units of conversion.
  • the effluents from the first reactor are directed to an intermediate fractionation unit, where the lighter components formed by cracking in this first reactor are separated, while the heavy part not converted from the charge is led to a second reactor hydrocracking known as "more converting".
  • the effluents from this second stage can then either be fractionated by distillation in a second unit of fractionation, or much more economically (since we only use one area of fractionation instead of two), be recycled to the unit fractionation located between the two reactors.
  • the present invention aims to provide a method of conversion to overcome the disadvantages cited above.
  • the process according to the invention makes it possible to avoid the mixture between the distillation residues of the effluents of the first reactor and the distillation residues of second reactor effluents, which come from a much more conversion and therefore contain the most refractory compounds.
  • vaporized fractions from two areas of a common fractionation unit can then either be directed to treatments such as isomerization or the reforming of the essences, either still constituting jet fuel or diesel cuts.
  • the distillation residues from the fractionation unit after having been purged, can be recycled to the second reactor and, according to a characteristic of the invention, the purge can advantageously be constituted mainly by the withdrawal of residues from the distillation of effluents of the second reactor.
  • fraction recycled to the second reactor and the purge obtained are thus of improved quality, insofar as they consist mainly of residues of distillation which have been treated in two successive passes, without using fractionation units multiple.
  • the purging of effluent distillation residues from the second reactor can be performed directly on a tray of distillation of the fractionation unit located above the effluent introduction zone of the first reactor.
  • the distillation residues from said zones can be separated from each other a vertical partitioning arranged inside the fractionation unit.
  • the invention also aims to propose a device for the implementation of the method described above.
  • the conversion assembly by hydrotreating a hydrocarbon charge includes a first reactor 10, a fractionation unit 12 and a second reactor 14.
  • the load is brought first by a line 2 to the within reactor 10, where it undergoes a first conversion.
  • the effluent which results therefrom is then discharged towards the unit of fractionation 12, via line 16.
  • the corresponding distillation residue is extracted from the unit 12 by racking in 18, then is led by line 8 to the second reactor 14.
  • the effluent from the latter is recycled through line 20 to the fractionation unit 12.
  • separation means 22 which will be described in more detail below, delimit two separate zones 24, 26 of the fractionation unit 12.
  • the supply lines 16,20 of this unit lead on either side of the separation means 22, so as to isolate distillation residues from effluents from of each reactor 10.14.
  • the residue of distillation of the effluent from the second reactor is extracted at racking level 28, the location of which is different from that of racking 18.
  • This residue is then partly recycled to the second reactor 14 via line 30 and line 8, and partly evacuated 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 unit of fractionation 12 by various common withdrawals 36
  • FIGS 2, 3 and 4 show more precisely various types of separation means, in the unit of fractionation 12, admission zones 24 and 26 of effluents from the two reactors.
  • the means of separation can be constituted by a partitioning vertical, respectively 22 or 38, which extends from the bottom 40 of the fractionation unit 12.
  • the partition 22 can be arranged in a plane transverse vertical in unit 10 of fractionation 12 and, in particular, along a plane passing through the axis of this one (see figure 2).
  • the pipes inlet 16, 20, effluents from each reactor lead respectively into separate zones 24, 26, located on either side of this partitioning 22.
  • withdrawals 18, 28 from each of the distillation residues are arranged, at the bottom 40 of the unit 12, on either side partitioning 22.
  • the partition 38 can alternatively form a chimney concentric with the vertical wall 42 of the fractionation (see Figure 3).
  • the pipes 16.20 of the effluents end up respectively in separate areas 44,46, located inside and outside outside the chimney 38.
  • the racking 48, 50 of each of the residues are disposed at the bottom 40 of the reactor 12, inside and outside respectively from 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 an area 34 of common vaporization for each of the effluents, which additionally includes common racking 36 of fractions vaporized recondensed.
  • the separation means can be constituted by a horizontal plate 52, on either side of which lead to different heights, in the unit of fractionation 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 from the effluent coming from the upper pipe 20.
  • the residue 56 of the effluent from the lower pipe 16 is collected, as usual, at the bottom 40 of unit 12.
  • the distillation residues 54, 56 are extracted at different racking levels, 58 and 60 respectively.
  • the plate 52 is provided with a chimney 64, surmounted by a cap 66, allowing the passage of fractions sprayed with effluent from the lower zone, towards the top of the unit 12.
  • the cap 66 has a shape substantially conical, which directs the effluents liquids from upper line 20 on the separation plate 52, for perfect segregation residues 54, 56.
  • Figure 5 shows another conversion set according to the invention. This set is similar to that shown in Figure 1, except that the unit of fractionation includes two distillation columns 72, 74.
  • the load is brought first by line 112 to reactor 110, where it undergoes a first conversion.
  • the resulting effluent is then directed to the first fractionation column 72 through line 76.
  • the residue corresponding distillation is extracted at the racking 78, then leads to the second column of fractionation 74 through line 80.
  • the distillation residue obtained in this second column is extracted at rack 82, then evacuated via 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 tray of separation 52 similar to that shown in FIG. 4, of so that the respective supply lines 76, 84 (i.e. the effluents coming respectively from the first and second reactor) open on both sides of this tray, in order to isolate from each other the residues distillation correspondents.
  • the respective supply lines 76, 84 i.e. the effluents coming respectively from the first and second reactor
  • the distillation residue from the second effluent reactor 114 is extracted by racking 90, then directed to the second column 74 via line 92.
  • This column 74 is also provided with a horizontal plate 152 of separation, on either side from which the lines 80.92, respectively bringing the residue of distillation, in the first column 72, of the effluent from the first reactor 110, and the residue from distillation, in the first column, of the effluent from the second reactor, in order to isolate these residues the each other.
  • the residue from the second column 74, from the distillation effluent from the second reactor 114 is then extract at 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 outside the conversion assembly via line 102, in order to constitute a purge of improved quality.
  • 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 of each reactor.
  • the effluent from the first reactor is then directed to a fractionation unit, where it is separated into a fraction of gas, a fraction of gasoline, a fraction of diesel, and a residual fraction distilling above the range of diesel distillation and representing approximately 40% by weight total effluent.
  • the effluent from the second reactor is then returned to the fractionation unit.
  • a purge is also drawn off at from the residual fraction from the splitting.
  • the residual fraction from this fractionation is sent to a hydrocracking reactor, the operating conditions are the same as in the first experience.
  • the effluent from this second reactor is directed towards fractionation, where its residual fraction is isolated so as to constitute the purge.
  • the process conforms the invention allows, with equal severity, to obtain higher quality products (higher cetane number for diesel, lower viscosity and higher VI index for purging).
  • the effluent from the first reactor is then directed to a fractionation unit, where it is separated into a fraction of gas, a fraction of gasoline, a fraction of diesel, and a residual fraction distilling above the range of diesel distillation and representing approximately 40% by weight total effluent.
  • the effluent from the second reactor is then returned to the splitting.
  • a purge is also drawn off from the residual fraction from the fractionation.
  • This purge has the following properties: Purge Without segregation According to the invention PI 375 ° C 375 ° C Point 95% 600 ° C 600 ° C Viscosity at 100 ° C (in mm 2 / s or cst) - before dewaxing 5.2 5 - after dewaxing 5.4 5.2 Index VI - before dewaxing 140 145 - after dewaxing 120 125

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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)

Claims (15)

  1. Verfahren zur Umwandlung einer Kohlenwasserstoffbeschickung durch Hydrobehandlung unter Einsatz von mindestens zwei Wasserstoffbehandlungsreaktoren (10, 110, 14, 114) und einer einzigen dazwischen angeordneten Fraktionierungsanlage (12), bei dem alle Ableitungen aus den beiden Reaktoren fraktioniert werden, dadurch gekennzeichnet, dass:
    die Ableitungen aus den beiden Reaktoren (10, 110, 14, 114) in mindestens zwei bestimmten Zonen (24, 26) der Fraktionierungsanlage (12) gesammelt werden;
    die in der Fraktionierungsanlage (12) verdampften Fraktionen der Ableitungen aus den beiden Reaktoren (10, 110, 14, 114) rekondensiert und in mindestens eine gemeinsame Zone (34) dieser Anlage abgezogen werden;
    bestimmte Entnahmen (18, 28) aus den aus den beiden Zonen (24, 26) der Fraktionierungsanlage (12), in denen die Ableitungen von den Reaktoren (10, 110, 14, 114) behandelt werden, stammenden Destillationsrückständen vorgenommen werden;
    die Ableitung aus dem ersten Reaktor (10, 110) innerhalb einer ersten Zone (24) der Fraktionierungsanlage gesammelt wird, während die Entnahme (18) aus den aus der Zone (24) stammenden Destillationsrückständen dem Eingang des zweiten Reaktors (14, 114) zugeführt wird.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass eine Spülung (32) von verbesserter Qualität, welche die bei der Umwandlung am beständigsten schweren Kohlenwasserstoffe enthält, in erster Linie an der Entnahme (28) des Destillationsrückstands aus der Ableitung des zweiten Reaktors (14, 114) in der zweiten Zone (26) der Fraktionierungsanlage (12) durchgeführt wird.
  3. Verfahren nach Anspruch 2, dadurch gekennzeichnet, dass ein Teil des aus der Entnahme (28) stammenden Destillationsrückstandes aus der zweiten Zone (26) der Fraktionierungsanlage (12) zum zweiten Reaktor (14, 114) recycelt wird.
  4. Verfahren nach irgendeinem der Ansprüche 1 bis 3, dadurch gekennzeichnet, dass in den beiden Reaktoren (10, 110, 14, 114) mit unterschiedlichen Betriebsbedingungen gearbeitet wird, wobei insbesondere die Druckverhältnisse im Bereich des ersten Reaktors (10, 110) weniger schwierig sind.
  5. Verfahren nach irgendeinem der Ansprüche 1 bis 4, dadurch gekennzeichnet, dass die Spülung der Destillationsrückstände aus den vom zweiten Reaktor (14, 114) stammenden Ableitungen direkt auf einer Destillationsebene (52) oberhalb der Eintrittszone der Ableitungen aus dem ersten Reaktor (10, 110) erfolgt.
  6. Verfahren nach irgendeinem der Ansprüche 1 bis 4, dadurch gekennzeichnet, dass die aus den Zonen (24, 26) der Fraktionierungsanlage (12) stammenden Destillationsrückstände mit Hilfe einer vertikalen Unterteilung (22, 28) im Innern der Fraktionierungsanlage voneinander getrennt sind.
  7. Einrichtung zur Umwandlung einer Kohlenwasserstoffbeschickung durch Hydrobehandlung unter Einsatz von zwei in Reihe geschalteten Wasserstoffbehandlungsreaktoren (10, 110, 14, 114), einer zwischen den beiden Reaktoren angeordneten Fraktionierungsanlage (12) sowie Leitungen zur Zuführung der aus den Reaktoren stammenden Ableitungen zur Fraktionierungsanlage, wobei die Einrichtung dadurch gekennzeichnet ist, dass:
    die Fraktionierungsanlage (12) Trennvorrichtungen (22, 38) umfasst, die zwei bestimmte Zonen (24, 26) abgrenzt, an deren beiden Seiten die Leitungen (16, 20) für die Zuführung der Ableitungen aus den beiden Reaktoren (10, 110, 14, 114) münden,
    die Fraktionierungsanlage (12) mit zwei verschiedenen Entnahmen (18, 28) versehen ist, durch welche jeweils die Destillationsrückstände aus den Ableitungen der beiden Reaktoren (10, 110, 14, 114) abgezogen werden, und
    die Leitung zur Zuführung der Ableitungen aus dem ersten Reaktor (10, 110) in die erste Zone (24) der Fraktionierungsanlage mündet und aus dieser Zone die Entnahme (18) des Destillationsrückstandes erfolgt, der dem zweiten Reaktor (14, 114) zugeführt wird.
  8. Einrichtung zur Umwandlung nach Anspruch 7, dadurch gekennzeichnet, dass es sich bei den Trennvorrichtungen um eine vertikale Unterteilung (22, 38) handelt, die sich vom Boden (60) der Fraktionierungsanlage (12) aus erstreckt.
  9. Einrichtung zur Umwandlung nach Anspruch 8, dadurch gekennzeichnet, dass die Unterteilung einen konzentrisch zur vertikalen Wandung (42) der Fraktionierungsanlage (12) verlaufenden Kamin (38) bildet.
  10. Einrichtung zur Umwandlung nach Anspruch 8, dadurch gekennzeichnet, dass die Unterteilung eine Wand (22) ist, die in einer zur Fraktionierungsanlage querverlaufenden Ebene liegt.
  11. Einrichtung zur Umwandlung nach Anspruch 7, dadurch gekennzeichnet, dass die Trennvorrichtungen (52) horizontal verlaufen und dass die beiden Leitungen (16, 20) zur Zuführung der Ableitungen aus den beiden Reaktoren (10, 110, 14, 114) in verschiedenen Höhen in die Fraktionierungsanlage (12) münden.
  12. Einrichtung zur Umwandlung nach Anspruch 11, dadurch gekennzeichnet, dass die horizontalen Trennvorrichtungen durch eine Platte (52) gebildet werden, die mindestens einen Kamin (54) umfasst.
  13. Einrichtung zur Umwandlung nach irgendeinem der Ansprüche 7 bis 12, dadurch gekennzeichnet, dass die Fraktionierungsanlage (12) eine gemeinsame Verdampfungszone (34) für die Ableitungen aus jedem der Reaktoren (10, 110, 14, 114) umfasst.
  14. Einrichtung zur Umwandlung nach irgendeinem der Ansprüche 7 bis 13, bei der die Fraktionierungsanlage mit mindestens zwei in Reihe geschalteten und unter atmosphärischem Druck oder Vakuum stehenden Kolonnen (72, 74) versehen ist, dadurch gekennzeichnet, dass jede Kolonne:
    Trennvorrichtungen (52, 152) zur Begrenzung von zwei bestimmten Zonen umfasst, an deren beiden Seiten jeweils die Ableitungen der beiden Reaktoren (10, 110, 14, 114) einmünden,
    zwei verschiedene Entnahmevorrichtungen (80, 90; 82, 98) aufweist, durch welche jeweils die flüssigen Restfraktionen der aus den beiden Reaktoren stammenen Ableitungen abgezogen werden,
    und mit einer gemeinsamen Verdampfungszone (86, 94) für die aus jedem Reaktor stammenden Ableitungen versehen ist.
  15. Einrichtung zur Umwandlung nach irgendeinem der Ansprüche 7 bis 14, dadurch gekennzeichnet, dass es sich bei dem ersten Reaktor um einen Reaktor zur Hydrobehandlung und bei dem zweiten Reaktor um einen Reaktor zum Hydrokracken handelt.
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
FR9609090 1996-07-19
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

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EP0819752A1 EP0819752A1 (de) 1998-01-21
EP0819752B1 true 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

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

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8591726B2 (en) 2010-06-30 2013-11-26 Exxonmobil Research And Engineering Company Two stage hydroprocessing with divided wall column fractionator
US8647500B2 (en) 2010-06-30 2014-02-11 Exxonmobil Research And Engineering Company Integrated gas and liquid phase processing of biocomponent feedstocks
US8828217B2 (en) 2010-06-30 2014-09-09 Exxonmobil Research And Engineering Company Gas and liquid phase hydroprocessing for biocomponent feedstocks
US8852425B2 (en) 2009-12-01 2014-10-07 Exxonmobil Research And Engineering Company Two stage hydroprocessing with divided wall column fractionator
US9028673B2 (en) 2011-11-09 2015-05-12 Exxonmobil Research And Engineering Company Production of low cloud point distillates
US9290703B2 (en) 2010-04-23 2016-03-22 Exxonmobil Research And Engineering Company Low pressure production of low cloud point diesel
US9493718B2 (en) 2010-06-30 2016-11-15 Exxonmobil Research And Engineering Company Liquid phase distillate dewaxing

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2757872B1 (fr) * 1996-12-31 1999-06-25 Total Raffinage Distribution Procede d'hydrotraitement d'une charge hydrocarbonee et dispositif pour sa mise en oeuvre

Family Cites Families (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 (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8852425B2 (en) 2009-12-01 2014-10-07 Exxonmobil Research And Engineering Company Two stage hydroprocessing with divided wall column fractionator
US9290703B2 (en) 2010-04-23 2016-03-22 Exxonmobil Research And Engineering Company Low pressure production of low cloud point diesel
US8591726B2 (en) 2010-06-30 2013-11-26 Exxonmobil Research And Engineering Company Two stage hydroprocessing with divided wall column fractionator
US8647500B2 (en) 2010-06-30 2014-02-11 Exxonmobil Research And Engineering Company Integrated gas and liquid phase processing of biocomponent feedstocks
US8828217B2 (en) 2010-06-30 2014-09-09 Exxonmobil Research And Engineering Company Gas and liquid phase hydroprocessing for biocomponent feedstocks
US9493718B2 (en) 2010-06-30 2016-11-15 Exxonmobil Research And Engineering Company Liquid phase distillate dewaxing
US9028673B2 (en) 2011-11-09 2015-05-12 Exxonmobil Research And Engineering Company Production of low cloud point distillates

Also Published As

Publication number Publication date
ATE200511T1 (de) 2001-04-15
FR2751339B1 (fr) 2003-08-08
EP0819752A1 (de) 1998-01-21
ES2157537T3 (es) 2001-08-16
FR2751339A1 (fr) 1998-01-23
DE69704519D1 (de) 2001-05-17
DE69704519T2 (de) 2001-08-09

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