EP0095792A2 - Procédé pour la séparation d'un liquide à plusieurs composants - Google Patents

Procédé pour la séparation d'un liquide à plusieurs composants Download PDF

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Publication number
EP0095792A2
EP0095792A2 EP83200509A EP83200509A EP0095792A2 EP 0095792 A2 EP0095792 A2 EP 0095792A2 EP 83200509 A EP83200509 A EP 83200509A EP 83200509 A EP83200509 A EP 83200509A EP 0095792 A2 EP0095792 A2 EP 0095792A2
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EP
European Patent Office
Prior art keywords
column
steam
fraction
liquid
pressure
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.)
Granted
Application number
EP83200509A
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German (de)
English (en)
Other versions
EP0095792A3 (en
EP0095792B1 (fr
Inventor
Pieter Van Der Heyden
Alfred Louis Van Kleef
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.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
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Publication date
Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of EP0095792A2 publication Critical patent/EP0095792A2/fr
Publication of EP0095792A3 publication Critical patent/EP0095792A3/en
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Publication of EP0095792B1 publication Critical patent/EP0095792B1/fr
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Classifications

    • 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
    • C10G7/00—Distillation of hydrocarbon oils

Definitions

  • the invention relates to a process for separating a multi-component liquid, in particular reduced crude into a plurality of fractions. More specifically the present invention relates to the separation of reduced crude with the objective to maximize the production of valuable distillate- fractions and to minimize the production of less valuable residue fraction.
  • Vacuum flashing is a process wherein the reduced crude is heated resulting in partial vaporization of the crude, whereafter the so formed mixture of vapour (s) and remaining liquid is passed to a flash tower operated at a very low absolute pressure to separate the vapours from the liquid.
  • the separated vapours are condensed for yielding one or more of so-called flashed distillate(s).
  • the liquid leaves the flash tower as bottoms fraction, and is called short residue.
  • the vacuum in a flash tower is normally obtained by a steam ejector system connected with the top of the flash tower.
  • the object of the present invention is to improve the above-mentioned known process for separating a multi-component liquid, in order to increase the production of distillate fractions from a given feed whilst consuming less energy compared to the known processes.
  • the process for separating a multi-component liquid comprises heating the multi-conponent liquid to provide a mixture of a liquid phase and a vapour phase, passing the mixture into a lower part of a first column while maintaining a subatmospheric pressure within the first column, components of the mixture being separated to yield at least one distillate fraction and a bottoms fraction, withdrawing said fractions from the first column, passing the bottoms fraction to a second column while maintaining a pressure within the second column which is higher than the pressure in the first column contacting the bottoms fraction with steam in the second column to obtain at least one heavy-distillate fraction and a residual fraction, the sub-atmospheric pressure in the first column being maintained by a steam ejector system, wherein driving steam of said steam ejector system is used in the second column for contacting the bottoms fraction.
  • the bottoms fraction from the first column, the flash tower is stripped with steam in a separate column.
  • the pressure in the first column can be maintained at a lower level compared to the pressure, prevailing in systems where flashing and steam stripping are carried out in one column.
  • a lower pressure results in an increased yield of distillate.
  • Reduced crude introduced via line 1 is passed through a plurality of preheaters 2 and a heating furnace 3 where the material is partially vaporized and heated to a transfer temperature of, for example, 425°C.
  • the transfer temperature is preferably the highest temperature to which the residue can be heated without any appreciable cracking, i.e. the incipient cracking temperature.
  • this temperature is normally in the range between 400 and 440°C.
  • the heated and partially vaporized reduced crude is subsequently passed via a transfer line 4 to a first column 5, hereinafter called flash tower.
  • the pressure in the flash tower 5 is maintained at a sub-atmospheric level by a steam ejector system 6, ccmmunicating with the flash tower 5 via a line 7.
  • a suitable pressure in the flash zone of the flash tower 5 may be in the order of magnitude of about 20 mm Hg absolute.
  • Each spray section 13 is composed of a plurality of liquid spray nozzles 14 and a draw-off tray 15, and optionally a layer of packing material 16 arranged between the spray nozzles 14 and the accompanying draw-off tray 15, for intensifying the contact between liquid and rising vapour.
  • the draw-off trays 15 are each provided with openings for the passage of rising vapour and a lower part for collecting descending liquid.
  • the draw-off trays may for example be formed by grid trays or bubble cap trays.
  • the nozzles 14 of the lowermost spray section 13 are supplied with liquid from the draw-off tray of the next upper spray section. Thereto the liquid from the next upper spray section is passed through an accumulator 16 and is partially recirculated via pump 17 and a return line 18 to the lower most spray nozzles 14. Upon passing through the demister mat 12 arranged above the lowermost spray section 13, any entrained liquid is separated from the vapour so that substantially liquid-free vapour enters the upper region of the flash tower 5.
  • the vapour passing upward through the flash tower 5 is gradually condensed in multiple boiling fractions by contact with relatively cool liquid.
  • liquid is discharged at several levels from the upper part of the flash tower 5, passed through coolers 19 for cooling and reintroduced into the flash tower 5 via the nozzles 14.
  • the upward flow of vapour is contacted with the relatively cool liquid, so that the vapour cools down and is partly condensed.
  • the flash tower 5 shown in the drawing is provided with 4 product side withdrawal lines 20.
  • the remaining vapour if any is withdrawn over the top of the flash tower 5 via line 7 by the action of the steam ejector system 6.
  • the driving steam from the steam ejector system 6 is directly passed together with vapour, if any, from the flash tower 5 via line 21 into a second column 22, hereinafter called stripping tower, which is maintained at a higher sub-atmospheric pressure than the pressure in the flash tower 5.
  • the driving steam is used for stripping the bottoms fraction from the flash tower supplied into said stripping tower 22 via line 11.
  • the bottoms fraction Prior to introducing the bottoms fraction into the stripping tower 22, the bottoms fraction is heated in a furnace 23 to bring the bottoms fraction temperature at or near its initial boiling point at the pressure prevailing in the stripping tower 22.
  • the downward flowing bottoms fraction introduced into an upper region of the stripping tower 22 is contacted with the upward flowing steam introduced into a lower region of the stripping tower 22.
  • the stripping tower 22 is provided with a plurality of contact trays 24, causing a redistribution of the liquid and steam over the cross section of the stripping tower.
  • the contact trays may for example be formed by grid trays, sieve trays or bubble cap trays.
  • the stripping tower 22 is suitably provided with a quench system 25 containing heat exchange means, for cooling a part of the residual fraction and reintroducing said cooled liquid into the lower part of the column at a level higer than the level of withdrawal.
  • the upper part of the stripping tower 22 is provided with a spray section 26 for reintroducing withdrawn cooled liquid into the stripping tower 22 for liquefying the vapour in the top of the column to prevent entrainment of vapour by the steam leaving the stripping tower 22 via line 27 over the top thereof.
  • the stripping tower 22 as shown in the drawing is further provided with two product withdrawal lines 28 and 29 for withdrawing a residual fraction and a heavy-distillate fraction, respectively.
  • the steam passed over the top of the stripping tower 22 is introduced into a plurality of condensers 30, one of which is shown in the drawing, for condensing the steam at substantially atmospheric pressure.
  • the heat obtained from the products withdrawn from the flash tower 5 and the stripping tower 22 may be applied for preheating the reduced crude to be introduced into the flash tower 5.
  • the pressure in the stripping tower 22 will also be substantially higher than the flash tower pressure. To obtain the highest possible amount of more valuable heavy distillate fraction and the least possible amount of less valuable residual fraction, the pressure in the stripping tower 22 should however be kept at a low sub-atmospheric pressure.
  • the minimum pressure in the stripping tower 22 is determined by the minimum condensation pressure of the steam leaving the stripping tower 22.
  • the pressure in the flash tower can be considerably reduced compared with wet fractionating systems wherein steam is introduced into the flash tower.
  • a lower pressure means in general a higher output of valuable products and less bottom product.
  • the present invention is not restricted to a process wherein the initial separation between liquid and vapour in the flash tower 5 is obtained by causing the reduced crude to flow along a plurality of vanes 8.
  • the reduced crude may for example be passed through a centrifugal separator positioned in the flash tower 5.
  • the invention is not restricted to the particular arrangement of spray sections, packing material and demister mat as shown in the drawing.
  • the packing material and demister mat can for example be suitably replaced by further spray sections.
  • the number of spray sections is chosen in relation to the number of side products which should be yielded at processing reduced crude with a given composition.

Landscapes

  • 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)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
EP83200509A 1982-05-28 1983-04-12 Procédé pour la séparation d'un liquide à plusieurs composants Expired EP0095792B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB8215707 1982-05-28
GB8215707 1982-05-28

Publications (3)

Publication Number Publication Date
EP0095792A2 true EP0095792A2 (fr) 1983-12-07
EP0095792A3 EP0095792A3 (en) 1985-10-02
EP0095792B1 EP0095792B1 (fr) 1988-01-13

Family

ID=10530713

Family Applications (1)

Application Number Title Priority Date Filing Date
EP83200509A Expired EP0095792B1 (fr) 1982-05-28 1983-04-12 Procédé pour la séparation d'un liquide à plusieurs composants

Country Status (6)

Country Link
EP (1) EP0095792B1 (fr)
JP (1) JPS58214302A (fr)
AU (1) AU555741B2 (fr)
CA (1) CA1197806A (fr)
DE (1) DE3375304D1 (fr)
ZA (1) ZA833819B (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013107738A1 (fr) * 2012-01-17 2013-07-25 Shell Internationale Research Maatschappij B.V. Procédé de distillation sous vide d'un flux d'hydrocarbure brut

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB8903011D0 (en) * 1989-02-10 1989-03-30 Shell Int Research Vacuum distillation process
CH684057A5 (de) * 1992-11-30 1994-07-15 Buss Ag Verfahren zum Weiterverarbeiten des Vakuumrückstandes in einer Rohölraffinerie.
DE10037774A1 (de) * 2000-08-03 2002-02-14 Bayer Ag Verfahren und Vorrichtung zur Gewinnung organischer Substanzen aus einem diese Substanzen enthaltenden Gasgemisch

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US204707A (en) * 1878-06-11 Improvement in vehicle-springs
US2092528A (en) * 1927-07-28 1937-09-07 Lummus Co Method of and apparatus for distilling petroleum mixtures
US3301778A (en) * 1964-06-15 1967-01-31 Phillips Petroleum Co Fractional distillation
EP0070140A2 (fr) * 1981-07-10 1983-01-19 Exxon Research And Engineering Company Procédé de distillation

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US204707A (en) * 1878-06-11 Improvement in vehicle-springs
US2092528A (en) * 1927-07-28 1937-09-07 Lummus Co Method of and apparatus for distilling petroleum mixtures
US3301778A (en) * 1964-06-15 1967-01-31 Phillips Petroleum Co Fractional distillation
EP0070140A2 (fr) * 1981-07-10 1983-01-19 Exxon Research And Engineering Company Procédé de distillation

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013107738A1 (fr) * 2012-01-17 2013-07-25 Shell Internationale Research Maatschappij B.V. Procédé de distillation sous vide d'un flux d'hydrocarbure brut
CN104053751A (zh) * 2012-01-17 2014-09-17 国际壳牌研究有限公司 真空蒸馏烃物流的方法
CN104053751B (zh) * 2012-01-17 2017-09-15 国际壳牌研究有限公司 真空蒸馏烃物流的方法
US9783741B2 (en) 2012-01-17 2017-10-10 Shell Oil Company Process for vacuum distillation of a crude hydrocarbon stream

Also Published As

Publication number Publication date
AU555741B2 (en) 1986-10-09
DE3375304D1 (en) 1988-02-18
AU1500383A (en) 1983-12-01
ZA833819B (en) 1984-02-29
JPH0512001B2 (fr) 1993-02-17
EP0095792A3 (en) 1985-10-02
EP0095792B1 (fr) 1988-01-13
JPS58214302A (ja) 1983-12-13
CA1197806A (fr) 1985-12-10

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