EP0251838B1 - Procédé de séparation de solvant d'un mélange de solvant et d'hydrocarbures, et installation comportant application de ce procédé - Google Patents

Procédé de séparation de solvant d'un mélange de solvant et d'hydrocarbures, et installation comportant application de ce procédé Download PDF

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Publication number
EP0251838B1
EP0251838B1 EP87401232A EP87401232A EP0251838B1 EP 0251838 B1 EP0251838 B1 EP 0251838B1 EP 87401232 A EP87401232 A EP 87401232A EP 87401232 A EP87401232 A EP 87401232A EP 0251838 B1 EP0251838 B1 EP 0251838B1
Authority
EP
European Patent Office
Prior art keywords
solvent
evaporation
exchanger
flasks
flask
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP87401232A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0251838A1 (fr
Inventor
Patricia Delbourgo
Michel Coupard
Jean-Jacques Delorme
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.)
Francaise dEtudes et de Construction Technip SA
Original Assignee
Francaise dEtudes et de Construction Technip SA
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Francaise dEtudes et de Construction Technip SA filed Critical Francaise dEtudes et de Construction Technip SA
Publication of EP0251838A1 publication Critical patent/EP0251838A1/fr
Application granted granted Critical
Publication of EP0251838B1 publication Critical patent/EP0251838B1/fr
Expired legal-status Critical Current

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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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/28—Recovery of used solvent
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S203/00—Distillation: processes, separatory
    • Y10S203/02—Laboratory distillation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S203/00—Distillation: processes, separatory
    • Y10S203/04—Heat pump

Definitions

  • the present invention essentially relates to a process for the extraction of solvent from a mixture of solvent and of hydrocarbons without the addition of external heat.
  • a method for separating a solvent from a solvent-hydrocarbon mixture by staged evaporation of the solvent at decreasing temperatures uses a succession of solvent evaporation exchangers, the first being heated by steam at 195 ° C outside the process and externally licking the wall of the exchanger.
  • the object of the present invention is therefore to remedy the above drawbacks in particular by proposing a method and an installation for recovering solvent in solvent-hydrocarbon mixtures, which are particularly simple, reliable and inexpensive in the sense that they do not require no external heat input.
  • the subject of the invention is a process for the separation of solvent from a mixture of solvent and of hydrocarbons, in which a stepwise evaporation of the solvent is carried out according to an order of decreasing pressures to separate it from the hydrocarbons, characterized in that the staged evaporation of the solvent is carried out in a substantially isothermal manner at a temperature between 100 and 200 ° C, and a heat exchange is carried out between the evaporated solvent and at least one intermediate fluid to obtain the condensation of the solvent and recover its heat of condensation, and said intermediate fluid, in the gas phase, is compressed to raise its temperature and is then used to heat the mixture and carry out the staged evaporation of the solvent itself without any external heat supply to effect this operation is necessary.
  • isothermal evaporation of the solvent is coupled with a heat pump which recovers the calories of condensation of the solvent and raises them to a sufficient thermal level so that they can be used for the clean solvent spray.
  • isothermal evaporation has high level energy saving advantages, which makes it possible to cover the calorie needs of this type with heat due to the irreversibility of the compression in the heat pump. .
  • the invention also relates to an installation for implementing the above process and of the type comprising at least two evaporation flasks or the like successively supplied by a charge consisting of a mixture to be separated, of solvent and of hydrocarbons, characterized in that it comprises at least one steam generator ensuring the condensation of the solvent, at least one circuit for transporting the evaporated solvent connecting the flasks to said generator, and at least one intermediate fluid circuit in the gaseous phase provided with at least one compressor and connecting said generator to at least one exchanger disposed upstream of each tank.
  • an installation according to the invention comprises three successive solvent evaporation flasks and is characterized in that the streams of vaporized solvent leaving the second and third flasks are combined before arriving at a first generator of steam, while the flow of vaporized solvent leaving the first flask reaches a second steam generator, the condensed solvent flows leaving the two aforementioned generators being combined.
  • the flow of intermediate fluid in the gaseous phase produced by the two aforementioned generators feeds an exchanger upstream of the third balloon then divides to pass through two exchangers upstream of the first and second balloons respectively, and forms again a single flow passing through a heat exchanger for the charge introduced into the installation.
  • the installation shown in the single figure is, for example, the solvent recovery section in dewaxed oil, of a dewaxing unit for lubricants.
  • the solvent used can be a mixture (50% - 50% by volume) of methyl ethyl ketone and toluene.
  • the charge constituted by a solvent-oil mixture reaches the installation for example at a pressure of 500 kPa absolute and at a temperature of 39 ° C by a pipe to constitute flow 1.
  • the charge is divided into two flows marked respectively in 2 and 3, and it is preheated in an exchange train comprising, in parallel, the exchangers E 1 , E 2 and E 3 then the exchanger E4.
  • the stream 4 is heated by a stream of water vapor 111 to constitute the stream 6.
  • the stream 3 is heated by the dewaxed oil 23 going to storage via the pipe 24, and the stream 3 becomes the stream 5 which is joined to the stream 6 so as to form a single stream 7 reaching the 'exchanger E4.
  • the flow 7 is heated, up to the conditions of the evaporator flask or of flash B 1 , by condensed water vapor 109.
  • the evaporator flask B 1 operates at a temperature of 148.5 ° C and at a pressure of 400 kPa absolute and makes it possible to vaporize approximately 40% of the solvent contained in the charge passing through line 8.
  • the mixed phase constituting the flow 10a after the valve V, and terminating in the evaporator flask B 2 is heated in heat exchangers E5 and E 6 to the aforementioned temperature of the evaporator flask B 2 .
  • the flow 10a is heated by the flow 9 of the vaporized solvent leaving the flask B 1 , and this heated flow 10a constitutes the flow 11 which is in turn heated by the exchanger E 6 thanks to the steam of condensed water passing through line 107.
  • the flash in the evaporator flask 8 2 occurs, as said above, at a lower pressure than that of the flash in the flask B t , which makes it possible to eliminate practically all the remaining solvent which leaves the flask 8 2 via the pipe 13.
  • the liquid leaving the flask B 2 is pumped into the bottom of this flask, passes through the pipe 14 and is heated by two exchangers in parallel E 7 and E 8 to a temperature of about 200 ° C which is the appropriate temperature for stripping hydrocarbons in a column C.
  • the derivative flow 14a is heated by the dewaxed oil leaving the column C via the line 22.
  • the derivative flow 14b is heated by the passing steam in a line 105 and produced by a steam compressor M.
  • This balloon operates at a temperature of 200 ° C and at a pressure of 243 kPa absolute identical to that of balloon B 2 .
  • the liquid fraction 21 leaving the flask B 3 is then stripped from the column C by water vapor 98 in order to remove the last traces of the solvent in the stream 99.
  • the dewaxed oil 22 leaving column C is, as explained above, sent to storage via line 24 after cooling in the exchangers E 8 and E 3 .
  • the vaporized solvent leaves the flask B 3 via line 20, and this vaporized solvent flow is mixed in 20a with the solvent flow 13 leaving the flask B 2 to constitute the solvent flow 25 (pressure 243 kPa absolute, temperature 154 ° C. ).
  • the vapors of stream 25 are fully condensed and then sub-cooled after passing through a first exchanger or steam generator G, carrying out the condensation of the solvent, which is supplied with liquid water via a line 100.
  • the stream of solvent thus condensed forms the stream 26.
  • the flow of vaporized solvent 9 leaving the first evaporator flask B 1 is partially condensed in the exchanger E5 which arrives via line 27 at a second exchanger or steam generator G 2 , which provides total condensation and subcooling of the vapors solvent.
  • the condensed solvent forms the flow 28, at the same temperature conditions as the flow 26.
  • the flow 28 is then expanded in a valve (not shown), then mixed with the flow 26, as seen in 28a, to form the flow 29 mentioned above which is cooled in the exchanger And then sent to storage via a pipe 30.
  • the water vapor At the outlet of compressor M the water vapor is at around 220 ° C and 580 kPa absolute, and this water vapor passing through line 105 is used to supply high level calories to the exchanger E 7 upstream of the third ball B 3 .
  • the water vapor passes through the pipe 106 and divides to form the two pipes 107 and 109 passing respectively through the exchangers E 6 and E4 to heat the supplies to the tanks 8 2 and B, respectively.
  • the water vapor condensates then passing through the pipes 107a and 109a are mixed to form the stream 111 and are sub-cooled to 117 ° C and then expanded in a valve V 2 at a pressure of 180 kPa absolute, finally return to steam generators G, and G 2 via lines 100 and 102.
  • a process and an installation for recovering solvent have therefore been carried out according to the invention which have a much higher energy yield and which do not require external heat input, which heat supply serves in particular to compensate for the irreversibilities and the losses of the system.
  • the irreversibilities are minimized and the thermal degradation is reduced.
  • the heat between the process fluids and the heat pump fluid is transferred with minimal temperature degradation, which allows the system to work under optimal energy conditions. It will also be added that the solvent is not heated to high temperatures during evaporation and will therefore undergo less thermal degradation.
  • the installation of the invention has remarkable operating stability by the fact that the heat recovered is mixed at the level of the heat pump and redistributed in parallel between the points of evaporation of the solvent, which allows d '' Adjust the heat to be supplied to each flash separately.
  • the evaporation of the solvent in the flasks B 1 and 8 2 is carried out in an order of decreasing pressures, so as to allow the evaporation of a very large quantity of solvent while remaining at a substantially constant temperature and which can for example be between 100 and 200 ° C.
  • a substantially constant temperature which can for example be between 100 and 200 ° C.
  • the invention finally provides a process and an installation for recovering solvent which present exceptional results due to the fact that an isothermal evaporation scheme for the solvent is used coupled with a heat pump recovering the calories of condensation of the solvent and raising them at a sufficient thermal level so that they can be used to ensure the proper vaporization of the solvent.
  • the method according to the invention can perfectly be incorporated into old solvent recovery installations.

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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Gas Separation By Absorption (AREA)
EP87401232A 1986-06-05 1987-06-02 Procédé de séparation de solvant d'un mélange de solvant et d'hydrocarbures, et installation comportant application de ce procédé Expired EP0251838B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8608132 1986-06-05
FR8608132A FR2599750B1 (fr) 1986-06-05 1986-06-05 Procede de separation de solvant d'un melange de solvant et d'hydrocarbures, et installation comportant application de ce procede

Publications (2)

Publication Number Publication Date
EP0251838A1 EP0251838A1 (fr) 1988-01-07
EP0251838B1 true EP0251838B1 (fr) 1989-08-23

Family

ID=9336044

Family Applications (1)

Application Number Title Priority Date Filing Date
EP87401232A Expired EP0251838B1 (fr) 1986-06-05 1987-06-02 Procédé de séparation de solvant d'un mélange de solvant et d'hydrocarbures, et installation comportant application de ce procédé

Country Status (7)

Country Link
US (1) US4830711A (el)
EP (1) EP0251838B1 (el)
DD (1) DD265333A5 (el)
DE (1) DE3760476D1 (el)
ES (1) ES2010709B3 (el)
FR (1) FR2599750B1 (el)
GR (1) GR3000296T3 (el)

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2276089A (en) * 1937-06-26 1942-03-10 Union Oil Co Recovery of solvents from oils
FR1543961A (fr) * 1967-05-25 1968-10-31 Fives Lille Cail Installation pour la production d'eau douce à partir d'eau salée
FR1562830A (el) * 1967-11-15 1969-04-11
US3607668A (en) * 1968-11-12 1971-09-21 Amf Inc Concentrated brine-incoming feed vapor compression desalination system
US4181577A (en) * 1974-07-18 1980-01-01 Auscoteng Pty. Ltd. Refrigeration type water desalinisation units
DE2600398C2 (de) * 1976-01-07 1985-01-10 Jakob Dr.-Ing. 8000 München Hoiß Verfahren und Vorrichtung zur Rohwasser-Destillation
US4177137A (en) * 1977-11-07 1979-12-04 Standard Oil Company Aromatics extraction process
US4214975A (en) * 1978-05-10 1980-07-29 The Lummus Company Solvent recovery process for processing of hydrocarbons
FR2490103B1 (fr) * 1980-09-12 1986-02-28 Inst Francais Du Petrole Utilisation d'evaporateur a film tombant en multiple effet pour la recuperation d'un compose organique leger a partir d'un melange dudit compose avec un compose organique lourd
US4390418A (en) * 1982-05-12 1983-06-28 Texaco Inc. Recovery of solvent in hydrocarbon processing systems

Also Published As

Publication number Publication date
GR3000296T3 (en) 1991-06-07
DE3760476D1 (en) 1989-09-28
FR2599750A1 (fr) 1987-12-11
US4830711A (en) 1989-05-16
EP0251838A1 (fr) 1988-01-07
ES2010709B3 (es) 1989-12-01
FR2599750B1 (fr) 1988-10-07
DD265333A5 (de) 1989-03-01

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