EP0142043A2 - Procédé de récupération d'huiles vaporisables à partir du résidu d'hydrogénation d'huiles lourdes, de bitume ou goudron, etc. - Google Patents

Procédé de récupération d'huiles vaporisables à partir du résidu d'hydrogénation d'huiles lourdes, de bitume ou goudron, etc. Download PDF

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Publication number
EP0142043A2
EP0142043A2 EP84112309A EP84112309A EP0142043A2 EP 0142043 A2 EP0142043 A2 EP 0142043A2 EP 84112309 A EP84112309 A EP 84112309A EP 84112309 A EP84112309 A EP 84112309A EP 0142043 A2 EP0142043 A2 EP 0142043A2
Authority
EP
European Patent Office
Prior art keywords
hydrogenation
screw machine
distillation
oils
residue
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
EP84112309A
Other languages
German (de)
English (en)
Other versions
EP0142043B1 (fr
EP0142043A3 (en
Inventor
Lothar Winckler
Klaus Dr. Dipl.-Chem. Fuhrmann
Ulrich Dr. Dipl.-Ing. Graeser
Peter Dipl.-Ing. Wenning
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.)
Veba Oel Technologie und Automatisierung GmbH
Original Assignee
Veba Oel Technologie und Automatisierung GmbH
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 Veba Oel Technologie und Automatisierung GmbH filed Critical Veba Oel Technologie und Automatisierung GmbH
Priority to AT84112309T priority Critical patent/ATE71133T1/de
Publication of EP0142043A2 publication Critical patent/EP0142043A2/fr
Publication of EP0142043A3 publication Critical patent/EP0142043A3/de
Application granted granted Critical
Publication of EP0142043B1 publication Critical patent/EP0142043B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation

Definitions

  • the object of the present invention is to overcome these difficulties. According to the invention, this is done by subjecting the residue to the hydrogenation of heavy or heavy oils, bitumen, tar, shale oils and the like in a single- or multi-shaft screw machine distillation under reduced pressure.
  • the hydrogenation residue which constantly increases its viscosity during the distillation, is continuously circulated by the screw and is thereby passed through the distillation zone of the screw machine, so that the evaporable constituents are removed from it.
  • the screw machine thus forms part of the polymerization reactor, the polymerization reaction being terminated by removing the monomers in the vacuum zone, whereas in the case of the hydrogenation of the aforementioned starting materials, the solidification in the hydrogenation residue is expedient.
  • pressures of 0.01-0.6 bar preferably 0.02-0.1 bar
  • the pressure drops from 0.6, preferably 0.1 bar to 0.01, preferably 0.02 bar over the length of the screw machine from the entry of the hydrogenation sludge to its exit. This measure reduces the risk of disturbances in the distillation process in the screw machine.
  • the distillation of the hydrogenation residue in the screw machine is carried out in particular at temperatures of 200-400 ° C., preferably 250-350 ° C.
  • the temperature increases from 200 ° C., preferably 250 ° C. to 400 ° C., preferably 350 ° C., over the length of the screw machine from the inlet to the outlet of the hydrogenation residue. This shortens the time during which the hydrogenation residue assumes high temperatures which favor changes and facilitates the further processing of the residue freed from the volatile constituents. Residues up to a final viscosity of approximately 2000 mPas (250 ° C.) can be handled in the distillate removal by the process according to the invention.
  • the gases withdrawn in gaseous form from the screw machine are expediently mixed with the other hydrogenating oils, e.g. B. combines the hot separator leaving gaseous hydrogenation products and together with these further treatment, for. B. subjected to a hydrogenation.
  • the non-evaporated material can be introduced from the screw machine into a cooling or granulating device, where it is solidified.
  • the goods that can be stored and transported in this form can e.g. B. can be used as fuel or as a feed of a gasification plant.
  • the unevaporated material is heated in the screw machine after distillation to higher temperatures, preferably 350-600 ° C., and is smelted at this temperature, in particular at atmospheric pressure or at a pressure below it.
  • the screw machine expediently has a smoldering zone in addition to the distillation zone, into which the hydrogenation residue is conveyed through the screws after passing through the former.
  • the sulfuric vapors generated are extracted separately from the oil vapors.
  • the resulting coke can finally z. B. can be used as fuel.
  • the screw machine expediently has a compression zone connected to a direct entry system into a gasification reactor.
  • the present method is suitable for processing all hydrogenation residues which occur in high-pressure hydrogenation processes of heavy or heavy oils, bitumen, tar, oils from oil shale or tar sand and the like, in which the starting material contains Hy Hydrogen hydrogen and optionally in the presence of a catalyst at elevated pressure and elevated temperature, for example by the so-called Bergius-Pier process.
  • the residue from the vacuum distillation of a Venezuelan crude oil with an initial boiling point of above 325 ° C was in a hydrogenation plant, which works essentially on the basis of an advanced Bergius-Pier process, at 300 bar and 450 ° C with the addition of an inorganic catalyst system and with the addition of Hydrogen is hydrogenated and fed via line 1 to a hot separator 2, in which the gaseous reaction products are separated from the liquid and solid components of the reaction mixture at reaction pressure and reaction temperature.
  • the gaseous constituents are drawn off via line 3 and processed further in the usual way.
  • the non-volatile solid and liquid constituents leave the hot separator via line 4 and are fed to the vacuum screw machine 7 after expansion to atmospheric pressure via nozzle 6.
  • a positive-displacement pump system 5 which also serves as a metering unit, is used as the conveying element for the feed stream.
  • the product used in the vacuum screw machine consists of 0.86 t of oil with a boiling range of 200 - 550 ° C at normal pressure, 0.12 t of residue with a start of boiling of at least 550 ° C at normal pressure and 0.02 t of inorganic constituents.
  • the vacuum screw machine 7 was equipped with a double screw and, in the case of the present example, was divided into an evaporation zone 8 and a smoldering zone 9 over the length of the screw cylinder.
  • the hydrogenation residue used is heated to 350 ° C. at 0.1 bar. 0.75 t of volatile constituents are drawn off via the connection piece 10 and passed into the condensate container 12 via line 11 following cooling which is not shown in the flow diagram.
  • the condensate container is connected to the vacuum line 13 and the condensate is drawn off via line 15.
  • the residue obtained from the evaporation zone 8 contained 0.13 t of oil constituents with a boiling range of about 450-500 ° C. under normal pressure, 0.10 t of a residue boiling above 550 ° C. under normal pressure and 0.02 t of inorganic constituents.
  • This residue was heated in the smoldering zone 9 adjoining the evaporation zone 8 from 350 ° C. over the length of the smoldering zone to gradually increase to 600 ° C., the evaporation zone 8 and smoldering zone 9 being separated by a mechanical compression stage 16, thereby compressing the residue he follows.
  • the vacuum screw machine was heated by means of jacket heating by means of superheated steam in the evaporation zone 8 and by means of flue gas in the smoldering zone 9.
  • the heating can also be carried out by means of electrically heated heating jaws or by induction heating or, in the case of jacket heating, by heat transfer oils.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Working-Up Tar And Pitch (AREA)
  • Lubricants (AREA)
EP84112309A 1983-10-15 1984-10-12 Procédé de récupération d'huiles vaporisables à partir du résidu d'hydrogénation d'huiles lourdes, de bitume ou goudron, etc. Expired - Lifetime EP0142043B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT84112309T ATE71133T1 (de) 1983-10-15 1984-10-12 Verfahren zur gewinnung von verdampfbaren oelen aus dem rueckstand der hydrierung von schweroelen, bitumen, teer und dergl.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19833337623 DE3337623A1 (de) 1983-10-15 1983-10-15 Verfahren zur gewinnung von verdampfbaren oelen aus dem rueckstand der hydrierung von schwer- oder schwerstoelen, bitumen, teer u.dgl.
DE3337623 1983-10-15

Publications (3)

Publication Number Publication Date
EP0142043A2 true EP0142043A2 (fr) 1985-05-22
EP0142043A3 EP0142043A3 (en) 1986-12-03
EP0142043B1 EP0142043B1 (fr) 1992-01-02

Family

ID=6211990

Family Applications (1)

Application Number Title Priority Date Filing Date
EP84112309A Expired - Lifetime EP0142043B1 (fr) 1983-10-15 1984-10-12 Procédé de récupération d'huiles vaporisables à partir du résidu d'hydrogénation d'huiles lourdes, de bitume ou goudron, etc.

Country Status (5)

Country Link
EP (1) EP0142043B1 (fr)
AT (1) ATE71133T1 (fr)
CA (1) CA1239105A (fr)
DD (1) DD226587A5 (fr)
DE (2) DE3337623A1 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3829986A1 (de) * 1988-09-03 1990-03-15 Enka Ag Verfahren zur erhoehung des mesophasenanteils in pech
CA2897875C (fr) * 2013-01-25 2015-12-08 Calaeris Energy & Environment Ltd. Procedes et systemes de separation thermique sous vide turbulent

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB188686A (en) * 1921-05-17 1922-11-17 Herman Plauson Improvements in the extraction of hydrocarbons from wood
GB288148A (en) * 1927-03-31 1929-06-28 Ig Farbenindustrie Ag Improvements in the production of low boiling point and other hydrocarbons and derivatives thereof by the destructive hydrogenation of coals, oils and the like and in the treatment of the residues thereof
US1942373A (en) * 1929-08-30 1934-01-02 Barrett Co Method of preparing creosoting compositions
DE619298C (de) * 1934-01-25 1935-09-27 Edwin M F Guignard Vorrichtung zum Verdampfen und Destillieren
DE704444C (de) * 1940-02-13 1941-03-31 Hydrierwerk Scholven Akt Ges Verfahren zum Aufarbeiten von oelhaltigen Schleuderrueckstaenden der Druckhydrierung aschehaltiger Brennstoffe
DE737780C (de) * 1940-09-01 1943-07-23 Dr Edwin M F Guignard Kessel zur fraktionierten Destillation von Fluessigkeiten
US2615199A (en) * 1945-05-15 1952-10-28 Welding Engineers Material treating apparatus
DE2327353A1 (de) * 1973-05-29 1975-01-02 Otto & Co Gmbh Dr C Verfahren zur umwandlung fester in fluessige und gasfoermige schwefelarme brennstoffe
DE2407217A1 (de) * 1974-02-15 1975-09-04 Kloeckner Humboldt Deutz Ag Verfahren und vorrichtung zur thermischen behandlung von koernigen feststoffen

Also Published As

Publication number Publication date
DE3485411D1 (de) 1992-02-20
DE3337623A1 (de) 1985-04-25
DD226587A5 (de) 1985-08-28
CA1239105A (fr) 1988-07-12
EP0142043B1 (fr) 1992-01-02
ATE71133T1 (de) 1992-01-15
EP0142043A3 (en) 1986-12-03

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