EP0064447B1 - Verfahren zur Herstellung von synthetischem Rohöl - Google Patents

Verfahren zur Herstellung von synthetischem Rohöl Download PDF

Info

Publication number
EP0064447B1
EP0064447B1 EP82400729A EP82400729A EP0064447B1 EP 0064447 B1 EP0064447 B1 EP 0064447B1 EP 82400729 A EP82400729 A EP 82400729A EP 82400729 A EP82400729 A EP 82400729A EP 0064447 B1 EP0064447 B1 EP 0064447B1
Authority
EP
European Patent Office
Prior art keywords
hydrocarbons
line
mixture
crude oil
charge
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
EP82400729A
Other languages
English (en)
French (fr)
Other versions
EP0064447A1 (de
Inventor
Jacques Devanneaux
Charles Yacono
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.)
Compagnie Francaise de Raffinage SA
Original Assignee
Compagnie Francaise de Raffinage 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 Compagnie Francaise de Raffinage SA filed Critical Compagnie Francaise de Raffinage SA
Publication of EP0064447A1 publication Critical patent/EP0064447A1/de
Application granted granted Critical
Publication of EP0064447B1 publication Critical patent/EP0064447B1/de
Expired legal-status Critical Current

Links

Images

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
    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
    • C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
    • C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step

Definitions

  • the present invention relates to a process for obtaining a liquid product hereinafter called 'synthetic crude oil' from a hydrocarbon product having a higher density.
  • hydrocarbon product a product composed essentially of hydrocarbons, but which may also contain other chemical compounds which, in addition to carbon and hydrogen atoms, may have heteroatoms, such as oxygen, nitrogen, sulfur or metals like vanadium and nickel.
  • the term 'synthetic crude oil' used above is a commonly used term, but does not mean that synthetic crude oil comes from crude oil proper.
  • This product can also come, for example, from heavy oils having a density at 15 ° C. greater than about 0.93 g / mi, bituminous shales, oil sands or even coal.
  • the heaviest part of crude oil which is the residue from petroleum distillation, is made up of a mixture of oil and bituminous compounds.
  • US-A-2,847,353 has already described a process for treating an asphaltic oil, for the preparation of a feed for a catalytic cracking unit.
  • the oil a distillation residue of a crude oil, having a boiling point higher than 650 ° (345 ° C), is subjected to visbreaking under mild conditions: 800 to 1000 ° (427 - 539 ° C), 50 to 800 psig (3.5 - 56 bar).
  • the effluent leaving the visbreaker is fractionated in two stages, first under atmospheric pressure, the residue from this first fractionation then being fractionated under reduced pressure.
  • the residue from this second fractionation is deasphalted.
  • the deasphalted oil, refined to furfural serves as a feedstock for catalytic cracking with the fraction having a boiling point at most equal to 500 ° F (260 ° C) separated in the first fractionation.
  • the Applicant has devised a means of obtaining synthetic crude oil by a process integrating a heat treatment step and a deasphalting step.
  • the object of the present invention is therefore to obtain synthetic crude oil with a lower density from heavier products.
  • the charge Prior to any treatment, the charge may - and even must, in the case where this charge is in particular crude oil - have been treated in a desalter 2, into which it is introduced, via line 1, in order to remove the salts it contains.
  • the aqueous phase is eliminated by line 7 and the hydrocarbon feed to be treated by line 8 is recovered by the process according to the invention.
  • This fraction can be used to constitute part of the synthetic crude oil and will be taken by line 16 to a tank 17, from which the synthetic crude oil will be collected by line 36.
  • the petrol fraction is collected in liquid form, via line 47. This fraction is recycled at least in part to tower 12 by line 20. It can also be used, at least in part, to constitute the diluent introduced by line 8 into the feed, in the case of heavy products. It is led in this case to line 6 by line 21. It can finally also be led, by line 48, to tank 17 and constitute a part of the synthetic crude.
  • the fraction collected by line 19 is conducted in a fractionation tower 22, the function of which will be explained more loip.
  • the effluent from line 23 is led into a first separator tank 24.
  • the operating conditions for operating this balloon are chosen so as to collect via line 25 an overhead fraction containing at least hydrogen sulfide and most of the hydrocarbons containing from 1 to 4 or 5 carbon atoms, as the case may be, so that the bottom fraction, collected by line 26 and which will be conducted in a liquid extractor - deasphalting liquid 27, contains as little as possible of these gases.
  • the head fraction is led by line 25 in a second separator balloon 30.
  • the oily part is extracted from the feed brought by line 26 by a solvent which is introduced into the extractor by line 33.
  • This solvent can be chosen from the group consisting of saturated or unsaturated aliphatic hydrocarbons saturated, having from 2 to 8 carbon atoms, preferably from 3 to 5 carbon atoms, mixtures of hydrocarbons, called distillates, obtained by distillation of crude oil and having molecular weights close to those of hydrocarbons having from 2 to 8 carbon atoms and the mixtures of all the previously mentioned hydrocarbons.
  • the solvent for starting the unit comes from a source outside the unit, via line 34.
  • the solvent losses can be compensated either by products coming from the unit, as will be explained more away, either by an external backup brought by line 34.
  • the pressure inside the extractor 27 can be between 1 and 100 bar absolute, the temperature between 15 and 300 ° C., the mass content of the solvent being com p r i e charge between 0.1 and 10.
  • the oily part in solution in the solvent is collected at the head of the extractor 27, via line 38.
  • This mixture is conducted by line 38 in a fractionation assembly 39.
  • this assembly has not been shown in detail, but it generally comprises a regulator controlling a pressure drop, evaporators and a steam column.
  • the precipitated bituminous part and the solvent are recovered at the bottom of the extractor 27 and this mixture is conducted, via line 42, in a fractionation assembly 43, which generally comprises an oven and an evaporator.
  • the heaviest fraction collected at the bottom of column 22 by line 46 and consisting of hydrocarbons having at least 3 carbon atoms, can be taken to tank 17, as shown in FIG. 1.
  • deasphalting solvent can also come from the fraction collected by line 48, or, as it was said previously, from line 35.
  • the bituminous part of line 44 can be conducted in a coking unit.
  • This coking unit can be of various natures, but, in the case of an installation implementing the method according to the invention and located on the field of production of the charge, it is more advantageous that this unit provides little coke and that it can be easily used as fuel. This is the case for coking units in a fluidized bed, where the coke produced can be easily handled or even gasified.
  • This coking unit makes it possible to produce coke and an effluent, which, after separation of the hydrogen sulfide and the hydrocarbons with 1 and 4 carbon atoms which it contains, can give a product containing hydrocarbons with 5 and more than 5 atoms of carbon, which may constitute part of the synthetic crude.
  • the synthetic crude oil obtained in tank 17, which therefore comes from line 41 and, optionally, lines 37, 16, 48 and 46, has a lower density than the starting product and contains fewer troublesome products such as sulfur, and especially much less metals like nickel and vanadium, which is very interesting for the subsequent treatment of crude oil.
  • FIG. 2 in which the elements identical to those represented in FIG. 1 have been identified by the same numbers assigned to the index '.
  • the start of the treatment is the same, but it changes in the treatment of the effluent collected by the line 23 ', at the outlet of the heat treatment enclosure 10'.
  • the flow of line 23 ′ is conducted in a fractionation tower 100.
  • a gasoline fraction is collected at the bottom of the tank 107, via the line 109, which is recycled, at least in part, to the tower 100 by the line 110. It can also be conducted, at least in part, by a non-line shown, for the sake of simplification, ü line 6 ′, to serve as a diluent for the load, in the case of heavy products. Finally, it can also be taken, by line 111, to tank 104, to constitute part of the synthetic crude.
  • the solvent is collected, on the one hand, by line 115, which is recycled to column 106, via line 112, on the other hand, by line 116 , the oily part, which is led into the tank 104.
  • the precipitated bituminous part and the solvent are recovered at the bottom of the extractor 106 and this mixture is led, via line 117, directly into a fractionation assembly 118.
  • a make-up of solvent can be introduced via line 121 into extractor 106, via line 112. This make-up can come, as the case may be, from the streams of lines 46 ', 48' and 111.
  • a coking unit can be provided to treat the bituminous part collected by line 120.
  • This example relates to the treatment, by the method according to the invention, of a crude oil obtained from a deposit by extraction with steam.
  • the product thus obtained contains approximately 25% by weight of water, which is eliminated.
  • a hydrocarbon product is thus obtained, the characteristics of which are shown in Table 1 below.
  • the charge is first fractionated in a column at atmospheric pressure.
  • a fraction 1 is collected, the boiling point range of which is between 150 and 350 ° C., and a fraction 2, boiling above 350 ° C.
  • Fraction 2 was then treated thermally, at a temperature of 420 ° C.
  • Table IV below gives the operating conditions for deasphalting used to obtain an oil yield close to 70% by weight and the main characteristics of the oils obtained for fraction 2 not heat treated, as well as for products A and B obtained after heat treatment of fraction 2.
  • the synthetic crude oils obtained by the process according to the invention have a lower density and nickel, vanadium and sulfur contents than the starting crude oil. Their Conradson residue is also much lower.
  • the nickel and vanadium contents and the Conradson residue decrease markedly with an increase in the duration of the heat treatment to 420 ° C.
  • the process according to the invention therefore makes it possible to obtain, under the same operating conditions, a better yield of oil and of lower density.
  • the synthetic crude oils obtained by the process according to the invention have a lower density and lower nickel and vanadium contents than the starting crude oil.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (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)

Claims (4)

1. Verfahren zur Herstellung von synthetischem Rohöl aus einer Kohlenwasserstoffcharge mit einer größeren spezifischen Masse,gekennzeichnet durch die folßenden Schritte:
a) gegebenenfalls Fraktionieren (in 12) der Kohlenwasserstoffcharge in wenigstens zwei Fraktionen:
wenigstens eine leichte Fraktion, welche den größten Teil der Verbindungen mit den niedrigsten Siedepunkten enthält,
eine schwere Fraktion, welche den größten Teil der Verbindungen mit den höchsten Siedepunkten enthält, b) thermisches Behandeln (in 10, 10')
der Kohlenwasserstoffcharge, falls das Fraktionieren gemäß Schritt a) nicht durchgeführt wird, oder
der schweren Fraktion, falls das Fraktionieren der Charge stattfindet,
wobei die thermische Behandlung zur Gewinnung eines Ausflusses führt, weicher in einern einzigen Schritt (in 100) fraktioniert wird, um
1.) ein erstes Gemisch, welches Wasserstoff, Schwefelwasserstoff und Kohlenwasserstoffe enthält,
2.) ein zweites Gemisch, welches aus Kohlenwasserstoffen mit höheren Molekulargewichten als die jenigen im ersten Gemisch besteht,
3.) ein drittes Gemisch von Kohlenwasserstoffen, deren Siedepunkte zwischen den Kohlenwasserstoffen des ersten Gemisches und denen des zweiten Gemisches liegen, wobei das dritte Gemisch wenigstens teilweise das synthetische Rohöl darstellt,
zu erhalten,
c) Behandeln des beim Schritt b) erhaltenen zweiten Gemisches mit einem Lösungsmittel (in 27, 106), wobei diese Behandlung zur Gewinnung
einerseits eines biturninösen Teils,
andererseits eines öligen Teils, welcher wenigstens teilweise das synthetische Rohöl darstellt, führt.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Kohlenwasserstoffcharge einem Entsalzungsvorgang (in 2, 2') unterworfen wird, und daß der Charge vor dieser Entsalzung wenigstens ein Teil der Kohlenwasserstoffe zugegeben wird, welche in der bei dem eventuellen Fraktionieren gem äß Schritt a) erhaltenen leichten Fraktion enthalten sind.
3. Verfahren nach einem der Ansprüche 1 und 2, dadurch gekennzeichnet, daß wenigstens ein Teil der Kohlenwasserstoffe, welche in der bei dem eventuellen Fraktionieren.(in 12, 12') gemäß Schritt a) erhaltenen leichten Fraktion enthalten sind, wenigstens teilweise das synthetische Rohöl darstellt.
4. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß der bituminöse Teil einern Verkoken unterworfen wird, und daß wenigstens ein Teil des Ausflusses der Verkokung einen Teil des synthetischen Rohöls darstellt.
EP82400729A 1981-04-29 1982-04-23 Verfahren zur Herstellung von synthetischem Rohöl Expired EP0064447B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8108563 1981-04-29
FR8108563A FR2504936B1 (fr) 1981-04-29 1981-04-29 Procede d'obtention d'un petrole brut synthetique

Publications (2)

Publication Number Publication Date
EP0064447A1 EP0064447A1 (de) 1982-11-10
EP0064447B1 true EP0064447B1 (de) 1986-02-05

Family

ID=9257914

Family Applications (1)

Application Number Title Priority Date Filing Date
EP82400729A Expired EP0064447B1 (de) 1981-04-29 1982-04-23 Verfahren zur Herstellung von synthetischem Rohöl

Country Status (7)

Country Link
EP (1) EP0064447B1 (de)
JP (1) JPS57185385A (de)
CA (1) CA1178231A (de)
DE (2) DE3268927D1 (de)
FR (1) FR2504936B1 (de)
MX (1) MX159610A (de)
OA (1) OA07085A (de)

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2566795A1 (fr) * 1984-07-02 1986-01-03 Raffinage Cie Francaise Procede de conversion d'une charge hydrocarbonee lourde
US4880415A (en) * 1986-05-02 1989-11-14 Hideaki Urakami Warm bath for hands and feet
JP4564176B2 (ja) * 1999-05-17 2010-10-20 千代田化工建設株式会社 原油の処理方法
DE19954141A1 (de) 1999-11-11 2001-06-13 Phenolchemie Gmbh & Co Kg Verfahren zur Verringerung des Salzgehaltes in Hochsieder aufweisenden Fraktionen, die bei der Herstellung von Phenol aus Cumol anfallen, durch Extraktion
US6524469B1 (en) * 2000-05-16 2003-02-25 Trans Ionics Corporation Heavy oil upgrading process
CN1325605C (zh) * 2005-12-07 2007-07-11 中国海洋石油总公司 一种油砂沥青的处理方法

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2790754A (en) * 1954-11-05 1957-04-30 Shell Dev Production of lubricating oil
US2847353A (en) * 1955-12-30 1958-08-12 Texas Co Treatment of residual asphaltic oils with light hydrocarbons
US2943048A (en) * 1958-12-02 1960-06-28 Exxon Research Engineering Co Removal of metallic contaminants from petroleum fractions
US3453206A (en) * 1966-06-24 1969-07-01 Universal Oil Prod Co Multiple-stage hydrorefining of petroleum crude oil
DE2805721A1 (de) * 1978-02-10 1979-08-16 Linde Ag Verfahren zur aufbereitung eines kohlenwasserstoffgemisches
US4201658A (en) * 1978-03-29 1980-05-06 Chevron Research Company Pour point depressant made from the asphaltene component of thermally treated shale oil

Also Published As

Publication number Publication date
EP0064447A1 (de) 1982-11-10
FR2504936A1 (fr) 1982-11-05
CA1178231A (en) 1984-11-20
OA07085A (fr) 1984-01-31
MX159610A (es) 1989-07-18
FR2504936B1 (fr) 1985-08-09
DE64447T1 (de) 1983-04-28
DE3268927D1 (en) 1986-03-20
JPS57185385A (en) 1982-11-15

Similar Documents

Publication Publication Date Title
EP0246956B1 (de) Verfahren zur Entfernung von Asphalt aus einer Kohlenwasserstoffbeschickung
CA2550443C (fr) Enchainement integre de procedes d'extraction et de traitement d'un brut extra lourd ou bitumeux
EP0708174B1 (de) Verfahren und Anlage zur Reinigung von Altölen
EP0053535B1 (de) Verfahren zur Lösungsmitteldesasfaltierung von Rückstands-Kohlenwasserstoffölen
CA2615197A1 (fr) Procede de conversion de residus incluant 2 desasphaltages en serie
EP0621334A1 (de) Verfahren zur Herstellung von Brennstoff-durch Extraktion und Wasserstoffbehandlung von Kohlenwasserstoff Einsätz und so hergestellte Gasöl
CA2346181A1 (en) Deep conversion combining the demetallization and the conversion of crudes, residues or heavy oils into light liquids with pure or impure oxygenated compounds
EP0201364B1 (de) Verfahren zur Entasphaltierung von Asphalt enthaltenden Kohlenwasserstoffeinsätzen
EP0222631B1 (de) Verfahren zur Entasphaltierung mit Energierückgewinnung bei der Trennung von deasphaltiertem Öl von Entasphaltierungslösungsmittel
EP0064447B1 (de) Verfahren zur Herstellung von synthetischem Rohöl
CA1191805A (fr) Procede de conversion d'huiles lourdes ou de residus petroliers en hydrocarbures gazeux et distillables
EP0256940A1 (de) Verfahren zur Entasphaltierung eines Schwerkohlenwasserstoffeinsatzes
EP0819752B1 (de) Verfahren und Einrichtung zur Umwandlung einer Kohlenwasserstoffbeschickung mit zwei Wasserstoffbehandlungsreaktoren und einer einzigen Fraktionierungsanlage
US5346615A (en) Process for deasphalting and demetalating crude petroleum or its fractions
CA2815618A1 (fr) Procede de conversion de charge hydrocarbonee comprenant une huile de schiste par hydroconversion en lit bouillonnant, fractionnement par distillation atmospherique et extraction liquide/liquide de la fraction lourde
BE1019627A3 (fr) Procede de valorisation de bruts lourds et de residus petroliers.
JPS6249917B2 (de)
FR2770225A1 (fr) Procede et dispositif de vaporisation selective des charges d'hydrocarbures en craquage catalytique
FR2542005A1 (fr) Procede de traitement de petrole et de residus de petrole pour produire des produits plus hydrogenes
FR2503734A1 (fr) Procede d'obtention d'un petrole brut synthetique
EP0329510B1 (de) Verfahren zur Entasphaltierung schwerer Erdölfraktionen und dessen Verwendung
FR2566795A1 (fr) Procede de conversion d'une charge hydrocarbonee lourde
US2952613A (en) Processing petroleum oils
BE559418A (de)
FR2621322A1 (fr) Procede de vaporisation d'une charge liquide dans un procede de craquage catalytique en lit fluide

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Designated state(s): BE DE GB IT NL

ITCL It: translation for ep claims filed

Representative=s name: BARZANO' E ZANARDO MILANO S.P.A.

TCNL Nl: translation of patent claims filed
17P Request for examination filed

Effective date: 19821129

DET De: translation of patent claims
GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Designated state(s): BE DE GB IT NL

ITF It: translation for a ep patent filed

Owner name: BARZANO' E ZANARDO MILANO S.P.A.

REF Corresponds to:

Ref document number: 3268927

Country of ref document: DE

Date of ref document: 19860320

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 19870430

Year of fee payment: 6

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Effective date: 19890423

ITTA It: last paid annual fee
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Effective date: 19890430

BERE Be: lapsed

Owner name: CIE FRANCAISE DE RAFFINAGE

Effective date: 19890430

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Effective date: 19891101

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee
GBPC Gb: european patent ceased through non-payment of renewal fee
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Effective date: 19900103