EP0064447B1 - Procédé d'obtention d'un pétrole brut synthétique - Google Patents
Procédé d'obtention d'un pétrole brut synthétique Download PDFInfo
- 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
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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
- 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)
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 (fr) | 1982-11-10 |
EP0064447B1 true EP0064447B1 (fr) | 1986-02-05 |
Family
ID=9257914
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP82400729A Expired EP0064447B1 (fr) | 1981-04-29 | 1982-04-23 | Procédé d'obtention d'un pétrole brut synthétique |
Country Status (7)
Country | Link |
---|---|
EP (1) | EP0064447B1 (ja) |
JP (1) | JPS57185385A (ja) |
CA (1) | CA1178231A (ja) |
DE (2) | DE64447T1 (ja) |
FR (1) | FR2504936B1 (ja) |
MX (1) | MX159610A (ja) |
OA (1) | OA07085A (ja) |
Families Citing this family (6)
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 |
EP0264447B1 (en) * | 1986-05-02 | 1993-07-28 | URAKAMI, Hideaki | Bath for warming hands and feet |
EP1199347B1 (en) * | 1999-05-17 | 2004-12-15 | Chiyoda Corporation | Process for treating crude oil |
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)
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 |
-
1981
- 1981-04-29 FR FR8108563A patent/FR2504936B1/fr not_active Expired
-
1982
- 1982-04-07 MX MX192218A patent/MX159610A/es unknown
- 1982-04-19 CA CA000401228A patent/CA1178231A/en not_active Expired
- 1982-04-23 DE DE198282400729T patent/DE64447T1/de active Pending
- 1982-04-23 DE DE8282400729T patent/DE3268927D1/de not_active Expired
- 1982-04-23 EP EP82400729A patent/EP0064447B1/fr not_active Expired
- 1982-04-28 JP JP57072509A patent/JPS57185385A/ja active Pending
- 1982-04-29 OA OA57671A patent/OA07085A/xx unknown
Also Published As
Publication number | Publication date |
---|---|
DE3268927D1 (en) | 1986-03-20 |
MX159610A (es) | 1989-07-18 |
DE64447T1 (de) | 1983-04-28 |
FR2504936A1 (fr) | 1982-11-05 |
FR2504936B1 (fr) | 1985-08-09 |
EP0064447A1 (fr) | 1982-11-10 |
JPS57185385A (en) | 1982-11-15 |
CA1178231A (en) | 1984-11-20 |
OA07085A (fr) | 1984-01-31 |
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