EP0768363A1 - Procédé pour réduire la viscosité d'huiles résiduelles lourdes - Google Patents

Procédé pour réduire la viscosité d'huiles résiduelles lourdes

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Publication number
EP0768363A1
EP0768363A1 EP96202825A EP96202825A EP0768363A1 EP 0768363 A1 EP0768363 A1 EP 0768363A1 EP 96202825 A EP96202825 A EP 96202825A EP 96202825 A EP96202825 A EP 96202825A EP 0768363 A1 EP0768363 A1 EP 0768363A1
Authority
EP
European Patent Office
Prior art keywords
residue
thermal
visbreaking
heavy oil
heavy
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
EP96202825A
Other languages
German (de)
English (en)
Other versions
EP0768363B1 (fr
Inventor
Franco Lattarulo
Pierluigi Bozza
Giacomo Rispoli
Agostino Cavanna
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.)
Agip Petroli SpA
Original Assignee
Agip Petroli SpA
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 Agip Petroli SpA filed Critical Agip Petroli SpA
Priority to SI9630137T priority Critical patent/SI0768363T1/xx
Publication of EP0768363A1 publication Critical patent/EP0768363A1/fr
Application granted granted Critical
Publication of EP0768363B1 publication Critical patent/EP0768363B1/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
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
    • C10G51/023—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only only thermal cracking steps

Definitions

  • the present invention relates to a process for reducing the viscosity of heavy oil residues.
  • visbreaking processes are widely used, described for example in Beuther et al. "Thermal Visbreaking of Heavy Residues", The Oil and Gas Journal", 57:46, Nov.9, 1959, pages 151-175; or described in Rhoe et al. "Visbreaking: A Flexible Process", Hydrocarbon Processing, January 1979, pages 131-136.
  • the above processes can be applied to various refinery streams, such as atmospheric or vacuum residues, furfural-extracts, propane-deasphalted tars, catalytic cracking bottoms.
  • Visbreaking processes are thermal processes, carried out under comparatively mild conditions, which produce lighter hydrocarbon fractions. Visbreaking processes typically produce gases, l.p.g., naphtha and gas oil, heavy distillates.
  • Visbreaking processes are often accompanied by thermal cracking processes in which the heavy vacuum gas oil coming from visbreaking, is subjected to thermal cracking under more drastic conditions than the previous visbreaking step. In this way other lighter fractions are recovered.
  • the present invention relates to a process for reducing the viscosity of heavy oil residues, which comprises a first step for the visbreaking (I) of heavy oil residues and a second step for the thermal cracking (II) of the heavy gas oil formed during the visbreaking process, the above thermal cracking producing a thermal residue as well as lighter products, said process being characterized in that:
  • visbreaking means the process, well known in the prior art, for reducing the viscosity of heavy oil fractions.
  • the above visbreaking processes can be carried out, as is known, on the heavy oil residue without or in the presence of hydrogen (hydrovisbreaking), or in the presence of so-called hydrogen donor solvents (see for example US-A-2.953.513), or in the presence of hydrogen and donor solvent (see US-A-4.292.168) and also in the presence of catalysts (see for example US-A-5.057.204).
  • the visbreaking process (I) is carried out without hydrogen, catalysts and hydrogen donor solvents. It consists in feeding the heavy oil residue into an oven heated to the desired temperature for a preset time.
  • reaction temperature As in most oil processes, there is a correlation between reaction temperature and residence time of the reagents. One visbreaking process will therefore be more rigid than another if, at the same temperature, the residence time is greater.
  • the visbreaking process can usually be carried out with one or more ovens, but in any case the temperature of the visbreaking oven or ovens is between 350 and 525°C, preferably between 380 and 500°C, with a residence time of between 2 and 20 minutes, preferably between 3 and 10.
  • the heavy oil residues to be subjected to the visbreaking step (I) can come from various refinery streams.
  • the visbreaking process can therefore be applied to a variety of heavy oil fractions, such as vacuum residues, atmospheric residues, furfural-extracts, propane-deasphalted tars, catalytic cracking bottoms, asphalts.
  • heavy oil fractions such as vacuum residues, atmospheric residues, furfural-extracts, propane-deasphalted tars, catalytic cracking bottoms, asphalts.
  • at least 75% by weight of the components of the heavy oil residue has a boiling point which is higher than 370°C.
  • the above heavy oil residues can also contain impurities due to heteroatoms, for example nitrogen or sulphur, and metals, particularly Vanadium.
  • the heavy oil residue fed to the visbreaking step (I) basically consists of atmospheric residue.
  • Atmospheric residues usually have the following characteristics: density of between 0.940 and 1,000 g/cm 3 ; initial distillation point (according to ASTM D 1160 method), of between 180 and 220°C; temperature at which 5% in volume distills from 330 to 370°C; temperature at which 10% in volume distills from 380 to 410°C; temperature at which 50% in volume distills from 490 to 520°C.
  • the visbreaking step (I) produces numerous hydrocarbon fractions.
  • the following fractions are normally recovered: a) gases and l.p.g., b) naphtha, c) gas oil, d) heavy vacuum distillate, e) vacuum residue + fuel oil and/or tar.
  • the separation of the visbreaking products into the above fractions is irrelevant. It is preferably however to recover the fractions with a high additional value such as naphtha and gas oil.
  • HVGO high vacuum gas oil
  • This heavy vacuum gas oil is usually recovered, at least mostly, by distillation under vacuum, normally at about 20-40 mm Hg.
  • Heavy vacuum gas oil can be recovered as a column bottom from a distillation column at atmospheric pressure, or at pressures slightly higher than atmospheric pressure, usually at pressures of 2-4 bars.
  • the characteristics of this fraction i.e. column residue at atmospheric pressure
  • reference to heavy vacuum gas oil obtained downstream of the vis-breaking process (I) means both that which is recovered by distillation at reduced pressure, and that recovered as an atmospheric residue.
  • Part or all of the heavy vacuum gas oil thus separated is fed to the thermal cracking step (II).
  • the remaining part can be any other oil fraction having the same physico-chemical characteristics mentioned above for the heavy vacuum gas oil.
  • the vacuum residue of the topping is a typical fraction which can possibly be used in the feeding of the thermal cracking (II) together with the heavy vacuum gas oil recovered downstream of the visbreaking process.
  • thermal cracking step it is preferably however for the thermal cracking step to be fed with all the heavy vacuum gas oil fraction recovered after the visbreaking.
  • the thermal cracking oven has dimensions for operating with quantities of heavy vacuum gas oil which are smaller than the isolated quantities after the visbreaking step, it will be necessary to bleed part of the heavy vacuum gas oil or separate only the desired quantity.
  • the thermal cracking step (II) is carried out under more severe conditions than the visbreaking step (I), and therefore either at higher temperatures, with the same residence time, or with greater residence times, at the same temperature.
  • the temperature of the thermal cracking step (II) is usually between 450 and 510°C and the residence times are between 20 and 60 minutes.
  • thermal residue is recovered, which consists of what results from the thermal cracking after removing the light fractions (350°C-).
  • the stream leaving the thermal cracking is normally fed into a separator where the lighter fractions, those at 350°C-, are separated.
  • the remaining product consists of the thermal residue, which has a density at 15°C of between 1.00 and 1.07, a P value (determined by the Shell method Nr. 1600 of 1983) of between 1.4 and 2.3, an initial distillation point (according to the regulation ASTM D 1160), of between 180 and 220°C, the temperature at which 50% distills of between 440 and 490°C, the temperature at which 90% distills of between 570 and 610°C.
  • the thermal residue thus recovered is mixed with another heavy oil residue, the same or different from the initial charge, and the mixture thus obtained is refed to the visbreaking step (I).
  • the mixture of heavy oil residue and thermal residue preferably consists of 5-50% by weight, more preferably from 10 to 40% by weight, even more preferably from 20 to 30% by weight, of thermal residue, the complement to 100 consisting of the heavy oil fraction.
  • the process of the present invention allows almost all the thermal residue to be eliminated in a combined visbreaking + thermal cracking plant.
  • FIG 1 represents the process scheme of the present invention.
  • (A) represents the vis-breaking plant
  • (1) is the heavy oil residue
  • (2) is the light Vacuum Gas oil
  • (3) is the heavy Vacuum Gas oil
  • (4) is the Visbreaking Residue
  • (5) is the external heavy vacuum Gas oil
  • (6) is the residue recycled from the fractionation unit
  • (7) is the thermal Residue.
  • FIG 1 shows the Visbreaker plant (A), fed by the heavy oil residue (1).
  • a light stream is obtained, which is sent to an atmospheric distillation unit (D), and a heavy stream, which is sent to a distillation unit under vacuum (B).
  • a light vacuum gas oil fraction is obtained (2), which is fed to the atmospheric distillation unit (D), together with the heavy vacuum gas oil fraction (3), and a visbreaking residue, which will be used as a component for fuel oils.
  • the heavy vacuum gas oil fraction (3) forms the charge for the Thermal Cracker plant (C), together with the heavy gas oil obtained as residue (6) of the atmospheric fractionation unit (D), and together with possible charges of a similar composition, of a different origin.
  • a light fraction is obtained from the Thermal Cracker plant (C), which is fed to the atmospheric distillation unit (D), and a thermal residue, which is recycled to the Visbreaker plant.
  • Figure 2 shows, for comparative purposes, a conventional process of the prior art, in which, there is no recycling of the thermal residue at the end of the thermal cracking step.
  • the feeding to the Thermal Cracking (II) had the following characteristics:
  • the feeding to the Thermal Cracking consists (in both tests 1 and 2) of 60% of HVGO from the distillation unit under vacuum (B), 30% from the bottom of the atmospheric fractionation unit (D), and the remaining 10% of heavy gas oil ex vacuum pot of the topping, the latter fraction obviously coming from other parts of the refinery.
  • test 1 the thermal residue was mixed with other heavy oil residue, and the whole mixture was sent to the visbreaking step (I).
  • the above composition consisted of 25% of thermal residue and the remaining 75% of fresh heavy oil residue.
  • test 1 was carried out recycling almost all of the thermal residue leaving the thermal cracking step
  • comparative test 2 was carried out according to the scheme of figure 2, i.e. without recycling the thermal residue obtained leaving the thermal cracking step.

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)
  • Lubricants (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
EP96202825A 1995-10-13 1996-10-10 Procédé pour réduire la viscosité d'huiles résiduelles lourdes Expired - Lifetime EP0768363B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
SI9630137T SI0768363T1 (en) 1995-10-13 1996-10-10 Process for reducing the viscosity of heavy oil residues

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ITMI952099 1995-10-13
IT95MI002099A IT1276930B1 (it) 1995-10-13 1995-10-13 Procedimento per ridurre la viscosita' di residui petroliferi pesanti

Publications (2)

Publication Number Publication Date
EP0768363A1 true EP0768363A1 (fr) 1997-04-16
EP0768363B1 EP0768363B1 (fr) 1999-12-29

Family

ID=11372354

Family Applications (1)

Application Number Title Priority Date Filing Date
EP96202825A Expired - Lifetime EP0768363B1 (fr) 1995-10-13 1996-10-10 Procédé pour réduire la viscosité d'huiles résiduelles lourdes

Country Status (17)

Country Link
EP (1) EP0768363B1 (fr)
AT (1) ATE188237T1 (fr)
BG (1) BG62815B1 (fr)
CZ (1) CZ292215B6 (fr)
DE (1) DE69605881T2 (fr)
DK (1) DK0768363T3 (fr)
EA (1) EA000032B1 (fr)
ES (1) ES2142016T3 (fr)
GR (1) GR3032398T3 (fr)
HR (1) HRP960464B1 (fr)
HU (1) HU218833B (fr)
IT (1) IT1276930B1 (fr)
PL (1) PL182542B1 (fr)
PT (1) PT768363E (fr)
RO (1) RO119310B1 (fr)
SI (1) SI0768363T1 (fr)
SK (1) SK281664B6 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7718839B2 (en) 2006-03-29 2010-05-18 Shell Oil Company Process for producing lower olefins from heavy hydrocarbon feedstock utilizing two vapor/liquid separators
US7829752B2 (en) 2006-03-29 2010-11-09 Shell Oil Company Process for producing lower olefins
WO2011068612A1 (fr) 2009-12-03 2011-06-09 General Electric Company Application d'outils d'analyse de viscoréducteur pour optimiser la performance

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7394545B2 (en) 2005-07-11 2008-07-01 Ge Betz, Inc. Apparatus for characterizing and measuring the concentration of opaque particles within a fluid sample
US20160115404A1 (en) * 2014-10-28 2016-04-28 Uop Llc Process for converting a vacuum tower bottoms stream

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3504941A1 (de) * 1985-02-13 1986-08-14 Linde Ag, 6200 Wiesbaden Verfahren zur spaltung eines kohlenwasserstoffeinsatzes
US4663021A (en) * 1985-01-16 1987-05-05 Fuji Standard Research, Inc. Process of producing carbonaceous pitch
EP0249052A2 (fr) * 1986-06-10 1987-12-16 Petrolchemie und Kraftstoffe Aktiengesellschaft Schwedt Procédé pour produire des produits légers et des carburants pour des applications conventionnelles à partir de résidus d'huile brute contenant des métaux lourds et du soufre
US4836909A (en) * 1985-11-25 1989-06-06 Research Association For Residual Oil Processing Process of thermally cracking heavy petroleum oil

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2054637B (en) * 1979-07-27 1983-04-07 Uop Inc Visbreaking process
SU1033532A1 (ru) * 1981-06-29 1983-08-07 Горьковский Государственный Институт По Проектированию Предприятий Нефтеперерабатывающей И Нефтехимической Промышленности Способ получени котельного топлива
US4508614A (en) * 1982-11-08 1985-04-02 Mobil Oil Corporation Visbreaker performance for production of heating oil
US4504377A (en) * 1983-12-09 1985-03-12 Mobil Oil Corporation Production of stable low viscosity heating oil

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4663021A (en) * 1985-01-16 1987-05-05 Fuji Standard Research, Inc. Process of producing carbonaceous pitch
DE3504941A1 (de) * 1985-02-13 1986-08-14 Linde Ag, 6200 Wiesbaden Verfahren zur spaltung eines kohlenwasserstoffeinsatzes
US4836909A (en) * 1985-11-25 1989-06-06 Research Association For Residual Oil Processing Process of thermally cracking heavy petroleum oil
EP0249052A2 (fr) * 1986-06-10 1987-12-16 Petrolchemie und Kraftstoffe Aktiengesellschaft Schwedt Procédé pour produire des produits légers et des carburants pour des applications conventionnelles à partir de résidus d'huile brute contenant des métaux lourds et du soufre

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
MAZEL: "LES PROCEDES DE CONVERSION (1ère PARTIE)", REVUE DE L'ASSOCIATION FRANCAISE DES TECHNICIENS DU PETROLE, no. 240, November 1976 (1976-11-01), PARIS, pages 27 - 31, XP002019993 *

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7718839B2 (en) 2006-03-29 2010-05-18 Shell Oil Company Process for producing lower olefins from heavy hydrocarbon feedstock utilizing two vapor/liquid separators
US7829752B2 (en) 2006-03-29 2010-11-09 Shell Oil Company Process for producing lower olefins
WO2011068612A1 (fr) 2009-12-03 2011-06-09 General Electric Company Application d'outils d'analyse de viscoréducteur pour optimiser la performance

Also Published As

Publication number Publication date
EP0768363B1 (fr) 1999-12-29
ATE188237T1 (de) 2000-01-15
CZ296396A3 (en) 1997-06-11
DE69605881D1 (de) 2000-02-03
DK0768363T3 (da) 2000-04-17
HUP9602821A2 (en) 1997-05-28
HRP960464A2 (en) 1998-06-30
ES2142016T3 (es) 2000-04-01
ITMI952099A1 (it) 1997-04-13
RO119310B1 (ro) 2004-07-30
DE69605881T2 (de) 2000-06-15
SK130396A3 (en) 1997-07-09
BG62815B1 (bg) 2000-08-31
HUP9602821A3 (en) 1997-09-29
HRP960464B1 (en) 2000-12-31
BG100905A (en) 1997-07-31
PT768363E (pt) 2000-04-28
HU218833B (hu) 2000-12-28
IT1276930B1 (it) 1997-11-03
HU9602821D0 (en) 1996-11-28
SI0768363T1 (en) 2000-04-30
SK281664B6 (sk) 2001-06-11
EA199600082A1 (ru) 1997-06-30
EA000032B1 (ru) 1998-02-26
ITMI952099A0 (fr) 1995-10-13
GR3032398T3 (en) 2000-05-31
CZ292215B6 (cs) 2003-08-13
PL182542B1 (pl) 2002-01-31
PL316489A1 (en) 1997-04-14

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