EP2260089A1 - Procédé de traitement de pétrole brut lourd - Google Patents

Procédé de traitement de pétrole brut lourd

Info

Publication number
EP2260089A1
EP2260089A1 EP09719531A EP09719531A EP2260089A1 EP 2260089 A1 EP2260089 A1 EP 2260089A1 EP 09719531 A EP09719531 A EP 09719531A EP 09719531 A EP09719531 A EP 09719531A EP 2260089 A1 EP2260089 A1 EP 2260089A1
Authority
EP
European Patent Office
Prior art keywords
hco
solvent
deasphalting
oil
solvent mixture
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.)
Withdrawn
Application number
EP09719531A
Other languages
German (de)
English (en)
Other versions
EP2260089A4 (fr
Inventor
James Hill
Claudio Arato
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.)
Petrosonic Energy Inc
Original Assignee
Sonic Technology Solutions Inc
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 Sonic Technology Solutions Inc filed Critical Sonic Technology Solutions Inc
Publication of EP2260089A1 publication Critical patent/EP2260089A1/fr
Publication of EP2260089A4 publication Critical patent/EP2260089A4/fr
Withdrawn legal-status Critical Current

Links

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
    • C10G21/003—Solvent de-asphalting
    • 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
    • C10G32/00—Refining of hydrocarbon oils by electric or magnetic means, by irradiation, or by using microorganisms
    • C10G32/02—Refining of hydrocarbon oils by electric or magnetic means, by irradiation, or by using microorganisms by electric or magnetic means

Definitions

  • the present invention relates to a method for deasphalting oils containing asphaltenes (such as heavy crude oil (HCO) , bitumen, and oil refinery residues) using solvents and acoustic sound energy resulting in an upgraded higher value synthetic crude oil which may be further upgraded by chemical or biological/chemical processes.
  • asphaltenes such as heavy crude oil (HCO) , bitumen, and oil refinery residues
  • solvents and acoustic sound energy resulting in an upgraded higher value synthetic crude oil which may be further upgraded by chemical or biological/chemical processes.
  • solvent deasphalting can be used to upgrade heavy crude oil (HCO) , including bitumen, to a synthetic crude oil (SCO) via enhancement of its chemical and physical properties such as:
  • API gravities above 19 and viscosities below 350 centistokes are particularly desirable for purposes of product pipelining .
  • Nickel contamination in oil refineries can come from two (2) sources: corrosion of stainless steel (e.g. via the presence of hydrogen chloride or naphthenic acids) or nickel organometallic compounds (e.g. porphyrins) in the asphaltene portion of bitumen.
  • Nickel a hydrogen scavenger, causes catalyst fouling via coke formation due to dehydrogenation of alkanes to olefins in refinery catalytic crackers. Therefore SCO containing less nickel is more valuable.
  • Vanadium contamination in oil refineries can come from vanadium organometallic compounds (e.g. porphyrins) in the asphaltene portion of bitumen. Vanadium destroys catalytic cracker catalysts by altering their crystal structure to non- catalytic forms. Therefore SCO containing less vanadium is more valuable.
  • vanadium organometallic compounds e.g. porphyrins
  • Canadian patent 2,549,358 (Boakye) describes a chemical and biological upgrading process for heavy oils which includes solvent deasphalting as a primary step. Although the process achieves high quality SCO output, the deasphalting step is prohibitively expensive and therefore not commercially viable due to excessive solvent requirements e.g. 10:1 preferred solvent to oil volume ratio (see page 5 section [0016]) and deasphalter processing times e.g. 2 to 3 hours (see page 2 section [0005] ) .
  • the process of deasphalting has two purposes: to initiate upgrading of the HCO, by an average quantity of 4-5 API, as per prior technical evaluation as well as to remove a substantial quantity of sulphur from the HCO to the precipitated, insoluble asphaltene fraction.
  • Deasphalting involves the solubilization of non-asphaltenes and the precipitation of asphaltenes, i.e. molecules insoluble in the deasphalting solvent.
  • Deasphalting was high for non-cyclic alkanes and improved as the molecular weight of the alkane was reduced. Deasphalting was efficient based on the low solvent : bitumen ratio, however, deasphalting was extremely slow (i.e. 8 hours) .
  • Prior art deasphalting of heavy crude oil and refinery residues suffers from the following problems alone or in combination:
  • the present invention is a method for converting heavy crude oil (HCO) , such as bitumen, or oil refinery residues to a higher grade synthetic crude oil (SCO) or refinery output via separation of the SCO from asphaltenes.
  • HCO heavy crude oil
  • SCO synthetic crude oil
  • Asphaltenes are defined as the part of the HCO or refinery residue precipitated by addition of a low-boiling paraffin solvent such as n-pentane.
  • the SCO can be used as is or further upgraded via chemical and/or biological processing e.g. Canadian patent 2,549,358.
  • a method for treating heavy crude oil which includes the steps of combining the HCO with an alkane containing non-polar solvent to form an HCO/solvent mixture, sonicating this mixture at audio frequency to precipitate asphaltenes from the HCO/solvent mixture, and separating the precipitated asphaltenes from the HCO/solvent mixture.
  • vacuum filtration is used to remove . precipitated asphaltenes from the HCO/solvent mixture.
  • Distillation may be used to remove solvent from the HCO/solvent mixture after removal of precipitated asphaltenes so as to create a deasphalted and solvent free synthetic crude oil (SCO) .
  • the alkane containing solvent may include pentane, hexane or iso-octane.
  • the deasphalted HCO/solvent mixture may advantageously be used as the feedstock for a chemical and/or biological oil upgrading process.
  • the chemical and/or biological .process uses enzyme sources and one or more oxidants in the presence of an acid.
  • the enzyme source may be soyabean husk and the enzyme, peroxidase .
  • the acid may be acetic acid.
  • the oxidant may be hydrogen peroxide combined with iron oxide .
  • the deasphalting time is preferably 2 minutes (120 seconds) or less.
  • the deasphalting time may be 60 seconds.
  • the deasphalting solvent: HCO weight ratio may be less than or equal to 3.5.
  • the deasphalting solvent: HCO weight ratio may be 1.16 or less .
  • the deasphalting solvent: HCO weight ratio may be 0.91.
  • the method exhibits improved solvent deasphalting, without excessive blending and dilution, by virtue of much faster deasphalting at low solvent to oil ratios, including separation of asphaltenes from deasphalted oil (in contrast to prior art methods) . More particularly, this improved deasphalting is achieved by applying low-frequency, high amplitude acoustic energy to the HCO-solvent process stream (referred to as "sonication" of the HCO-solvent mixture) followed by separation of precipitated solvent insolubles (asphaltenes) via filtration, centrifugation, settling, or other appropriate technique. The method results in a SCO product that meets pipeline specifications in terms of API gravity and viscosity.
  • the current invention is a method for simplified, accelerated deasphalting of HCO' s with non-polar solvents, under low frequency acoustic sonication at an audio frequency that is well below the ultrasonic range (ultrasound frequency range commences at approximately 20,000 Hertz (Hz) ) .
  • “Audio frequency” refers to a range of 16Hz to 20,000Hz, however, in the preferred embodiment of the invention the sonic mixing takes place at a frequency range of 30Hz-5, 000Hz, or more preferably, in a range of lOOHz-1, 000Hz .
  • Such sonication devices come in two preferred types: sonicating probes in direct contact with fluids; and fluid containing vessels where the sonication is applied indirectly to the fluids via the vessel (e.g. component #44 on United States patent 5,005,773) .
  • Sonication devices can be of any type which can generate the desired acoustic frequency, high amplitude and sufficient energy density to the process fluids at an industrial scale.
  • the preferred sonication device would achieve a high energy efficiency by using a balanced dynamic system operating at its natural resonance frequency to sonicate the fluid containing vessel (e.g. see Nyberg United States patents 4,941,134 and 5,005,773 component #44 where such vessel is mounted axially to the resonating member but in the absence of grinding media) .
  • non-polar, non-cyclic, low molecular weight alkane solvents and their associated analogs such as propane, pentane, hexane, heptane and iso-octane are used.
  • “Sonication” and “low frequency acoustic sonication” refer to methods whereby a material is subjected to low frequency acoustic vibration.
  • Devices for producing such vibration, “sonicators” are disclosed in, for example, U.S. Patents No. 4,941,134 and 5,005,773 (Nyberg et al.) .
  • these low frequency sonic reactors are reducible to large scale commercial practice (e.g. ⁇ 20 kilowatt sonicator modules) and can achieve HCO deasphalting at low solvent :HCO doses (with ultra-low residence times in the sonicator (e.g. less than 120 seconds) .
  • Figure 1 is a Heavy Oil Deasphalting Process Flow Diagram
  • Figure 2 is a Heavy Oil Upgrading Process Flow Diagram
  • Figure 3 is a SIMDIST graph for Upgraded and Raw oil showing boiling point temperature versus percentage of oil distilled at that temperature for heavy oil from South Western Texas;
  • Figure 4 is a SIMDIST graph for heavy oil from Lloydminster
  • Figure 5 is a SIMDIST graph for heavy oil from Bulgaria
  • Figure 6 is a SIMDIST graph for American Oil Refinery Residue .
  • the process is comprised of the following key unit operations:
  • the sonication device reactor typically involves the conversion of electric power, via sequentially activated magnets, to produce vibrational energy.
  • one sonication device used an electro-magnetic drive system to resonate a three tonne solid steel bar. Vibrational energy from the bar is transmitted to the attached to the fluid containing sonic reaction chambers (vessels containing the HCO-solvent mixture) and through which fluid materials can be pumped and be subjected to very intense audio frequency agitation ("sonication”) .
  • the vigorous sonication is used in the current process to enhance solvent extraction of the non- asphaltene fraction from the HCO through enhanced mass transfer as a result of the sonication and secondary effects such as cavitation.
  • the sonic reactors are large (beyond bench and lab scale) low frequency sonication reactors that have sufficient processing capacity for commercial applications.
  • the sonic reactors are readily transportable and require no anchoring once on site.
  • Heat generation testwork indicates specific energy inputs for the 20 kW to 50 kW sonic reactor ranging up to 90 kW/m 3 of reactor volume (450 Horsepower/1, 000 US gallons) .
  • This range of power input is at least one to two orders of magnitude (10 to 100 times) greater than is achieved by energy intensive industrial mixing systems such as flotation cells or standard agitation systems.
  • the energy and fluid dynamic conditions and energy intensity produced by sonication devices, and in particular by the sonic reactors, is advantageous for chemical process operations. Sonication enhances process reactions by causing intense mixing and other fluid dynamic effects such that sonication improves the selectivity or efficiency of the desired chemical or physical reaction.
  • the oil came from a heavy oil field located in Southwestern Texas. Fifty grams of the Southeastern Texas HCO was blended with 175 grams of iso-octane solvent (225 grams total) for sonic deasphalting in a baffled 1.7 litre stainless steel reaction chamber. The deasphalting occurred at 25 kW power applied continuously for 120 seconds in batch mode in a 1.7 fire sonic reaction chamber. Subsequently the deasphalted material was separated through direct vacuum filtration. Optionally, the subsequent deasphalted oil was oxidized via the prior art described by Boakye (Canadian patent #2,549,358) utilizing acetic acid, hydrogen peroxide, peroxidase enzyme source (i.e.
  • soyabean husk soyabean husk
  • iron oxide The oxidation reaction was quenched through absorption of generated polar compounds and sulfur compounds by passing the deasphalted HCO/solvent/reagent reaction product through a natural clay and activated carbon mixture that removes excess and/or unconsumed oxidation reagents.
  • the solvent is recovered by atmospheric distillation at temperatures sufficient to evaporate the solvent. Any solvent recovery system may be used and persons skilled in the art may specify equipment based on recovery and cost considerations.
  • IBP Initial Boiling Point ( 0 C)
  • the SIMDIST shows the simulated distillation via gas chromatography of upgraded and raw oil from Southeastern, Texas.
  • the upper curve corresponds to raw- crude and the lower one to upgraded crude. This is the same for Figs. 4 to 6. If one arbitrarily chooses a value of 20 on the x-axis then 20 % of the upgraded oil is distilled at 260 0 C while 20 % of the raw oil is distilled at 310 0 C. Oil value tends to increase as the boiling points of its components decrease .
  • this SIMDIST graph corresponds to Example 2.
  • the oxidation reaction was quenched through absorption of generated polar compounds and sulfur compounds by passing the deasphalted HCO/solvent/reagent reaction product through a natural clay and activated carbon mixture that remove all excess and/or unconsumed oxidation reagents .
  • this SIMDIST refers to the heavy oil from Bulgaria
  • the next test sample was Processed American oil refinery residue.
  • the oil refinery residue (“asphalt extender tank bottoms”) came from an oil refinery manufacturing refinery gas fuels, fuel additives, lubricants and anticorrosive materials.
  • the oxidation reaction was quenched through absorption of generated polar compounds and sulfur compounds by passing the deasphalted HCO/solvent/reagent reaction product through a natural clay and activated carbon mixture that remove all excess and/or unconsumed oxidation reagents.
  • IBP Initial Boiling Point ( 0 C) Referring to Fig. 6, this SIMDIST corresponds to Example 4.
  • the methodology involved mixing to a solvent: oil ratio of 1.09 by adding 690.9 g heavy crude oil (HCO) from Alberta with 631.6 g of solvent (n-hexane) (1,323 grams total) and therefore a solvent:oil weight ratio of 0.91, in a baffled 1.7 litre stainless steel reaction chamber. Acoustic energy was applied for 60 seconds at 40 kW continuously in batch mode followed by direct insoluble asphaltenes fraction filtration and atmospheric pressure distillation for solvent removal. The mass yield on deasphalted oil was 95.5% of the HCO feedstock. Table 11

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  • 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)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

La présente invention concerne un procédé de traitement du pétrole brut lourd (HCO), comprenant les étapes suivantes : mélange du pétrole brut lourd (HCO) avec un alcane contenant du solvant pour former un mélange HCO/solvant; sonication de ce mélange à une fréquence audio pour précipiter les asphaltènes provenant du mélange HCO/solvant; et séparation des asphaltènes précipités provenant du mélange HCO/solvant.
EP09719531A 2008-03-11 2009-03-11 Procédé de traitement de pétrole brut lourd Withdrawn EP2260089A4 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US3569008P 2008-03-11 2008-03-11
PCT/CA2009/000289 WO2009111871A1 (fr) 2008-03-11 2009-03-11 Procédé de traitement de pétrole brut lourd

Publications (2)

Publication Number Publication Date
EP2260089A1 true EP2260089A1 (fr) 2010-12-15
EP2260089A4 EP2260089A4 (fr) 2011-10-05

Family

ID=41064697

Family Applications (1)

Application Number Title Priority Date Filing Date
EP09719531A Withdrawn EP2260089A4 (fr) 2008-03-11 2009-03-11 Procédé de traitement de pétrole brut lourd

Country Status (4)

Country Link
US (1) US20130277275A1 (fr)
EP (1) EP2260089A4 (fr)
EA (2) EA201401282A1 (fr)
WO (1) WO2009111871A1 (fr)

Families Citing this family (19)

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Publication number Priority date Publication date Assignee Title
US8475652B2 (en) * 2009-10-19 2013-07-02 Jan A. K. Paul Method for purification of uncatalyzed natural fuels from metal ions by means of at least one hemeprotein and use of the at least on hemeprotein
CN101798523A (zh) * 2010-03-16 2010-08-11 李守春 一种重油的辅助过滤方法
EP2404983A1 (fr) * 2010-07-06 2012-01-11 Total Raffinage Marketing Réacteurs de préparation de catalyseur à partir d'un précurseur de catalyseur utilisé pour alimenter les réacteurs en vue d'améliorer les produits de départ hydrocarbonés lourds
CA2729457C (fr) 2011-01-27 2013-08-06 Fort Hills Energy L.P. Procede pour l'integration d'un centre de traitement de l'ecume paraffinique a une installation de forage et d'extraction de minerai bitumineux
CA2853070C (fr) 2011-02-25 2015-12-15 Fort Hills Energy L.P. Procede de traitement de bitume dilue a forte teneur en paraffine
CA2733342C (fr) 2011-03-01 2016-08-02 Fort Hills Energy L.P. Procede et unite pour la recuperation de solvant dans des residus dilues dans un solvant, provenant du traitement de la mousse de bitume
CA2733862C (fr) 2011-03-04 2014-07-22 Fort Hills Energy L.P. Procede et systeme pour l'ajout de solvant a de la mousse de bitume
CA2735311C (fr) 2011-03-22 2013-09-24 Fort Hills Energy L.P. Procede pour un chauffage a injection de vapeur directe de la mousse de bitume des sables bitumineux
CA2737410C (fr) 2011-04-15 2013-10-15 Fort Hills Energy L.P. Dispositif de recuperation de chaleur pour integration dans une usine de traitement de mousse de bitume avec circuit de refroidissement en boucle fermee
CA2805804C (fr) 2011-04-28 2014-07-08 Fort Hills Energy L.P. Procede et ursr avec configuration multi buse pour la distribution des residus dilues par solvant
CA2832269C (fr) 2011-05-18 2017-10-17 Fort Hills Energy L.P. Regulation de temperature pour un procede de traitement de mousse de bitume avec chauffage de compensation de courants de solvant
US9650312B2 (en) 2013-03-14 2017-05-16 Lummus Technology Inc. Integration of residue hydrocracking and hydrotreating
US20140259883A1 (en) * 2013-03-15 2014-09-18 Petrosonic Energy Inc. Emulsion fuel from sonication-generated asphaltenes
US20140262962A1 (en) * 2013-03-15 2014-09-18 Petrosonic Energy Inc. Hydrocarbons recovery with sonic treatment
US20140262961A1 (en) * 2013-03-15 2014-09-18 Petrosonic Energy Inc. Solvent selection process
CN103450920A (zh) * 2013-09-13 2013-12-18 中国农业大学 一种超声波处理生物原油提高重油产率的方法
WO2017185166A1 (fr) 2016-04-25 2017-11-02 Sherritt International Corporation Procédé de valorisation partielle d'huile lourde
RU2628611C1 (ru) * 2016-10-03 2017-08-21 федеральное государственное бюджетное образовательное учреждение высшего образования "Санкт-Петербургский горный университет" Способ переработки тяжелого нефтяного сырья
CN111575055B (zh) * 2020-05-22 2021-11-19 中国石油化工股份有限公司 渣油加氢原料预处理方法及其装置以及渣油加氢工艺

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See also references of WO2009111871A1 *

Also Published As

Publication number Publication date
EP2260089A4 (fr) 2011-10-05
WO2009111871A1 (fr) 2009-09-17
EA201071060A1 (ru) 2011-04-29
EA201401282A1 (ru) 2015-03-31
EA021729B1 (ru) 2015-08-31
US20130277275A1 (en) 2013-10-24

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