EP1838815A1 - Process for the conversion of heavy charge stocks such as heavy crude oils and distillation residues - Google Patents
Process for the conversion of heavy charge stocks such as heavy crude oils and distillation residuesInfo
- Publication number
- EP1838815A1 EP1838815A1 EP05819257A EP05819257A EP1838815A1 EP 1838815 A1 EP1838815 A1 EP 1838815A1 EP 05819257 A EP05819257 A EP 05819257A EP 05819257 A EP05819257 A EP 05819257A EP 1838815 A1 EP1838815 A1 EP 1838815A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- process according
- distillation
- section
- sda
- 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.)
- Ceased
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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
- C10G67/0454—Solvent desasphalting
- C10G67/049—The hydrotreatment being a hydrocracking
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- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1033—Oil well production fluids
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1077—Vacuum residues
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/205—Metal content
- C10G2300/206—Asphaltenes
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/207—Acid gases, e.g. H2S, COS, SO2, HCN
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4081—Recycling aspects
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/44—Solvents
Definitions
- PROCESS FOR THE CONVERSION OF HEAVY CHARGE STOCKS SUCH AS HEAVY CRUDE OILS AND DISTILLATION RESIDUES
- the present invention relates to a process for the conversion of heavy charge stocks , among which heavy crude oils , bitumens from oil sands and distillation residues , by means of at least three process units : deasphalting, hydro- conversion of the charge stock using phase-dispersed catalysts and distillation.
- the conversion of heavy crude oils , bitumens from oil sands and petroleum residues into liquid products can be substantially effected in two ways : an exclusively thermal one and the other by means of hydrogenating treatment .
- the hydroconversion technologies which are at present on the market , use fixed or ebullated bed reactors and make use of catalysts generally consisting of one or more transition metals (Mo, W, Ni , Co, etc .. ) supported on silica/alumina (or equivalent material ) .
- Fixed bed technologies have several problems in treating particularly heavy charge stocks , containing high percentages of hetero-atoms , metals and asphaltenes , as these contaminants lead to a fast deactivation of the catalyst .
- Hydrotreating technologies using dispersed phase catalysts can represent an interesting solution to the drawbacks of the fixed and ebullated bed technologies .
- Slurry processes in fact , combine the advantage of a high flexibility on the charge stock with high performances in terms of conversion and upgrading, proving, at least in principle , to be simpler from a technological point of view .
- Slurry technologies are characterized by the presence of catalyst particles having very small average dimensions and suitably dispersed in the medium: for this reason the hydrogenation processes are easier and immediate in all parts of the reactor .
- the formation of coke is considerably reduced and the upgrading of the charge stock is high .
- the catalyst can be introduced as powder with suffi- ciently reduced dimensions (US- 4 , 303 , 634 ) or as an oil- soluble precursor (US-5 , 288 , 681) .
- the active form of the catalyst generally the metal sulphide
- the metal components of the dispersed catalysts are normally one or more transition metals (preferably Mo, W, Ni , Co or Ru) .
- Molybdenum and tungsten have much more sat- isfactory performances with respect to nickel , cobalt or ruthenium, and even more with respect to vanadium and iron (N. Panariti et al . , Appl . Ctal . A: Gen . 2000 , 204 , 203 ) .
- the way these catalysts are used are extremely important both from an economical and environmental point of view .
- the catalyst can be used at a low concentration (a few hundred ppm) in the "once-through" mode , but in this case the upgrading of the reaction products is generally unsatisfactory (N . Pnariti et al . , Appl . Ctal . A: Gen . , 2000 , 204 , 203 and 215 ) .
- the catalyst at the reactor outlet can be recovered by separation of the product obtained from the hydrotreating (preferably from the bottom of the distillation column downstream of the reactor) through conventional methods such as , for example , decanting, centrifugation or filtration (US-3 , 240 , 718 ; US-4 , 762 , 812 ) which are , however, ex- tremely complex if applied to heavy charge stocks rich in poisoning substances .
- asphaltenes are hydrocarbons which can be precipitated from a crude oil or an oil residue , by treatment with a paraffinic hydrocarbon with a number of carbon atoms ranging from 3 to 7 , for example n-heptane un- der the standard conditions provided for by the regulation IP - 143 .
- control of the loss of stability of a heavy charge stock during a thermal and/or catalytic conversion is therefore fundamental for obtaining the maximum conversion degree without creating problems due to the formation of coke or fouling .
- the optimum operative conditions (mainly reaction temperature and residence time) are simply determined on the basis of the stability of the reactor effluent through direct measurements on the non- converted residue (P value , Hot Filtration Test , Spot Test , etc .. ) .
- hydroconversion with catalysts in slurry phase (HT) , distillation or flash (D) , deasphalting (SDA) is characterized in that the three units operate on mixed streams consisting of fresh charge stock and recycled streams , using the following steps : * sending at least one fraction of the heavy charge stock to a deasphalting section (SDA) in the presence of solvents , obtaining two streams , one consisting of deasphalted oil (DAO) , the other of asphalts ; * mixing the asphalt with a suitable hydrogenation cata- lyst and possibly with the remaining fraction of the heavy charge stock not sent to the deasphalting section and sending the mix obtained to a hydrotreating reactor (HT) , introducing into the same reactor hydrogen or a mix of hydrogen and H 2 S; * sending the stream containing the product of the hy- drotreating reaction and the catalyst in dispersed phase to one or more distillation or flash (D)
- n represents the number of carbon atoms of the paraffin used in the deasphalting operation (normally from 3 to 6) .
- the process, obj ect of the present invention for the conversion of heavy and extra-heavy charge stocks by the combined use of at least the three following process units : solvent deasphalting (SDA) , hydroconversion with catalysts in slurry phase (HT) , distillation or flash (D) , is characterized in that it comprises the following steps :
- the heavy charge stocks treated can be of a varying nature : they can be selected from heavy crude oils , distillation residues , heavy oils coming from catalytic treatments , for example “unconverted oils” from fixed or ebul- lated bed hydrotreatment , “heavy cycle oils” from catalytic cracking treatment , “thermal tars” (coming, for example from visbreaking or similar thermal processes) , bitumens from “oil sands” , different kinds of coals and any other high boiling charge stock of a hydrocarbon origin, normally known in the art as “black oils” .
- the stream containing asphaltenes obtained in the deasphalting section (SDA) can be optionally mixed with the remaining part of the distillation residue (tar) , or the liquid coming from the flash unit , not recycled to the hy- drotreatment section (HT) .
- Said stream containing asphaltenes , mixed or not mixed with part of the distillation residue (tar) or of the liquid coming from the flash unit can be :
- the gasification can be effected by feeding to the gasification unit , in addition to the charge stock, oxygen and vapour which react under exothermic conditions at a temperature of over 1300 0 C and a pressure ranging from 30 to 80 bar, to produce mainly H 2 and CO .
- a stream of syngas , or a mix of H 2 and CO, can be obtained from the gasification section, which can be further used as fuel by means of combustion with combined cycles (IGCC) or transformed into paraffinic hydrocarbons by means of Fisher-Tropsch synthesis or converted into methanol , dimethyl ether, formaldehyde and, more generally, into the whole series of products deriving from Cl chemistry .
- IGCC combustion with combined cycles
- the same paraffinic hydrocarbons obtained via Fisher- Tropsch can be mixed with the various cuts obtained from the distillation or flash step , improving their composition characteristics .
- the catalyst precursors used can be selected from those obtained from easily decomposable oil -soluble precursors (metal naphthenates , metal derivatives of phosphonic acids , metal-carbonyls , etc .. ) or from preformed compounds based on one or more transition metals such as Ni , Co, Ru, W and Mo : the latter is preferred thanks to its higher catalytic activity.
- the catalyst concentration defined on the basis of the concentration of the metal or metals present in the hy- droconversion reactor, ranges from 350 to 30 , 000 ppm, preferably from 3 , 000 to 20 , 000 ppm, more preferably from 5 , 000 to 15 , 000 ppm.
- the hydrotreatment step (HT) is preferably carried out at a temperature ranging from 360 to 450 0 C, more preferably from 380 to 440 0 C, and at a pressure ranging from 3 to 30 MPa, preferably from 10 to 20 MPa .
- Hydrogen is fed to the reactor, which can operate in both a down-flow mode and, preferably, up-flow. Said gas can be fed to several sections of the reactor .
- the distillation steps are preferably effected under reduced pressure , ranging from 0.001 to 0.5 MPa, preferably from 0.1 to 0.3 MPa .
- the hydrotreatment step (HT) can consist of one or more reactors operating within the condition range mentioned above . Part of the distillates produced in the first reactor can be recycled to the subsequent reactors of the same step .
- the deasphalting step (SDA) effected by means of an extraction with solvent , either a hydrocarbon solvent or not , is normally carried out at temperatures ranging from 40 to 200 0 C and a pressure of 0.1 to 7 MPa .
- the solvent recovery can be effected under sub-critical or supercritical multi-step conditions , thus allowing a further fractionation between the deasphalted oil and resins .
- the solvent of this deasphalting step is selected from light paraffins having from 3 to 6 carbon atoms , preferably from 4 to 5 carbon atoms , more preferably having 5 carbon atoms .
- a further secondary section can be optionally present for the hydro- genation post-treatment of the C 2 -500 °C fraction, pref- erably the C 5 -350 °C fraction, coming from the section of high pressure separators envisaged upstream of the distillation .
- the stream containing the hydro- treatment reaction product and the catalyst in dispersed phase is subj ected to a separation pre-step, effected at high pressure , so as to obtain a light fraction and a heavy fraction, this heavy fraction alone being sent to said distillation (D) step (s) .
- the light fraction obtained from the high pressure separation step can be sent to a hydrotreatment section, producing a lighter fraction containing Ci-C 4 and H 2 S gas and a less light fraction containing hydrotreated naphtha and gas oil .
- fuels can be obtained, starting from oil charge stocks which are extremely rich in sulphur, in line with the strictest specifications on the sulphur content ( ⁇ 10-50 ppm of sulphur) and improved as far as other characteristics of diesel gas oil are concerned, such as density, poly-aromatic hydrocarbon content and the cetane number;
- the post-treatment hydrogenation on a fixed bed consists of the preliminary separation of the reaction effluent of the hydrotreatment reactor (HT) by means of one or more separators operating at high pressure and high temperature .
- the heavy part extracted from the bottom, is sent to the main distillation unit , the aliquot which is extracted from the head, a C 5 -350 °C fraction, is sent to a secondary treatment section in the presence of hydrogen, available at high pressure , where the reactor is of the fixed bed type and contains a typical desulphurisa- tion/dearomatisation catalyst , in order to obtain a product which having a considerably lowered sulphur content and also lower nitrogen contents , a lower total density and, at the same time, increased cetane numbers as far as the gas oil fraction is concerned .
- the hydrotreatment section normally consists of one or more reactors in series ; , the product of this system can be subsequently further fractionated by distillation to obtain a thoroughly desulphurated naphtha and a diesel gas oil within specification as fuel .
- the fixed-bed hydrodesulphurisation step normally uses typical fixed-bed catalysts for gas oil hydrodesulphurisation; said catalyst , or possibly a mix of catalysts or a series of reactors with various catalysts having different properties , causes a deep refining of the light fraction, significantly reducing the sulphur and nitrogen content , increasing the hydrogenation degree of the charge stock, thus diminishing the density and increasing the cetane number of the gas oil fraction, at the same time reducing the formation of coke .
- the catalyst normally consists of an amorphous part based on alumina, silica, silico-alumina and blends of different mineral oxides , on which a hydrodesulphurizing component in association with a hydrogenating product , is deposited (with several methods) .
- Catalysts based on molybde- nura or tungsten with the addition of nickel and/or cobalt , deposited on a mineral amorphous carrier, are typical catalysts for this type of operation .
- the post-treatment hydrogenation reaction is effected at an absolute pressure slightly lower than that of the pri- mary hydrotreatment step, normally ranging from 7 to 14
- the space velocity is another im- portant variable in controlling the quality of the product obtained : it can range from 0.1 to 5 h "1 , preferably from
- the quantity of hydrogen mixed with the charge stock is fed at a flow-rate ranging from 100 to 5 , 000 Nm 3 /m 3 , pref- erably from 300 to 1 , 000 Nm 3 /m 3 .
- Two streams are obtained from the deasphalting unit (SDA) : one stream (2 ) consisting of deasphalted oil (DAO) , the other stream containing asphaltenes (3 ) .
- the stream containing asphaltenes (3 ) is sent to a gasi- fication section (PO x ) in order to obtain syngas, i . e . a gaseous mix of H 2 and CO (4 ) .
- the stream consisting of deasphalted oil (2 ) is mixed with the fresh make-up catalyst (5) (necessary for reinte- grating that lost with the stream (15 ) described hereunder) and with the stream ( 14) (described hereunder) coming from the bottom of the distillation or flash column (D) to form the stream (6) which is fed to the hydrotreatment reactor (HT) into which hydrogen (or a mix containing hydrogen and H 2 S) (7) is fed .
- HT hydrotreatment reactor
- the hydrogen fed can be part of the hydrogen coming from the gasification step (PO x ) (not schematised in the figure) .
- a stream (8) leaves the reactor (HT) , containing the hy- drogenation product and the catalyst in dispersed phase , which is fractionated in a distillation or flash column (D) from which the lighter fraction (9) separates together with the distillable products (10 ) , (11) and (12 ) from the distillation residue (13 ) containing the dispersed catalyst and coke .
- This stream (13 ) (called tar) is mostly recycled (14 ) to the hydrotreatment unit (HT) , the remaining part (15) being sent to the gasification section (PO x ) .
- Example 1 An example is provided for a better understanding of the invention, it being understood that the invention should not be considered as being limited thereto or thereby .
- Example 1
- the yield obtained by the procedure described is equal to 82% by weight of deasphalted oil with respect to the starting vacuum residue .
- RV Ural and deasphalted oil are shown in table 1.
- Table 1 Characteristics of the vacuum residue Ural 500 0 C and DAO n-C5 extracted .
- Catalytic tests were carried out using a stirred micro-autoclave of 30 cm 3 , in accordance with the following general operative procedure : about 10 g of the charge stock are introduced into the reactor and the catalyst precursor is added; the system is then pressurized with hydrogen and brought to temperature by means of an electrically heated oven; the system is maintained under stirring during the reaction by a swinging capillary system operating at a rotational rate of 900 rpm; moreover, the total pressure is kept constant by means of an automatic reintegration system of the hydrogen consumed; - quenching of the reaction is carried out once the test has been completed; the autoclave is then de- pressurised and the gas collected in a sampling bag; the gaseous samples are then sent for gas- chromatographic analysis ; - the products present in the reactor are recovered without the addition of any solvent , and analyzed in terms of distribution of the distillates , sulphur content , nitrogen content , coal residue and metal content .
- Atmospheric gas oil (AGO, 170-350 0 C) : 27%
- Vacuum gas oil (VGO, 350 -500 0 C) : 31%
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
IT002446A ITMI20042446A1 (en) | 2004-12-22 | 2004-12-22 | PROCEDURE FOR CONVERSION OF PESANTYI CHARGES SUCH AS HEAVY CRATES AND DISTILLATION RESIDUES |
PCT/EP2005/013684 WO2006066857A1 (en) | 2004-12-22 | 2005-12-19 | Process for the conversion of heavy charge stocks such as heavy crude oils and distillation residues |
Publications (1)
Publication Number | Publication Date |
---|---|
EP1838815A1 true EP1838815A1 (en) | 2007-10-03 |
Family
ID=35134129
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP05819257A Ceased EP1838815A1 (en) | 2004-12-22 | 2005-12-19 | Process for the conversion of heavy charge stocks such as heavy crude oils and distillation residues |
Country Status (9)
Country | Link |
---|---|
US (2) | US20060272982A1 (en) |
EP (1) | EP1838815A1 (en) |
CN (1) | CN101098949B (en) |
AU (1) | AU2005318443B2 (en) |
BR (1) | BRPI0519489B1 (en) |
CA (1) | CA2530906C (en) |
IT (1) | ITMI20042446A1 (en) |
MX (1) | MX2007007545A (en) |
WO (1) | WO2006066857A1 (en) |
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ITMI20011438A1 (en) * | 2001-07-06 | 2003-01-06 | Snam Progetti | PROCEDURE FOR THE CONVERSION OF HEAVY CHARGES SUCH AS HEAVY FATS AND DISTILLATION RESIDUES |
US7678732B2 (en) | 2004-09-10 | 2010-03-16 | Chevron Usa Inc. | Highly active slurry catalyst composition |
US7972499B2 (en) | 2004-09-10 | 2011-07-05 | Chevron U.S.A. Inc. | Process for recycling an active slurry catalyst composition in heavy oil upgrading |
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US8372266B2 (en) | 2005-12-16 | 2013-02-12 | Chevron U.S.A. Inc. | Systems and methods for producing a crude product |
US8048292B2 (en) | 2005-12-16 | 2011-11-01 | Chevron U.S.A. Inc. | Systems and methods for producing a crude product |
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ITMI20061511A1 (en) * | 2006-07-31 | 2008-02-01 | Eni Spa | PROCEDURE FOR THE TOTAL CONVERSION TO HEAVY DISTILLATES |
ITMI20061512A1 (en) * | 2006-07-31 | 2008-02-01 | Eni Spa | PROCEDURE FOR THE TOTAL CONVERSION OF HEAVY DUTIES TO DISTILLATES |
WO2008027139A1 (en) | 2006-08-31 | 2008-03-06 | Exxonmobil Chemical Patents Inc. | Method for upgrading steam cracker tar using pox /cocker |
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CN101098949B (en) | 2012-09-05 |
CN101098949A (en) | 2008-01-02 |
BRPI0519489A2 (en) | 2009-02-03 |
BRPI0519489B1 (en) | 2015-10-27 |
AU2005318443B2 (en) | 2011-01-20 |
US20060272982A1 (en) | 2006-12-07 |
CA2530906C (en) | 2010-06-29 |
MX2007007545A (en) | 2007-08-14 |
AU2005318443A1 (en) | 2006-06-29 |
ITMI20042446A1 (en) | 2005-03-22 |
US20130112593A1 (en) | 2013-05-09 |
CA2530906A1 (en) | 2006-06-22 |
WO2006066857A1 (en) | 2006-06-29 |
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