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WO2005066309A2 - Systemes et procedes de production d'un produit brut - Google Patents

Systemes et procedes de production d'un produit brut Download PDF

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Publication number
WO2005066309A2
WO2005066309A2 PCT/US2004/042222 US2004042222W WO2005066309A2 WO 2005066309 A2 WO2005066309 A2 WO 2005066309A2 US 2004042222 W US2004042222 W US 2004042222W WO 2005066309 A2 WO2005066309 A2 WO 2005066309A2
Authority
WO
WIPO (PCT)
Prior art keywords
grams
crude product
crude
crude feed
catalyst
Prior art date
Application number
PCT/US2004/042222
Other languages
English (en)
Other versions
WO2005066309A3 (fr
Inventor
Thomas F. Brownscombe
Scott Lee Wellington
Original Assignee
Shell Internationale Research Maatschappij B.V.
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 Shell Internationale Research Maatschappij B.V. filed Critical Shell Internationale Research Maatschappij B.V.
Priority to EP04814410A priority Critical patent/EP1704210A2/fr
Priority to CA002550255A priority patent/CA2550255A1/fr
Priority to JP2006545418A priority patent/JP2007514829A/ja
Priority to MXPA06006796A priority patent/MXPA06006796A/es
Publication of WO2005066309A2 publication Critical patent/WO2005066309A2/fr
Publication of WO2005066309A3 publication Critical patent/WO2005066309A3/fr

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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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/78—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with alkali- or alkaline earth metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
    • B01J27/04—Sulfides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
    • B01J27/04—Sulfides
    • B01J27/043—Sulfides with iron group metals or platinum group metals
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/02—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used
    • 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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • 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
    • C10G2300/1074—Vacuum distillates
    • 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
    • C10G2300/1096—Aromatics or polyaromatics
    • 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
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/301—Boiling range
    • 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
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]

Definitions

  • High residue crudes may be treated at high temperatures to convert the crude to coke.
  • high residue crudes are typically treated with water at high temperatures to produce less viscous crudes and/or crude mixtures.
  • water removal from the less viscous crudes and/or crude mixtures may be difficult using conventional means.
  • Disadvantaged crudes may include hydrogen deficient hydrocarbons. When processing of hydrogen deficient hydrocarbons, consistent quantities of hydrogen generally need to be added, particularly if unsaturated fragments resulting from cracking processes are produced. Hydrogenation during processing, which typically involves the use of an active hydrogenation catalyst, may be needed to inhibit unsaturated fragments from forming coke.
  • the invention also provides a method of producing a crude product, comprising: contacting a crude feed with a hydrogen source in the presence of one or more catalysts comprising a transition metal sulfide catalyst to produce a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °C and 0.101 MPa, the transition metal sulfide catalyst has a total of least 0.4 grams of one or more transition metal sulfides per gram of total transition metal sulfide catalyst, the crude feed has a total Ni/N/Fe content of at least 0.0001 grams of ⁇ i N/Fe per gram of crude feed, and the crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed; and controlling contacting conditions such that the crude product has at most 0.05 grams of coke per gram of crude product, the crude product has a total ⁇ i/N/Fe content of at most 90% of the ⁇ i/N/Fe content of the crude feed, the crude product has a residue
  • the invention also provides a method of producing a crude product, comprising: contacting a crude feed with a hydrogen source in the presence of one or more catalysts comprising a transition metal sulfide catalyst to produce a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °C and 0.101 MPa, the transition metal sulfide catalyst comprises a transition metal sulfide, the crude feed having a residue content of at least 0.2 grams of residue per gram of crude feed, as determined by ASTM Method D5307; controlling contact conditions such that the crude product has a residue content of at most 30% of the residue content of the crude feed; and wherein the transition metal sulfide catalyst is obtainable by: mixing a transition metal oxide and a metal salt to form a transition metal oxide/metal salt mixture; reacting the transition metal oxide/metal salt mixture with hydrogen to form an intermediate; and reacting the intermediate with sulfur in the presence of one or more hydrocarbons to produce the transition metal sulfide catalyst.
  • the invention also provides, in combination with one or more of the methods or compositions according to the invention, a crude product that has at least one of the catalysts comprising one or more alkali metals, in which: (a) at least one of the alkali metals is potassium, rubidium; or cesium, or mixtures thereof; and/or (b) at . least one of the ' .catalysts further comprises a transition metal, a transition metal sulfide and/or bartonite.
  • features from specific embodiments of the invention may be combined with features from other embodiments of the invention. For example, features from one embodiment may be combined with features from any of the other embodiments.
  • FIG. 3 is a schematic of an embodiment of a separation zone in combination with a contacting system.
  • FIG. 4 is a schematic of an embodiment of a blending zone in combination with a contacting system.
  • FIG. 5 is a schematic of an embodiment of a separation zone, a contacting system, and a blending zone.
  • FIG. 6 is a schematic of an embodiment of multiple contacting systems.
  • FIG. 7 is a schematic of an embodiment of an ionic conductivity measurement system.
  • FIG. 8 is a tabulation of properties of the crude feed and properties of crude products obtained from embodiments of contacting the crude feed with the transition metal sulfide catalyst.
  • FIG. 9 is a tabulation of compositions.
  • Disadvantaged crudes may include, per gram of disadvantaged crude: at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons with a boiling range distribution between 200 °C and 300 °C at 0.101 MPa; at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons with a boiling range distribution between 300 °C and 400 °C at 0.101 MPa; and at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons with a boiling range distribution between 400 °C and 700 °C at 0.101 MPa, or combinations thereof.
  • the vapor produced from the top of contacting zone 102 includes from 0.8-0.99 grams, or 0.9- 0.98 grams of crude product per gram of crude feed.
  • Used catalyst and/or solids may remain in contacting zone 102 as by-products of the contacting process.
  • the solids and/or used catalyst may include residual crude feed and/or coke.
  • separation unit 116 the vapor is cooled and separated to form the crude product and gases using standard separation techniques.
  • the crude product exits separation unit 116 and enters crude product receiver 119 via conduit 118.
  • the resulting crude product may be suitable for transportation and/or treatment.
  • Crude product receiver 119 may include one or more pipelines, one or more storage units, one or more transportation vessels, or combinations thereof.
  • the crude product may have a nitrogen content of at most 90% or at most 80% of a nitrogen content of the crude feed.
  • the nitrogen content of the crude product, per gram of crude product may be at most 0.004 grams, at most 0.003 grams, or at most 0.001 grams.
  • the crude product has, per gram of crude product, a nitrogen content in a range from 0.0001-0.005 grams, or 0.001-0.003 grams.
  • the crude product has, per gram of crude product, from 0.05-0.2 grams, or 0.09-0.15 grams of hydrogen.
  • the H/C of the crude product may be at most 1.8, at most 1.7, at most 1.6, at most 1.5, or at most 1.4.
  • the crude product has, per gram of crude product, a paraTxylene content from 0.001-0.09 grams, 0.005-0.08 grams, or 0.001-0.06 grams.
  • An increase in the aromatics content of naphtha tends to increase the octane number of the naphtha.
  • Crudes may be valued based on an estimation of a gasoline potential of the crudes. Gasoline potential may include, but is not limited to, a calculated octane number for the naphtha portion of the crudes. Crudes typically have calculated octane numbers in a range of 35-60.
  • the octane number of gasoline tends to reduce the requirement for additives that increase the octane number of the gasoline.
  • Example 2 Contact of a Crude Feed With a Hydrogen Source in the Presence of a K-Fe Sulfide Catalyst.
  • a 600 mL continuously stined tank reactor (composed of 316 stainless steel) was fitted with a bottom inlet feed port, a single vapor effluent sport, three thermocouples located in the reactor interior, and a shaftdriven 1.25 -inch diameter six- blade Rushton turbine.
  • ⁇ • -i The K-Fe sulfide catalyst (110.3 grams) prepared as described in Example 1 was charged to the reactor.
  • Hydrogen gas was metered at 8,000 Nm Ira. (50,000 SCFB) into the reactor and mixed with bitumen (Lloydminster region of Canada). The bitumen entered the reactor through the bottom inlet feed port to form a hydrogen/crude feed mixture.
  • bitumen Lioydminster region of Canada
  • Crude feed was fed at a rate of 67.0 g/hr to maintain the crude feed liquid level at 60% of the reactor volume.
  • a 50 milli-curie Cs gamma ray source and a sodium iodide scintillation detector were used to measure the liquid level in the reactor.
  • the K 2 CO 3 /Rb 2 CO /Cs CO 3 catalyst supported on alumina showed a cunent inflection of greater than 0.2 volts for emitted carbon dioxide and a cunent inflection of 0.01 volts for emitted water from the inorganic salt catalyst at 360 °C.
  • the minimum TAP temperature was 360 °C, as determined by plotting the log 10 of the ion cunent versus temperature.
  • FIG. 11 is a graphical representation of log 10 plots of ion cunent of emitted gases from the K 2 CO 3 /Rb 2 CO 3 /Cs2CO 3 catalyst ("log (I)") versus temperature ("T").
  • the used catalyst (“first used catalyst”) was removed from the reactor, weighed, and then analyzed.
  • the first used catalyst had an increase in weight from 31.6 grams to a total weight of 37.38 grams (an increase of 18 wt%, based on the weight of the original

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Catalysts (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Lubricants (AREA)
  • Liquid Carbonaceous Fuels (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

La présente invention a trait à un procédé comprenant la mise en contact avec un ou des catalyseurs pour la production d'un produit total comportant un produit brut. La charge brute comporte une teneur en résidus d'au moins 0,2 grammes de résidu par gramme de charge brute. Le produit brut est un mélange liquide à 25°C et 0,101 MPa. Une ou plusieurs propriété(s) du produit brut peut/peuvent être modifiée(s) par au moins 10% par rapport aux propriétés respectives de la charge brute. Dans certains modes de réalisation, du gaz est produit lors du contact entre un ou des catalyseurs et la charge brute.
PCT/US2004/042222 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut WO2005066309A2 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP04814410A EP1704210A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
CA002550255A CA2550255A1 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
JP2006545418A JP2007514829A (ja) 2003-12-19 2004-12-16 原油生成物を製造するシステム及び方法
MXPA06006796A MXPA06006796A (es) 2003-12-19 2004-12-16 Sistemas y metodos de produccion de un crudo producto.

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US53150603P 2003-12-19 2003-12-19
US60/531,506 2003-12-19
US61879904P 2004-10-14 2004-10-14
US60/618,799 2004-10-14

Publications (2)

Publication Number Publication Date
WO2005066309A2 true WO2005066309A2 (fr) 2005-07-21
WO2005066309A3 WO2005066309A3 (fr) 2006-01-05

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PCT/US2004/042123 WO2005066304A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042120 WO2005066302A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042127 WO2005061665A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042654 WO2005063936A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes permettant de produire un produit brut
PCT/US2004/042136 WO2005066305A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de fabrication de produits bruts
PCT/US2004/042648 WO2005061671A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production de produit brut
PCT/US2004/042222 WO2005066309A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042344 WO2005063928A2 (fr) 2003-12-19 2004-12-16 Systemes et procede de production d'un produit de petrole brut
PCT/US2004/042652 WO2005063675A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes permettant de produire un produit brut
PCT/US2004/042638 WO2005063932A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042218 WO2005066308A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042126 WO2005061664A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042122 WO2005066316A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut

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PCT/US2004/042123 WO2005066304A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042120 WO2005066302A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042127 WO2005061665A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042654 WO2005063936A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes permettant de produire un produit brut
PCT/US2004/042136 WO2005066305A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de fabrication de produits bruts
PCT/US2004/042648 WO2005061671A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production de produit brut

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PCT/US2004/042344 WO2005063928A2 (fr) 2003-12-19 2004-12-16 Systemes et procede de production d'un produit de petrole brut
PCT/US2004/042652 WO2005063675A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes permettant de produire un produit brut
PCT/US2004/042638 WO2005063932A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042218 WO2005066308A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042126 WO2005061664A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042122 WO2005066316A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut

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