WO2005063932A2 - 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
WO2005063932A2
WO2005063932A2 PCT/US2004/042638 US2004042638W WO2005063932A2 WO 2005063932 A2 WO2005063932 A2 WO 2005063932A2 US 2004042638 W US2004042638 W US 2004042638W WO 2005063932 A2 WO2005063932 A2 WO 2005063932A2
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WO
WIPO (PCT)
Prior art keywords
grams
crude product
crude
catalyst
crude feed
Prior art date
Application number
PCT/US2004/042638
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English (en)
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WO2005063932A3 (fr
Inventor
Stanley Nemec Milam
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 EA200601185A priority Critical patent/EA010396B1/ru
Priority to MXPA06006741A priority patent/MXPA06006741A/es
Priority to CA002551164A priority patent/CA2551164A1/fr
Priority to AU2004309348A priority patent/AU2004309348B2/en
Priority to JP2006545519A priority patent/JP2007514844A/ja
Priority to EP04814781A priority patent/EP1702023A2/fr
Priority to CN200480037852.2A priority patent/CN1894379B/zh
Publication of WO2005063932A2 publication Critical patent/WO2005063932A2/fr
Publication of WO2005063932A3 publication Critical patent/WO2005063932A3/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

  • the invention also provides, in combination with one or more of the methods or compositions according to the invention, an inorganic salt catalyst that includes alkali metals in which: (a) the atomic ratio of an alkali metal having an atomic number of at least 11 to an alkali metal having an atomic number greater than 11 is in a range from 0.1 to 4; (b) at least two of the alkali metals are sodium and potassium and an atomic ratio of sodium to potassium is in a range from 0.1 to 4; (c) at least three of the alkali metals are sodium, potassium, and rubidium, and each of the atomic ratios of sodium to potassium, sodium to rubidium, and potassium to rubidium is in a range from 0.1 to 5; (d) at least three of the alkali metals are sodium, potassium, and cesium, and each of the atomic ratios of sodium to potassium, sodium to cesium, and potassium to cesium is in a range from 0.1 to 5; (e) at least three of the alkali metals
  • Topped refers to a crude that has been treated such that at least some of the components that have a boiling point below 35 °C at 0.101 MPa are removed.
  • topped crudes typically have a content of at most 0.1 grams, at most 0.05 grams, or at most 0.02 grams of such components per gram of the topped crude.
  • Some stabilized crudes have properties that allow the stabilized crudes to be transported to conventional treatment facilities by transportation carriers (for example, pipelines, trucks, or ships).
  • Other crudes have one or more unsuitable properties that render them disadvantaged. Disadvantaged crudes may be unacceptable to a transportation carrier, and/or a treatment facility, thus imparting a low economic value to the disadvantaged crude.
  • disadvantaged crude may include, per gram of disadvantaged crude, at least 0.2 grams of residue, at least 0.3 grams of residue, at least 0.5 grams of residue, or at least 0.9 grams of residue. In certain embodiments, disadvantaged crude has 0.2-0.99 grams, 0.3-0.9 grams, or 0.4-0.7 grams of residue per gram of disadvantaged crude. In certain embodiments, disadvantaged crudes, per gram of disadvantaged crude, may have a sulfur content of at least 0.001 grams, at least 0.005 grams, at least 0.01 grams, or at least 0.02 grams. Disadvantaged crudes may include a mixture of hydrocarbons having a range of boiling points.
  • the total product includes the crude product that is a liquid mixture at STP and, in some embodiments, hydrocarbons that are not condensable at STP.
  • the total product and/or the crude product may include solids (such as inorganic solids and/or coke).
  • the solids maybe entrained in the liquid and/or vapor produced during contacting.
  • a contacting zone typically includes a reactor, a portion of a reactor, multiple portions of a reactor, or multiple reactors.
  • Aromatic compounds may include monocyclic ring compounds and/or polycyclic ring compounds.
  • the monocyclic ring compounds may include, but are not limited to, benzene, toluene, ortho-xylene, meta-xylene, para-xylene, ethyl benzene, l-ethyl-3-methyl benzene; 1-ethyl- 2-methyl benzene; 1, 2,3 -trimethyl benzene; 1,3,5-trimethyl benzene; l-methyl-3-propyl benzene; l-methyl-2-propyl benzene; 2-ethyl-l,4-dimethyl benzene; 2-ethyl-2,4-dimethyl benzene; 1,2,3,4-tetra-methyl benzene; ethyl, pentylmethyl benzene; 1,3 diethyl-2,4,5,6- tetramethyl benzene; tri-isopropyl-or
  • the kerosene has, per gram of kerosene, an aromatics content in a range from 0.1-0.5 grams, or from 0.2-0.4 grams.
  • a freezing point of the kerosene may be below -30 °C, below -40 °C, or below -50 °C.
  • An increase in the content of aromatics of the kerosene portion of the crude product tends to increase the density and reduce the freezing point of the kerosene portion of the crude product.
  • a crude product with a kerosene portion having a high density and low freezing point may be refined to produce aviation turbine fuel with the desirable properties of high density and low freezing point.
  • inorganic compositions are dissolved in a solvent (for example, water or a suitable organic solvent) to form an inorganic composition/solvent mixture.
  • a solvent for example, water or a suitable organic solvent
  • the solvent may be removed using standard separation techniques to produce the inorganic salt catalyst.
  • inorganic salts of the inorganic salt catalyst may be incorporated into a support to form a supported inorganic salt catalyst.
  • the x-ray diffraction pattern of the individual inorganic salt may exhibit relatively narrow Dooi peaks at the same temperatures.
  • Contacting conditions may be controlled such that the total product composition (and thus, the crude product) may be varied for a given crude feed in addition to limiting and/or inhibiting formation of by-products.
  • the total product composition includes, but is not limited to, paraffins, olefins, aromatics, or mixtures thereof. These compounds make up the compositions of the crude product and the non-condensable hydrocarbon gases. Controlling contacting conditions in combination with the catalyst described herein may produce a total product with lower than predicted coke content. Comparison of the MCR content of various crudes may allow crudes to be ranked based on their tendency to form coke.
  • per gram of crude feed at most 0.2 grams, at most 0.1 grams, at most 0.05 grams, at most 0.03 grams, or at most 0.01 grams of the crude feed is converted to non-condensable hydrocarbons. In some embodiments, from 0 to 0.2 grams, 0.0001-0.1 grams, 0.001-0.05 grams, or 0.01-0.03 grams of non-condensable hydrocarbons per gram of crude feed is produced.
  • T ⁇ may be 30 °C below, 20 °C below, or 10 °C below the minimum TAP temperature and/or the minimum DSC temperature.
  • the contacting temperature may be controlled to be 370 °C, 380 °C, or 390 °C during the reaction period when the minimum TAP temperature and/or minimum DSC temperature is 400 °C.
  • the contacting temperature is controlled such that the temperature is at, or above, the catalyst TAP temperature and/or the catalyst DSC temperature.
  • the contacting temperature may be controlled to be 450 °C, 500 °C, or 550 °C during the reaction period when the minimum TAP temperature and/or minimum DSC temperature is 450 °C.
  • the ratio of hydrogen source to crude feed may also be altered to alter the properties of the crude product. For example, increasing the ratio of the hydrogen source to crude feed may result in crude product that has an increased VGO content per gram of crude product.
  • contact of the crude feed with the inorganic salt catalyst in the presence of light hydrocarbons and/or steam yields more liquid hydrocarbons and less coke in a crude product than contact of a crude feed with an inorganic salt catalyst in the presence of hydrogen and steam
  • the volume of crude product produced from a crude feed contacted with the hydrogen source in the presence of the inorganic salt catalyst is at least 5% > greater, at least 10%» greater, or at least 15%>, or at most 100%> greater than a volume of crude product produced from a
  • a stable resistance indicates an ordered structure and/or ions that tend not to move apart from one another during heating.
  • the K 2 CO 3 /Rb 2 CO 3 /Cs 2 CO 3 catalyst, Li 2 CO 3 /K 2 CO 3 /Rb 2 CO 3 /Cs2CO 3 catalyst, and Na 2 CO 3 /K 2 C ⁇ 3 /Rb 2 CO 3 /Cs 2 C ⁇ 3 catalyst show a sharp decrease in resistivity relative to K 2 CO 3 at temperatures in a range from 350-500 °C.
  • a decrease in resistivity generally indicates that current flow was detected during application of voltage to the wires embedded in the inorganic salt catalyst.
  • the crude feed had an API gravity of 6.7.
  • the crude feed had, per gram of crude feed, a sulfur content of 0.042 grams, a nitrogen content of 0.011 grams, and a total Ni/V content of 0.009 grams.
  • the crude feed was heated to 150 °C.
  • the K 2 CO 3 /Rb 2 CO 3 /Cs 2 CO 3 catalyst (31.39 grams) was charged to the reactor.
  • the K 2 CO 3 /Rb 2 CO 3 /Cs 2 CO 3 catalyst was prepared by combining of 16.44 grams of K 2 CO 3 , 19.44 grams of Rb 2 CO 3 , and 24.49 grams of Cs 2 CO 3 .
  • the K 2 C ⁇ 3 /Rb 2 CO 3 /Cs 2 CO 3 catalyst had a minimum TAP temperature of 360 °C.
  • Examples 11 and 12 provide a comparison of the use of methane as a hydrogen source to the use of hydrogen gas as a hydrogen source.
  • Methane is generally less expensive to produce and/or transport than hydrogen, thus a process that utilizes methane is desirable.
  • methane is at least as effective as hydrogen gas as a i hydrogen source when contacting a crude feed in the presence of an inorganic salt catalyst to produce a total product.
  • Example 21 86.17 grams (66.1 wt%, based on the weight of the crude feed) of a dark reddish brown hydrocarbon liquid (crude product) and water (97.5 g) were produced as a vapor from contact of the crude feed with the K 2 CO 3 /Rb2CO /Cs 2 CO 3 catalyst in the hydrogen atmosphere.
  • Example 22 water vapor and a small amount of gas was produced from the reactor. The reactor was inspected, and a dark brown viscous hydrocarbon liquid was removed from the reactor. Less than 50 wt%> of the dark brown viscous liquid was produced from contact of the crude feed with silicon carbide in the hydrogen atmosphere. A 25% increase in yield of crude product was observed in Example 21 relative to a yield of crude product produced in Example 22.

Abstract

La présente invention a trait à un procédé comprenant la mise en contact d'une charge brute avec un ou des catalyseurs menant à la production d'un produit total comportant un produit brut. La charge brute présente une teneur en résidus inférieure à 0,2 grammes de résidus par gramme de charge brute. Le produit brut est un mélange liquide à 25 °C et 0,101 MPa. Une ou des 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 d'un ou des catalyseurs avec la charge brute.
PCT/US2004/042638 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut WO2005063932A2 (fr)

Priority Applications (7)

Application Number Priority Date Filing Date Title
EA200601185A EA010396B1 (ru) 2003-12-19 2004-12-16 Неочищенный продукт процессов нефтедобычи и способ его переработки
MXPA06006741A MXPA06006741A (es) 2003-12-19 2004-12-16 Sistemas y metodos de produccion de un crudo producto.
CA002551164A CA2551164A1 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
AU2004309348A AU2004309348B2 (en) 2003-12-19 2004-12-16 Systems and methods of producing a crude product
JP2006545519A JP2007514844A (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
EP04814781A EP1702023A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
CN200480037852.2A CN1894379B (zh) 2003-12-19 2004-12-16 生产原油产品的系统和方法

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
WO2005063932A2 true WO2005063932A2 (fr) 2005-07-14
WO2005063932A3 WO2005063932A3 (fr) 2005-12-22

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Family Applications (13)

Application Number Title Priority Date Filing Date
PCT/US2004/042218 WO2005066308A2 (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/US2004/042122 WO2005066316A2 (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/US2004/042344 WO2005063928A2 (fr) 2003-12-19 2004-12-16 Systemes et procede de production d'un produit de petrole brut
PCT/US2004/042126 WO2005061664A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042638 WO2005063932A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042222 WO2005066309A2 (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/US2004/042652 WO2005063675A2 (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/US2004/042123 WO2005066304A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut
PCT/US2004/042648 WO2005061671A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production de produit brut

Family Applications Before (6)

Application Number Title Priority Date Filing Date
PCT/US2004/042218 WO2005066308A2 (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/US2004/042122 WO2005066316A2 (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/US2004/042344 WO2005063928A2 (fr) 2003-12-19 2004-12-16 Systemes et procede de production d'un produit de petrole brut
PCT/US2004/042126 WO2005061664A2 (fr) 2003-12-19 2004-12-16 Systemes et procedes de production d'un produit brut

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