WO2004104142A1 - Process to upgrade kerosenes and a gasoils from naphthenic and aromatic crude petroleum sources - Google Patents
Process to upgrade kerosenes and a gasoils from naphthenic and aromatic crude petroleum sources Download PDFInfo
- Publication number
- WO2004104142A1 WO2004104142A1 PCT/EP2004/050819 EP2004050819W WO2004104142A1 WO 2004104142 A1 WO2004104142 A1 WO 2004104142A1 EP 2004050819 W EP2004050819 W EP 2004050819W WO 2004104142 A1 WO2004104142 A1 WO 2004104142A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- fraction
- kerosene
- petroleum
- gas oil
- crude
- Prior art date
Links
- 239000003208 petroleum Substances 0.000 title claims abstract description 39
- 238000000034 method Methods 0.000 title claims abstract description 29
- 125000003118 aryl group Chemical group 0.000 title description 13
- 239000003350 kerosene Substances 0.000 claims abstract description 52
- 239000000203 mixture Substances 0.000 claims abstract description 21
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 claims abstract description 19
- 239000000779 smoke Substances 0.000 claims abstract description 12
- 238000012512 characterization method Methods 0.000 claims abstract description 10
- 150000002790 naphthalenes Chemical class 0.000 claims abstract description 8
- 238000002955 isolation Methods 0.000 claims abstract description 3
- 239000011369 resultant mixture Substances 0.000 claims abstract description 3
- 238000004821 distillation Methods 0.000 claims description 10
- 238000009835 boiling Methods 0.000 claims description 6
- 239000012188 paraffin wax Substances 0.000 claims 2
- 239000003209 petroleum derivative Substances 0.000 claims 1
- 239000003921 oil Substances 0.000 description 31
- 239000007789 gas Substances 0.000 description 30
- 238000002156 mixing Methods 0.000 description 17
- 239000000446 fuel Substances 0.000 description 12
- 239000002283 diesel fuel Substances 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 239000008186 active pharmaceutical agent Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000003502 gasoline Substances 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 238000007142 ring opening reaction Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000002199 base oil Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000012432 intermediate storage Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 230000001050 lubricating effect Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- VYQNWZOUAUKGHI-UHFFFAOYSA-N monobenzone Chemical compound C1=CC(O)=CC=C1OCC1=CC=CC=C1 VYQNWZOUAUKGHI-UHFFFAOYSA-N 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
Classifications
-
- 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
- C10L1/08—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
-
- 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
Definitions
- Crude petroleum sources featuring a value for the Watson characterisation factor K of in between 11 and 12 are also referred to as “naphthenic" crude. If the K factor below 11 the crude is also referred to as
- Virgin naphtha fractions as distilled from Napthenic or Aromatic crudes are very suitable to prepare high octane motor gasoline components as they are easy convertable via Catalytic Reforming to high octane value reformates .
- virgin kerosenes and virgin gasoils produced from Naphthenic and/or Aromatic crudes are being characterised by certain quality properties which makes them unsuitable to meet certain environmentally driven fuels specifications as required by an increasing number of legislators in various Regions and Markets.
- Aviation kerosenes produced from naphthenic and/or aromatic crudes by distillation and treating will typically have a smoke point far below the required international specifica ion (min. 25 mm) set for Aviation Turbine Fuels (Avtur) in Checklist No. 19 of Aviation Fuel Quality Requirements for Jointly Operated Systems (AFQRJOS) , or does not meet the alternative specification of maximum smokepoint (min. 19 mm) if naphthalenes content of the kerosene is below 3 %vol. Sometimes naphthalenes levels are too high in kerosenes produced from these crudes in case of high final boiling points of the kerosenes.
- Diesel quality gasoils produced from such naphthenic or aromatic crudes will typically feature a low cetane number (CN) .
- the cetane number will be between 35-50 below the required international Cetane number specifications set for Diesel grades.
- the minimum Cetane Number requirement in the European Diesel specification (EN 590) has been increased to minimum of 51 from year 2000 onwards to meet the European Diesel fuel and emissions requirements set in the EU Fuels Directive 98/70 for Euro III fuels.
- European Diesel specification EN 590
- EU Fuels Directive 98/70 for Euro III fuels.
- Global car manufacturers want to increase Diesel fuel Cetane Number requirements even further to minimum 55 as published in their World Wide Fuel Charter in year 2002.
- US-A-3775297 describes a process wherein the gas oil fraction as isolated from a naphthenic crude is converted into a lubricating base oil and a motor gasoline. More recent developments as illustrated in
- a second option to improve the kerosene and gas oil properties is to blend and co-process these inferior quality types of naphthenic and aromatic crudes with more paraffinic type of crudes.
- the final distillate yields of this crude blend can be calculated from the crude blend ratio multiplied by the distillate yields obtainable for each crude.
- a disadvantage of blending with paraffinic crudes is that such crudes are not always available at the refinery location or only at a much higher price.
- Another disadvantage is, that it is not always possible to find a paraffinic crude to blend which will meet both kerosene and gas oil properties and volume demands of distillates to the qualities respectively quantities as specified.
- quality giveaway for example it is either the kerosene blend or the gas oil blend which will meet the smoke point respectively the cetane number specification after blending such crudes.
- the other blend will have a property value exceeding the specification while the property value of said blend will be the same or near a blend having a property closer to the specification.
- quality give away is preferably to be avoided for obvious reasons. Nevertheless, as explained above, when optimizing both kerosene and gas oil products in a refinery blending environment such quality give-away cannot always be avoided.
- Co-processing of a paraffinic crude will also result in more crude storage and handling, blending, crude distilling and processing requirements.
- the object of the present invention is to obtain a process to prepare kerosene and gas oil from a naphthenic or aromatic crude wherein the product quality give away is being reduced and wherein special measures to reduce the naphthenic or aromatic hydrocarbon contents is not required.
- the process according to the invention provides a simple method to obtain kerosene and gas oil products having desired properties while avoiding the need to coprocessing a paraffinic crude.
- Fischer-Tropsch products as blending components also facilitates the use of virgin kerosene and gas oil distilled from a naphthenic or aromatic crude type. This will thus reduce the need or even avoid hydroprocessing steps, which are normally applied to reduce the naphthenic or aromatics contents in these fractions.
- the petroleum crude source feature a value of the Watson characterisation factor K of equal or below 12.0. These K values are being calculated according to formulae and nomograms described in the API Technical Data Book
- the petroleum derived fraction of the gas oil and kerosene products as obtained from the process according to the invention are for more than 50 wt%, more preferably more than 70 wt% and most preferably more than 90 wt% based on a crude having a K value equal or below 12.0.
- a petroleum derived kerosene and gas oil is isolated, preferably by distillation. Such distillation is preferably carried out in an atmospheric distillation column by well known processes for the person skilled in refinery operations.
- the fractions isolated by distillation and which have not been subjected to another conversion process are referred to as virgin distillate fractions.
- the petroleum derived kerosene fraction will preferably have an ASTM D 86 distillation IBP of between 140 and 200 °C and a final boiling point of between 200 and max 300 °C.
- the petroleum derived gas oil fraction should preferably have an ASTM D 86 IBP of between 250 and 300 °C and a FBP of between 340 and 380 °C.
- Fischer-Tropsch derived kerosene and gas oil fractions are suitably obtained from the (hydrocracked) Fischer-Tropsch synthesis product.
- Fischer- Tropsch derived kerosene and gas oils are described in EP-A-583836, WO-A-9714768, WO-A-9714769, WO-A-011116, WO-A-011117, WO-A-0183406, WO-A-0183648, WO-A-0183647, WO-A-0183641, WO-A-0020535, WO-A-0020534, EP-A-1101813, US-A-5766274, US-A-5378348, US-A-5888376 and US-A-6204426.
- the Fischer-Tropsch derived kerosene will consist of at least 90 wt%, more preferably at least 95 wt% of iso and linear paraffins.
- the weight ratio of iso-paraffins to normal paraffins will suitably be greater than 0.3. This ratio may be up to 12. Suitably this ratio is between 2 and 6. The actual value for this ratio will be determined, in part, by the hydroconversion process used to prepare the Fischer-Tropsch derived kerosene or gas oil from the Fischer-Tropsch synthesis product. Some cyclic-paraffins may be present.
- the Fischer-Tropsch derived kerosene will suitably have a smoke point of higher than 25 mm and preferably above 50 mm and the ASTM D 86 distillation curve which will for its majority be within the typical kerosene range: between about 150 and 200 °C, a density of about
- the Fischer-Tropsch derived gas oil will consist of at least 90 wt%, more preferably at least 95 wt% of iso and linear paraffins.
- the weight ratio of iso-paraffins to normal paraffins will suitably be greater than 0.3. This ratio may be up to 12. Suitably this ratio is between 2 and 6. The actual value for this ratio will be determined, in part, by the hydroconversion process used to prepare the Fischer-Tropsch derived kerosene or gas oil from the Fischer-Tropsch synthesis product. Some cyclic-paraffins may be present.
- the Fischer-Tropsch derived gas oil will suitably have a cetane number of higher than 60 and preferably above 70 and an ASTM D 86 distillation curve which will for its majority be within the typical gas oil range: between about 200 and 400 °C.
- the Fischer-Tropsch gas oil will suitably have a T90 %vol of between 300-400 °C, a density of between about 0.76 and 0.79 g/cm 3 at 15 °C, and a viscosity between about 2.5 and 4.0 centistokes at 40 °C.
- Blending can either be performed by so-called in-line blending, on-line blending or batch blending. This depends on the level of automation.
- in batch blending the petroleum derived fraction and the Fischer-Tropsch derived fraction are first mixed and subsequently supplied to a storage vessel and than supplied to a ship, rail or road car or other means of transport of the final blend.
- the desired product quality, i.e. smoke point or cetane number, of the feed to the storage vessel is measured and the quantity of the blending components is adjusted such that the property value is maintained within a pre-determined range in order to minimise quality give-away.
- Example 1 The invention will be illustrated with the following non-limiting examples. The Examples are based on calculations using known blending rules.
- Example 1 is based on calculations using known blending rules.
- a naphthenic crude having a UOPK value of 11.5 is distilled into a naphtha fraction, a kerosene fraction and a gas oil fraction.
- the properties of the different fractions are listed in Table 1.
- Example 1 is repeated.
- an paraffinic crude having a Watson K characterisation factor value of 12.3 was distilled to obtain blending components to improve the kerosene and gas oil properties of the fractions listed in Table 1.
- the amount of paraffinic crude that was used was enough to obtain a kerosene and gas oil mixture to adjust the respective fraction of Table 1 to meet the desired specification.
- the properties of the blends are reported in Table 2.
- Table 2 Distillates properties of Paraffinic and Naphthenic crudes and blend
- Example 1 is repeated. To the kerosene and gas oil fractions of Table 1 an amount of Fischer-Tropsch kerosene and gas oil (having the properties as listed in Table 3) respectively is added in an amount sufficient to meet the smoke point and cetane number specifications. The resulting properties are listed in Table 4.
Landscapes
- 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)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Fats And Perfumes (AREA)
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP04741581A EP1627028B1 (en) | 2003-05-22 | 2004-05-17 | Process to upgrade kerosenes and a gasoils from naphthenic and aromatic crude petroleum sources |
JP2006530200A JP5478806B2 (en) | 2003-05-22 | 2004-05-17 | A method for improving the quality of kerosene and gas oil from naphthenic and aromatic crudes. |
DE602004010648T DE602004010648T2 (en) | 2003-05-22 | 2004-05-17 | METHOD FOR THE EVALUATION OF CEROSINE AND GAS OIL CUTS FROM RAW OIL |
DK04741581T DK1627028T3 (en) | 2003-05-22 | 2004-05-17 | Process for upgrading petroleum types and gas oils from naphthenic and aromatic petroleum sources |
US10/557,870 US20070021636A1 (en) | 2003-05-22 | 2004-05-17 | Process to upgrade kerosenes and a gasoils from naphthenic and aromatic crude petroleum sources |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP03076566 | 2003-05-22 | ||
EP03076566.3 | 2003-05-22 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2004104142A1 true WO2004104142A1 (en) | 2004-12-02 |
Family
ID=33462163
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2004/050819 WO2004104142A1 (en) | 2003-05-22 | 2004-05-17 | Process to upgrade kerosenes and a gasoils from naphthenic and aromatic crude petroleum sources |
Country Status (8)
Country | Link |
---|---|
US (1) | US20070021636A1 (en) |
EP (1) | EP1627028B1 (en) |
JP (1) | JP5478806B2 (en) |
CN (1) | CN100362085C (en) |
AT (1) | ATE380855T1 (en) |
DE (1) | DE602004010648T2 (en) |
DK (1) | DK1627028T3 (en) |
WO (1) | WO2004104142A1 (en) |
Cited By (21)
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WO2006108839A1 (en) * | 2005-04-11 | 2006-10-19 | Shell Internationale Research Maatschappij B.V. | Process to blend a mineral and a fischer-tropsch derived product onboard a marine vessel |
WO2007039460A1 (en) * | 2005-09-21 | 2007-04-12 | Shell Internationale Research Maatschappij B.V. | Process to blend a mineral derived hydrocarbon product and a fisher-tropsch derived hydrocarbon product |
WO2007071747A1 (en) * | 2005-12-22 | 2007-06-28 | Shell Internationale Research Maatschappij B.V. | Fuel composition |
WO2007110448A1 (en) * | 2006-03-29 | 2007-10-04 | Shell Internationale Research Maatschappij B.V. | Process to prepare an aviation fuel and an automotive gas oil |
WO2007113967A1 (en) * | 2006-03-30 | 2007-10-11 | Nippon Oil Corporation | Method for treatment of synthetic oil, process for production of hydrocarbon oil, hydrocarbon oil for hydrogen production, hydrocarbon oil for the smoke point improver for kerosene, and hydrocarbon oil for diesel fuel base |
JP2007269899A (en) * | 2006-03-30 | 2007-10-18 | Nippon Oil Corp | Method for treating synthetic oil, hydrocarbon oil for improving agent of smoke point of kerosene and hydrocarbon oil for base material of diesel fuel |
JP2007269901A (en) * | 2006-03-30 | 2007-10-18 | Nippon Oil Corp | Method for treating synthetic oil, hydrocarbon oil for producing hydrogen and hydrocarbon oil for base material of diesel fuel |
WO2008124607A1 (en) * | 2007-04-06 | 2008-10-16 | Syntroleum Corporation | Process for co-producing jet fuel and lpg from renewable sources |
US7666294B2 (en) | 2003-09-17 | 2010-02-23 | Shell Oil Company | Depressed freeze point kerosene fuel compositions and methods of making and using same |
US7968757B2 (en) | 2008-08-21 | 2011-06-28 | Syntroleum Corporation | Hydrocracking process for biological feedstocks and hydrocarbons produced therefrom |
US8026401B2 (en) | 2007-12-20 | 2011-09-27 | Syntroleum Corporation | Hydrodeoxygenation process |
US8058484B2 (en) | 2007-08-24 | 2011-11-15 | Syntroleum Corporation | Flexible glycerol conversion process |
US8231804B2 (en) | 2008-12-10 | 2012-07-31 | Syntroleum Corporation | Even carbon number paraffin composition and method of manufacturing same |
US8536390B2 (en) | 2010-03-18 | 2013-09-17 | Syntroleum Corporation, A Delaware Corporation | Profitable method for carbon capture and storage |
US8558042B2 (en) | 2008-06-04 | 2013-10-15 | Syntroleum Corporation | Biorenewable naphtha |
US8575409B2 (en) | 2007-12-20 | 2013-11-05 | Syntroleum Corporation | Method for the removal of phosphorus |
US8969259B2 (en) | 2013-04-05 | 2015-03-03 | Reg Synthetic Fuels, Llc | Bio-based synthetic fluids |
US9133080B2 (en) | 2008-06-04 | 2015-09-15 | Reg Synthetic Fuels, Llc | Biorenewable naphtha |
US9328303B2 (en) | 2013-03-13 | 2016-05-03 | Reg Synthetic Fuels, Llc | Reducing pressure drop buildup in bio-oil hydroprocessing reactors |
WO2017081199A1 (en) | 2015-11-11 | 2017-05-18 | Shell Internationale Research Maatschappij B.V. | Process for preparing a diesel fuel composition |
US12049434B2 (en) | 2023-03-07 | 2024-07-30 | Reg Synthetic Fuels, Llc | Even carbon number paraffin composition and method of manufacturing same |
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US20100116711A1 (en) * | 2008-11-12 | 2010-05-13 | Kellogg Brown & Root Llc | Systems and Methods for Producing N-Paraffins From Low Value Feedstocks |
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WO2018077976A1 (en) * | 2016-10-27 | 2018-05-03 | Shell Internationale Research Maatschappij B.V. | Process for preparing an automotive gasoil |
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US11248176B2 (en) | 2019-08-28 | 2022-02-15 | Saudi Arabian Oil Company | Low-sulfur aromatic-rich fuel oil blending component |
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US6180842B1 (en) * | 1998-08-21 | 2001-01-30 | Exxon Research And Engineering Company | Stability fischer-tropsch diesel fuel and a process for its production |
WO2001083648A2 (en) * | 2000-05-02 | 2001-11-08 | Exxonmobil Research And Engineering Company | Low emissions f-t fuel/cracked stock blends |
US20020104779A1 (en) * | 2000-02-14 | 2002-08-08 | Connor Daniel Stedman | Synthetic jet fuel and diesel fuel compositions and processes |
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- 2004-05-17 AT AT04741581T patent/ATE380855T1/en not_active IP Right Cessation
- 2004-05-17 JP JP2006530200A patent/JP5478806B2/en not_active Expired - Lifetime
- 2004-05-17 EP EP04741581A patent/EP1627028B1/en not_active Expired - Lifetime
- 2004-05-17 CN CNB2004800140603A patent/CN100362085C/en not_active Expired - Lifetime
- 2004-05-17 DK DK04741581T patent/DK1627028T3/en active
- 2004-05-17 US US10/557,870 patent/US20070021636A1/en not_active Abandoned
- 2004-05-17 DE DE602004010648T patent/DE602004010648T2/en not_active Expired - Lifetime
- 2004-05-17 WO PCT/EP2004/050819 patent/WO2004104142A1/en active IP Right Grant
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EP1664249B1 (en) * | 2003-09-17 | 2012-11-28 | Shell Internationale Research Maatschappij B.V. | Petroleum- and fischer-tropsch- derived kerosene blend |
US7666294B2 (en) | 2003-09-17 | 2010-02-23 | Shell Oil Company | Depressed freeze point kerosene fuel compositions and methods of making and using same |
WO2006108839A1 (en) * | 2005-04-11 | 2006-10-19 | Shell Internationale Research Maatschappij B.V. | Process to blend a mineral and a fischer-tropsch derived product onboard a marine vessel |
JP2008535990A (en) * | 2005-04-11 | 2008-09-04 | シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ | Method for blending mineral and Fischer-Tropsch derived products on a ship |
US7837853B2 (en) | 2005-04-11 | 2010-11-23 | Shell Oil Company | Process to blend a mineral and a Fischer-Tropsch derived product onboard a marine vessel |
WO2007039460A1 (en) * | 2005-09-21 | 2007-04-12 | Shell Internationale Research Maatschappij B.V. | Process to blend a mineral derived hydrocarbon product and a fisher-tropsch derived hydrocarbon product |
US7867377B2 (en) | 2005-12-22 | 2011-01-11 | Shell Oil Company | Fuel composition |
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Publication number | Publication date |
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EP1627028A1 (en) | 2006-02-22 |
US20070021636A1 (en) | 2007-01-25 |
ATE380855T1 (en) | 2007-12-15 |
JP5478806B2 (en) | 2014-04-23 |
JP2007502899A (en) | 2007-02-15 |
DE602004010648D1 (en) | 2008-01-24 |
DK1627028T3 (en) | 2008-03-17 |
CN100362085C (en) | 2008-01-16 |
CN1795258A (en) | 2006-06-28 |
EP1627028B1 (en) | 2007-12-12 |
DE602004010648T2 (en) | 2008-12-11 |
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