EP1558702A2 - Procede pour reorganiser des dispositifs de reformage catalytique a lit fixe - Google Patents

Procede pour reorganiser des dispositifs de reformage catalytique a lit fixe

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Publication number
EP1558702A2
EP1558702A2 EP03777914A EP03777914A EP1558702A2 EP 1558702 A2 EP1558702 A2 EP 1558702A2 EP 03777914 A EP03777914 A EP 03777914A EP 03777914 A EP03777914 A EP 03777914A EP 1558702 A2 EP1558702 A2 EP 1558702A2
Authority
EP
European Patent Office
Prior art keywords
catalyst
reactor
bed
moving
fixed
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP03777914A
Other languages
German (de)
English (en)
Inventor
Stuart Scott Goldstein
John Harland Thurtell
John Werner Viets
Tomas R. Melli
Jason Robert Vollbracht
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ExxonMobil Technology and Engineering Co
Original Assignee
ExxonMobil Research and Engineering Co
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 ExxonMobil Research and Engineering Co filed Critical ExxonMobil Research and Engineering Co
Publication of EP1558702A2 publication Critical patent/EP1558702A2/fr
Withdrawn legal-status Critical Current

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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
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • 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
    • C10G2300/4056—Retrofitting operations
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Definitions

  • the invention relates generally to catalytic reformers. More particularly, the invention relates to an improved method for converting or revamping high pressure, fixed-bed catalytic reformers to catalytic reformers with continuous, moving-bed reactors.
  • Catalytic reforming is an established refinery process. It is used for improving the octane quality of hydrocarbon feeds.
  • reforming refers to the total effect of molecular changes, or hydrocarbon reactions on the hydrocarbon feed, produced by a number of reactions.
  • Typical reforming reactions include dehydrogenation of cyclohexanes, dehydroisomerization of alky ley clo- pentanes, dehydrocyclization of paraffins and olefins, isomerization of substituted aromatics, and hydrocracking of paraffins.
  • Typical reforming catalysts are multifunctional catalysts having a hydrogenation-dehydrogenation component dispersed on a porous, inorganic oxide support. The support may typically also contain an acid functionality needed for the reforming reactions.
  • Reforming reactions are both endothermic and exothermic. Endothermic reactions are typically predominant in the early stages of reforming. Exothermic reactions are predominant in the later reaction stages.
  • a reforming unit typically comprises a plurality of serially connected reactors with furnaces for supplying additional heat to the reaction stream as it passes from one reactor to the next in order to compensate for the heat taken up in the overall endothermic character of the process.
  • reforming processes have been operated as semiregenerative or cyclic processes using fixed bed reactors or continuous processes using moving bed reactors.
  • Proposals have also been made for combining fixed and moving bed reactors with the regeneration mode being appropriate to the reactor types used in the hybrid configuration, so that the fixed bed reactors have retained the fixed bed type regeneration, usually semiregenerative, and the moving bed reactors in the unit have retained the dedicated moving bed regenerator.
  • Units of this hybrid type are disclosed, for example, in US 5,190,638; US 5,190,639; US 5,5,196,110; US 5,5,211,838; US 5,5,221,463; US 5,354,451; US 5,368,720 and US 5,417,843.
  • the unit described in US 5,417,843 uses two trains of fixed bed reactors with each train having a final moving bed reactor at the end and the moving bed reactors sharing a moving bed regenerator.
  • the entire reforming process unit is operated by gradually and progressively increasing the temperature to compensate for deactivation of the catalyst caused by coke deposition, until finally the entire unit is shut-down for regeneration and reactivation of the catalyst which is carried out with the catalyst remaining in the reactor cases.
  • the reactors are individually isolated by various piping arrangements. The catalyst is regenerated and then reactivated while the other reactors of the series remain on line. A "swing reactor” temporarily replaces the reactor which is removed from the series for regeneration and reactivation of the catalyst, which is then put back in the series.
  • the reactors are moving-bed reactors with continuous or intermittent addition and withdrawal of catalyst through which the catalyst moves progressively before it is passed to a regeneration zone for regeneration and rejuvenation before being returned once again to the reactor.
  • the regenerator In the regenerator, at least a portion of the deposited coke is burned off and the regenerated catalyst is recycled to the reactor to continue the cycle.
  • Commercial continuous reforming units may have the reactors arranged in a side-by-side or in a stacked configuration. Because the continuous mode of operation with its frequent regeneration can tolerate a higher degree of coke lay-down on the catalyst, it is possible to operate continuous units at lower pressures than those normally used with semi-regenerative and cyclic units in which it is important or at least desirable to extend catalyst life between successive regenerations.
  • Semiregenerative reforming units may be converted to continuous moving-bed units to take advantage of the improved yield of higher octane reformate and hydrogen associated with continuous operation but the conversions which have so far been considered are essentially entire unit replacements which require replacement of all existing vessels and most of the ancillary equipment as well as installation of an integrated catalyst regenerator which is one of the most costly items in the conversion.
  • the cost of the regenerator can be as much as about 80 percent of the total cost required for the conversion.
  • the present invention relates generally to a technique for converting fixedtbed, catalytic reformer units to moving-bed catalytic reformer units.
  • the costs of conversion associated with the present conversion technique will be significantly less than existing conversions partly because the present technique makes use of existing facilities and does not require dedicated onsite continuous catalyst regeneration facilities.
  • Another advantage of the present invention is that it allows a number of existing moving-bed catalytic reformers to share a single catalyst regeneration facility, further reducing the investment required to convert several fixed-bed units.
  • the technique for converting a fixed-bed catalytic reformer unit which has at least one fixed-bed catalytic reformer reactor to a moving bed unit converts the fixed-bed catalytic reformer reactor to a moving-bed catalytic reformer reactor which allows continuous or intermittent addition of fresh or regenerated catalyst to its catalyst inlet and continuous or intermittent removal of spent catalyst from the catalyst outlet of the reactor.
  • the unit is provided with catalyst feed facilities for continuously or intermittently charging fresh or regenerated catalyst in a continuous or intermittent mode of operation to the moving-bed reactor.
  • spent catalyst recovery facilities are added for collecting the spent catalyst, storing it temporarily, and transferring it to a catalyst regeneration facility.
  • the moving- bed reactor, the catalyst feeding facilities and the catalyst recovery facilities are operatively connected between themselves and to the existing facilities (piping, ancillary equipment) of the fixed-bed unit that will not require replacement.
  • the moving-bed reactor is operated at an effective pressure to improve reformate quality and yield compared to the quality and yield from the fixed-bed unit before the conversion. It is an advantage of the present invention that the moving-bed reformer reactors of the converted unit may be operated at an effective pressure that is sufficiently low to improve substantially the reformate quality and yield as compared to the reformate quality and yield obtained from tiie fixed-bed unit before conversion.
  • the pressure is, however, maintained during normal operation at a value which is sufficiently high to allow the use of some of the existing equipment of the fixed-bed catalytic reformer unit such as compression, heat exchangers and furnaces.
  • the use of a higher pressure than typical for a fully integrated continuous reactor-regenerator is desirable in that it enables the rate of catalyst flow for regeneration to be reduced (relative to that of an integrated unit) and so relieves the burden of catalyst handling.
  • An effective operating pressure for a converted reformer unit may typically be substantially lower than the operating reactor pressure of the fixed- bed unit.
  • an effective operating pressure for the converted reformer unit may be from about 15 to about 70 percent, preferably from about 20 to about 60 percent, and more preferably from about 25 to about 50 percent lower than the operating reactor pressure of the fixed-bed unit prior to conversion.
  • the present invention may employ an offsite catalyst regeneration facility. Alternatively, it may employ a community onsite continuous catalyst regeneration facility, i.e., a continuous catalyst regenerator that is shared between more than one reactors. Also, a non-continuous onsite regeneration facility may be used for one or more catalytic reformer units.
  • a continuous regeneration facility' may be located onsite near a plurality of converted reformers. Catalyst from the continuous reactors in the reformer units may be transported to the regeneration facility and, after regeneration, be transferred back to the reformers for re-use n the reactors. Transfer from the reactors to the regenerators may be continuous ,e.g. by suitable transfer devices, for example j by conveyers, or intermittently, for example, by truck or rail car, depending on the extent of site requirements, proximity of the regenerator and other factors.
  • Another variation would be to use an onsite, non-continuous regeneration facility such as a cyclic type regenerator that can be used to regenerate catalyst from a plurality of moving-bed reformer units.
  • Figure 1 shows a continuous moving-bed reforming process built from an existing high pressure fixed-bed reformer unit. Thicker lining indicates new equipment and piping while thinner lining indicates existing equipment and piping. DETAILED DESCRIPTION
  • Non-continuous (or fixed-bed) catalytic reformers could be semiregenerative catalytic reformers, swing-reactor (also referred to as cyclic regeneration reformers) catalytic reformers or hybrid systems, all of which are known.
  • the non-continuous catalytic reformer unit may be a semiregenerative unit.
  • Semiregenerative units typically contain one or more fixed-bed reactors operating in series with inter-bed heaters to maintain operating severity as the catalyst deactivates by increasing the reaction temperature. Eventually, a semiregenerative unit is shut down for catalyst regeneration and reactivation.
  • a high pressure semiregenerative catalytic reformer can be effectively converted to operate at a lower effective reactor pressure in the reactors of the converted unit to secure substantial improvements in reformate quality and yield (relative to the semiregenerative unit prior to conversion) but which does not create an insuperable problem of catalyst handling (charge, discharge, transfer, regeneration) once conversion has taken place.
  • the present invention method allows production of reformate preferably having an octane number of from 90 to 105, more preferably from 95 to 103, and most preferably from 98 to 102.
  • an effective reactor pressure as used in the present invention, allows the use of existing facilities such as compression equipment, heat exchangers, furnaces, piping, drums and pumps.
  • This effective pressure is typically lower from the reactor pressure of typical semiregenerative units but also higher than with a typical continuous reactor where there are no similar constraints on catalyst rate created by handling consdierations. It may range from 345 to 2760 kPag (50 to 400 psig), preferably from 690 to 2620 kPag (100 to 380 psig), and more preferably from about 1035 to 2415 kPag (150 to about 350 psig).
  • the converted unit will be operated at an effective reactor pressure that provides substantially improved reformate quality and yield compared to existing fixed-bed reforming units.
  • the extent of reduction in reactor pressure may be limited, if desired, to the extent that much of the existing compression, furnace, piping, etc., equipment can be reused with the new moving-bed reactors. Limiting the extent of the pressure reduction also reduces the required catalyst circulation rate (between reactors and regeneration facilities). This is particularly attractive in a system where the spent catalyst is sent offsite for regeneration.
  • a reactor pressure reduction of from about 25 to about 50% can be realized without having to replace most of the existing facilities.
  • much larger pressure reductions may also be used where it may be attractive under some site-specific conditions to replace much of the existing facilities.
  • the fixed-bed reformer unit will converted to a moving-bed reformer reactor that allows continuous addition of freshly regenerated catalyst to an inlet of the reactor and continuous removal of spent catalyst from an outlet of the reactor.
  • a regenerator which is shared by two or more reactor trains, e.g. the catalyst from a converted unit is regenerated in the regenerator of a second reformer unit in which the regenerator is integrated with the (second) reactor train but not with the first reactor train, i.e. the regenerator for the converted unit is a non-dedicated regenerator.
  • a shared regenerator may be fully integrated with one reactor train but constructed so that it has the capacity to regenerate the catalyst from two or more reactors.
  • the non- integrated reactors may be on-site (same refinery plant) or at remote sites. In this way, the substantial capital cost of the regenerator is proportionately reduced because of the economies of scale associated with regeneration facilities.
  • the conversion of a fixed bed (semiregenerative or cyclic) reformer unit to operation with moving-bed reactors may include the replacement or conversion of at least one fixed-bed reactor and preferably all of the fixed bed reactors in the unit to moving-bed reactors.
  • the catalyst facilities of the converted unit and the continuous moving-bed reactors will be operatively connected with existing plant equipment, as necessary.
  • the moving bed reactors may be disposed in a side-by-side or stacked arrangement, depending on site requirements.
  • the conversion does require addition of catalyst loading, recovery (unloading) and transfer facilities associated with the interface between the continuous reactor(s) and the regeneration facilities which have been selected, that is, off-site, non-integrated on-site or partly integrated (shared regenerator) regeneration.
  • the spent catalyst recovered from the reforming unit may be collected and transferred to on offsite regeneration facility.
  • the catalyst may be recovered in a continuous manner.
  • the spent catalyst that exits the last reactor will be collected in a spent catalyst storage container and then transferred in smaller batches to drums or special containers suitable for transportation to an offsite regeneration facility.
  • the catalyst may be collected in storage devices (drums, containers, vessels) and transferred to the regeneration facility.
  • the facilities for collecting and transferring the spent catalyst may differ.
  • they could be as simple as a dump nozzle at the bottom of the last reactor emptying into conventional 200 litre (55 US gallon) drums.
  • they could include specially designed trucks, rail cars, or shipping containers capable of maintaining an inert atmosphere during loading, transportation and unloading.
  • the catalyst regeneration facility can be an offsite or an onsite facility preferably centrally located if site conditions permit. In most cases the regeneration facility will preferably be independent and only indirectly associated with a particular reforming unit although the shared regenerator configuration may be possible and even desirable in certain circumstances. Independent regeneration facilities will thus operate autonomously from any particular reforming unit and may regenerate catalyst from one or more reforming units. This will allow for increased operational flexibility for the reforming units as well as the regeneration facility, lower investment cost (on unit basis) and improved reformate product. According to this embodiment a centrally located catalyst regeneration facility receives spent catalyst from a plurality of moving-bed reformers continuously or intermittently and supplies the reactors of these units continuously or intermittently with regenerated catalyst.
  • Any typical reforming catalyst may be used, including those comprising one or more Group VIII noble metals on a refractory support.
  • the catalyst will contain a hydrogenation-dehydrogenation function (hydrogen transfer) and an acid function. Examples include catalysts comprising platinum, tin, rhenium, iridium, tin or combinations of these metals.
  • a preferred support includes substantially spherical alumina support particles.
  • a preferred catalyst comprises platinum, platinum and tin, or platinum and rhenium on substantially spherical alumina support particles. Spherical particles are preferred for movement through the moving bed reactors and other equipment with minimal attrition.
  • Any type of regeneration facilities may be used.
  • One preferred regeneration facility may include a continuous moving-bed regeneration tower characteristic of commercially available continuous reforming processes or it may include a batch regeneration process unit.
  • One example of a batch regeneration process is the Hot Flue Gas Regeneration Circuit characteristic of Cyclic POWERFORMINGTM.
  • Another example is a shut down semiregenerative unit used exclusively for catalyst regeneration.
  • a suitable regeneration procedure may include a hydrocarbon purge, coke burn, oxy-chlorination, oxides purge, and reduction procedure. However, depending on the type of catalyst it may also include presulfiding as part of the regeneration procedure. It may be preferable to complete the reduction and presulfiding (if necessary) after the regenerated catalyst has been returned from the offsite regeneration facility immediately before feeding the regenerated catalyst to the top of the lead reactor.
  • the oxy-chlorination procedure may vary significantly. At a minimum it may include the addition of a chloride containing agent such as Cl 2 , HC1, or a pumpable organic chloride after the coke burn to replace the chloride lost during the coke burn.
  • the coke burn may also include a continuous addition of a chloride agent during the coke burn. It may also include over-chlorination after the coke burn followed by a chloride equilibration step after the platinum metal has been thoroughly redispersed. The actual regeneration procedure might include any combination of these chlorination techniques.
  • Figure 1 shows a continuous catalytic moving-bed reforming process unit 10. This unit is built from an existing high pressure semiregenerative reformer unit by removing the fixed bed reactor cases and installing moving bed cases which are deployed in a side-by-side arrangement. If site requirements, for example, limited area, dictate, a stacked reactor configuration could well be used with a consequent reduction in catalyst transfer equipment as the lift pots and transfer lines shown in Figure 1 could simply be replaced by gravity trickle from one reactor to the next reactor in the train.
  • thicker lining indicates new equipment and piping while thinner lining indicates existing equipment and piping.
  • the conversion includes replacing each semiregenerative reactor (not shown) with a new moving-bed reactor 27, 57, 65, installing a fresh/regenerated catalyst loading platform 18, a fresh catalyst storage drum 20 which can be fed with fresh/regenerated catalyst through line 11 with feed controlled by valve 13.
  • Other newly added items include spent catalyst storage drums 71 and 73, intra- unit catalyst transfer equipment including collectors 24, 54, 64, lift pots 31, 61, 69 and transfer lines 53, 58, 59, a spent catalyst loading platform 24, dust filters 26, a N2 cooler 28, a N2 circulator 30, make-up nitrogen supply 32 and a H2 preheater 34.
  • Fresh catalyst or regenerated catalyst from the offsite regeneration facility is placed on loading platform 18 and added to the regenerated catalyst .storage drum 20.
  • the catalyst then enters the lock hopper 17 where it is purged with nitrogen from line 15 to remove residual air.
  • the catalyst is then transferred to the lift engager 19 where it is lifted with hydrogen gas fed through line 19 and valve 21 to reduction/purge/ disengaging chamber 12 on top of first reactor 27 by way of transfer line 52.
  • Gas is removed from hopper 12 in elutriation tube 12 and passes through line 43 to dust filters (new) 26.
  • Reduced catalyst is added to the first reactor 27 via catalyst flow lines 37.
  • Catalyst moves by gravity downwards in reactor 27 until it exits through lines 41 and enters catalyst collector 24 which is fed with hydrogen rich gas through line 39.
  • Catalyst from catalyst collector 24 then enters lift engager 31 where it is lifted with a H2 rich stream to disengaging hopper 55. Lift gas is admitted through valve/inlet 33. The catalyst enters the second disengaging hopper 44 atop second reactor 57 after which it enters reactor 57 where it moves downward to the outlet and passes into catalyst collector 54, followed by lift engager 61. Catalyst from lift engager 61 is then lifted with a hydrogen rich gas to disengaging hopper 16 atop third and last reactor 65 from which it then passes to the inlet of the third and last reactor 65. Catalyst flows downward through reactor 65 to collector 64 and then to lift engager 69.
  • Catalyst from lift engager 69 is lifted with a hydrogen rich gas to disengaging/storage drum 71 in which gas is separated from the catalyst and passes through elutriation tube 22 to dust filter 26.
  • the spent catalyst is then transferred to lock hopper 73 where it is purged with nitrogen and finally loaded into the shipping containers on Spent Catalyst Loading Platform 24.
  • the reformer charge enters the unit at inlet 85 and passes through line
  • Nitrogen for purge is introduced through make up inlet 32 and passes to the nitrogen loop via knock out drum 45 and then through line 51 to lift engager 17 with nitrogen also being introduced into lock hopper 23 through line 15. Gas from the reactors passes through the dust filters 26 to nitrogen cooler 28 before returning to the nitrogen loop through knock out drum 45.
  • Figure 1 does not depict the actual offsite or centrally located on-site regeneration facilities. Several different designs for these regeneration facilities may be used. A preferred design is likely to vary based on the actual project specifics. Options for offsite regeneration systems may include:
  • Variations of the present method may include:
  • the facility may be sized to regenerate catalyst from other units that may also be converted;
  • Table 1 presents results of a feasibility study to evaluate the unit of
  • Reactor pressure is reduced about 25 percent, from 3344 to 2482 kPag (485 to 360 psig) despite an increase in feed rate from 4,770 to 5,406 m 3 /day (30 to 34 kbd). This reduction in reactor pressure allows the refiner to maintain a relatively constant C5+ reformate yield despite a severity increase from 95 to
  • Catalyst regeneration facilities may be used to regenerate spent catalyst from more than one reformer, thus achieving economies of scale and (2) to achieve somewhat more modest pressure reductions and yield improvements, but at a significantly lower project investment than existing conversions with dedicated continuous catalyst regeneration facilities.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Catalysts (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

La présente invention concerne un procédé pour convertir une unité de reformage catalytique à lit fixe en une unité à lit mobile. Le réacteur à lit fixe est converti en un réacteur à lit mobile qui comprend des installations d'apport continu ou intermittent de catalyseur pour permettre l'introduction continue ou intermittente de catalyseur frais ou régénéré par l'entrée de catalyseur du réacteur à lit mobile, et l'extraction continue ou intermittente de catalyseur usagé par la sortie de catalyseur du réacteur à lit mobile. Le catalyseur usagé extrait du réacteur est régénéré dans un dispositif de régénération non intégré qui peut être un dispositif de régénération extérieur, un dispositif de régénération sur site centralisé qui alimente différentes unités de reformage ou un dispositif de régénération partagé avec une seconde unité à lit mobile. Le réacteur à lit mobile, les installations d'alimentation en catalyseur et les installations en récupération de catalyseur sont reliés, d'un point de vue fonctionnel, entre eux et à des installations existantes de l'unité à lit fixe, telles qu'un système de traitement et chauffage de charge de reformage, canalisation et compression. On fait fonctionner l'unité convertie à une pression de réacteur efficace pour améliorer la qualité du reformat et son rendement par rapport au produit de reformat de l'unité à lit fixe avec conversion.
EP03777914A 2002-10-29 2003-10-24 Procede pour reorganiser des dispositifs de reformage catalytique a lit fixe Withdrawn EP1558702A2 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
US42189202P 2002-10-29 2002-10-29
US421892P 2002-10-29
US10/690,801 US20040129605A1 (en) 2002-10-29 2003-10-22 Method for revamping fixed-bed catalytic reformers
US690801 2003-10-22
PCT/US2003/034041 WO2004039720A2 (fr) 2002-10-29 2003-10-24 Procede pour reorganiser des dispositifs de reformage catalytique a lit fixe

Publications (1)

Publication Number Publication Date
EP1558702A2 true EP1558702A2 (fr) 2005-08-03

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EP03777914A Withdrawn EP1558702A2 (fr) 2002-10-29 2003-10-24 Procede pour reorganiser des dispositifs de reformage catalytique a lit fixe

Country Status (6)

Country Link
US (1) US20040129605A1 (fr)
EP (1) EP1558702A2 (fr)
JP (1) JP2006515798A (fr)
AU (1) AU2003286704A1 (fr)
CA (1) CA2504224A1 (fr)
WO (1) WO2004039720A2 (fr)

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US20040129605A1 (en) 2004-07-08
CA2504224A1 (fr) 2004-05-13
WO2004039720A3 (fr) 2004-07-01
WO2004039720A2 (fr) 2004-05-13
AU2003286704A1 (en) 2004-05-25
JP2006515798A (ja) 2006-06-08

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