EP1448749B1 - Verfahren zur umwandlung in serien-reaktoren - Google Patents

Verfahren zur umwandlung in serien-reaktoren Download PDF

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Publication number
EP1448749B1
EP1448749B1 EP02790546A EP02790546A EP1448749B1 EP 1448749 B1 EP1448749 B1 EP 1448749B1 EP 02790546 A EP02790546 A EP 02790546A EP 02790546 A EP02790546 A EP 02790546A EP 1448749 B1 EP1448749 B1 EP 1448749B1
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EP
European Patent Office
Prior art keywords
reactor
reactors
catalyst
suspension
process according
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EP02790546A
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English (en)
French (fr)
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EP1448749A1 (de
Inventor
Ari Minkkinen
Reynald Bonneau
Alexandre Rojey
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IFP Energies Nouvelles IFPEN
Eni SpA
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IFP Energies Nouvelles IFPEN
Eni SpA
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Priority claimed from FR0115023A external-priority patent/FR2832415B1/fr
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • 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
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts 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
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C10G2/34—Apparatus, reactors
    • C10G2/342—Apparatus, reactors with moving solid catalysts

Definitions

  • Fischer-Tropsch liquid fuels offers significant prospects for the exploitation of gas deposits far from major markets. These developments are conditioned by the need to reduce costs and especially investment costs to improve the profitability of this sector.
  • One way to achieve this goal is to play on a scale factor to reduce investment costs per tonne of liquid product obtained.
  • Such triphasic reactors comprising a catalyst in suspension in a solvent generally inert in the reaction. They are usually called slurry reactors.
  • slurry reactors There are notably well-agitated autoclave-type reactors, or even bubble-column type reactors which operate in variable hydrodynamic conditions ranging from the perfectly stirred reactor to the reactor operated in piston mode without dispersion, this for both the gas phase and the liquid phase.
  • patents US 5,961,933 and US 6,060,524 describe a method and apparatus for operating a bubble-column type slurry reactor for Fischer-Tropsch synthesis.
  • the slurry reactor comprises an internal or external recirculation system of the liquid, which makes it possible to achieve higher productivities for each Fischer-Tropsch reactor.
  • the patent application WO 01/00595 describes a process for synthesizing hydrocarbons from synthesis gas in a three-phase reactor, preferably of the bubble column type, and wherein the hydrodynamic conditions of the liquid phase are such that the number of Peclet of the liquid phase is greater than at 0 and lower than 10. Furthermore, the superficial gas velocity is preferably less than 35 cm.s-1.
  • the patent EP-B-450 860 discloses a method for optimally operating a three-phase reactor of the bubble column type. This patent seeks to optimize the operation of a single reactor of this type. it is stated that the performance depends essentially on the dispersion of the gas phase (number of Peclet for the gas phase) and the suspension maintenance of the catalyst in the liquid phase. In particular, the number of Peclet for the gas phase must imperatively be greater than 0.2. Thus, this patent recommends not to use a substantially perfectly stirred reactor with respect to the gas phase (number of gas Peclet close to 0), because this type of reactor leads to insufficient performance levels.
  • Requirement EP 0 823 470 A1 describes a Fischer-Tropsch process using a piston flow for both the suspension and the gas phase.
  • the reactors are therefore not perfectly agitated, or substantially perfectly agitated.
  • the patent GB-615,381 describes a synthesis gas conversion process in a multi-stage reactor, supplemented with fresh catalyst at the top stage, but it is a two-phase gas / solid reactor.
  • the method according to the invention aims to overcome these problems by combining at least two triphasic reactors, preferably at least three triphasic reactors. It has indeed been observed that the use of highly mixed reactors in series makes it possible to obtain a correct progress of the reaction, while promoting the evacuation of calories. This sequence makes it possible to achieve high productivities in the desired products, that is to say essentially paraffins having essentially a carbon number greater than 5, preferably greater than 10, while limiting the formation of light products (C1-C4 hydrocarbons).
  • the invention relates to a process for the synthesis of hydrocarbons preferably having at least 2 carbon atoms in their molecule and more preferably at least 5 carbon atoms in their molecule by contacting a gas containing essentially monoxide of carbon and hydrogen and in a reaction zone containing a suspension of solid particles in a liquid, which comprises solid particles of catalyst of the reaction. Said catalytic suspension is also called slurry.
  • the process according to the invention is therefore carried out in a three-phase reactor.
  • the process according to the invention will be carried out in a three-phase reactor of the bubble column type.
  • the process according to the invention according to claim 1 is a process for converting a synthesis gas into liquid hydrocarbons used in at least two reactors in series, preferably at least three reactors in series containing at least one catalyst in series. suspension in a liquid phase, wherein said reactors are perfectly mixed, the last reactor is at least partly supplied with at least a portion of at least one of the gaseous fractions collected at the outlet of at least one of said reactors, and the product mixture in liquid phase and catalyst leaving at least one reactor is at least partly separated so as to obtain a substantially catalyst-free liquid product and a catalyst-enriched liquid fraction (catalyst-enriched catalyst suspension, or catalytic suspension concentrated), which is recycled to the last reactor. More precisely, the invention proposes a method according to claim 1. The method according to the invention can in particular be implemented in an installation according to the figure 8 . However, it is described below, and in Figures 1 to 7 technical elements useful for understanding the claimed invention, these elements may belong to the state of the art.
  • Each of the reactors used is a reactor of the bubble column type, with contacting of the gas with a liquid / solid mixture very divided ("slurry” reactor or “slurry bubble column” according to the English terminology)
  • the catalysts used can be of various kinds and usually contain at least one metal preferably selected from the metals of groups 5 to 11 of the new periodic table of elements.
  • the catalyst may contain at least one activating agent (also called promoter) preferably chosen from the elements of groups 1 to 7 of the new periodic classification. These promoters can be used alone or in combination.
  • the support is generally a porous material and often a porous inorganic refractory oxide.
  • this support may be chosen from the group formed by alumina, silica, titanium oxide, zirconia, rare earths or mixtures of at least two of these porous mineral oxides.
  • the suspension may contain from 10 to 65% by weight of catalyst.
  • the catalyst particles have a mean diameter most often between about 10 and about 100 microns. Finer particles may be produced by attrition, ie by fragmentation of the initial catalyst particles.
  • each of the reactors is strongly mixed and approaches the conditions of perfect mixing.
  • the reactors according to the invention are therefore defined as being substantially perfectly stirred and the number of Peclet can be advantageously used as a criterion for measuring the degree of agitation of said reactors.
  • the piston-dispersion model can be applied to the liquid phase because it is well suited to continuous phases.
  • the mixing effect in the gaseous phase will be increased if said gaseous phase is finely dispersed, in gas bubbles with a diameter not exceeding, for example, a few millimeters. Such a condition is also favorable to the kinetics of reaction.
  • reactors in series at least two, but preferably at least three, are used. This further allows and this is another object of the present invention, to stagger the injection of synthesis gas. In this way it is possible to optimize the configuration of the reactors in series.
  • the maximum diameter of a reactor is generally limited for reasons of road construction and transport. This diameter may be for example 11 m. In this case, to maximize the production capacity, it is advantageous to use reactors of the same diameter and this can be achieved by adjusting the amount of synthesis gas sent to each of the reactors.
  • Each of the reactors is operated at a temperature preferably between 180 ° C and 370 ° C, preferably between 180 ° C and 320 ° C, more preferably between 200 ° C and 250 ° C, and at a pressure preferably between 1 and 5 MPa (megapascal), preferably between 1 and 3 MPa.
  • the process according to the invention is a process for converting a synthesis gas into liquid hydrocarbons used in at least two reactors in series containing at least one catalyst in suspension in a liquid phase, in which said reactors are substantially fully mixed, the last reactor is at least partly supplied with at least a portion of at least one of the gaseous fractions collected at the outlet of at least one of said reactors, and the mixture of liquid phase product and catalyst leaving at least one reactor is at least partially separated so as to obtain a substantially catalyst-free liquid product and a catalyst-enriched liquid fraction, which is recycled to the last reactor.
  • the process according to the invention preferably comprises at least 3 reactors in series.
  • the number of liquid Peclet is preferably less than 8, and independently the number of Peclet gas is preferably less than 0.2 and more preferably less than 0.1.
  • the gaseous phase is separated from the liquid phase containing the catalyst in suspension. More preferably, the gaseous fractions leaving the first reactors are combined, treated and sent to the inlet of the last reactor and very preferably, the gaseous fraction leaving the last reactor is recycled to the input of the production step. of synthesis gas.
  • the introduction of synthesis gas is distributed to the inlet of the reactors in series so that all the reactors are of identical size.
  • the catalyst of the process according to the invention is preferably formed of a porous mineral support and at least one metal deposited on this support.
  • the catalyst is preferably suspended in the liquid phase in the form of particles with a diameter preferably of less than 200 microns.
  • the synthesis gas arrives via line 100. It is sent to the first reactor R1, in which it is dispersed within the liquid phase formed by the reaction products which are recycled. At the outlet of this first reactor R1, the mixture of liquid product formed containing the catalyst in suspension (catalytic suspension) and the unreacted gas is discharged through line 101, in the form of a dispersed phase. Through line 102 a second supply of synthesis gas is introduced and the resulting mixture is sent through line 103 to the second reactor R2. At the outlet of this second reactor R2, the liquid product mixture containing the suspension catalyst and the unreacted gas in the form of a dispersed phase are discharged through line 104.
  • the conduit 106 Via the conduit 106 is introduced a third supply of synthesis gas and the resulting mixture is sent through the conduit 107 to the third reactor R3.
  • the mixture of liquid product containing the suspended catalyst and the unreacted gas in the form of a dispersed phase is discharged through line 108.
  • the gas phase is separated from the liquid phase in the SL separator. This gaseous phase is discharged through line 111, treated and recycled.
  • the liquid phase containing the catalyst in suspension (catalytic suspension) is sent to the separation and filtration system SC.
  • the liquid phase separated from the catalyst is discharged through line 110 while the concentrated liquid phase catalyst (concentrated catalytic suspension) is recycled via line 109 to the first reactor R1.
  • intermediate separations may optionally be carried out.
  • the residual gaseous fractions are separated at the outlet of each of the reactors by means of the separators SL1, SL2 and SL3.
  • the separators SL1, SL2, SL3 operate for example by decantation, providing a residence time in the separation tank sufficient.
  • the gaseous fractions thus collected by the conduits 111, 112 and 113 are combined, treated and recycled.
  • the gaseous fractions collected by the conduits 111, 112 and 113 contain water, carbon dioxide, light hydrocarbons and a mixture of carbon monoxide and hydrogen. It is advantageous to send the oxide mixture of carbon and hydrogen collected at the outlet of a reactor to the next reactor (not shown).
  • the gaseous phase is sent to a treatment section T1, so as to separate at least part of the carbon dioxide that it contains.
  • the gaseous fraction rich in carbon dioxide, which is thus separated, is discharged via line 117.
  • the treatment section T1 can use the various known methods for separating carbon dioxide. For example, a washing method with a solvent, such as for example an amine, or a physical solvent such as refrigerated methanol, propylene carbonate or tetraethylene glycol dimethyl ether (DMETEG) can be used. Any other method based on, for example, adsorption separation or selective membrane separation may also be used.
  • the gaseous mixture obtained, which is discharged from the treatment unit T1 through line 106 is enriched with carbon monoxide and hydrogen.
  • the synthesis gas is sent to the first reactor R1 via line 100.
  • the gaseous phase and the liquid phase are separated in separator SL1.
  • the gas phase leaving the separator SL1 is cooled in the exchanger C1. This refrigeration leads to the condensation of an aqueous phase and the evacuation of this condensed phase through the conduit 210, moreover a condensed phase of light hydrocarbons is evacuated via the conduit 211.
  • the resulting gas phase is discharged through the conduit. 113 and sent to the reactor R2, being mixed at the inlet of the reactor R2 with an addition of synthesis gas arriving via the conduit 102.
  • the gas phase and the liquid phase are separated in the separator SL2 .
  • the gas phase leaving the separator SL2 is cooled in the exchanger C2.
  • This refrigeration leads to the condensation of an aqueous phase and the evacuation of this condensed phase through the conduit 212 and also a condensed phase of light hydrocarbons which is discharged through the conduit 213.
  • the resulting gas phase is evacuated by the conduit 112 and sent to the reactor R3, with a supplement of synthesis gas arriving via the conduit 106.
  • the gaseous phase and the liquid phase are separated in the separator SL3.
  • the gas phase leaving the separator SL3 is cooled in the exchanger C3. This refrigeration leads to the condensation of an aqueous phase and the evacuation of this condensed phase through the conduit 213; in addition, a condensed phase of light hydrocarbons is evacuated via line 214.
  • the separators SL1, SL2 and SL3 are shown as distinct from the reactors R1, R2 and R3.
  • the gas phase leaving each reactor could, alternatively, be separated from the liquid phase containing the catalyst in suspension in the reactor itself, the liquid phase containing the catalyst can then be removed under control level.
  • This example describes a usable mode of circulation of the catalyst between the various reactors.
  • the figure 5 presents the corresponding diagram.
  • the catalyst introduced at the base of each reactor is distributed homogeneously throughout the liquid phase occupying the reactor.
  • the unconverted gaseous fraction disengages at the top of each reactor and the liquid phase containing the catalyst in suspension (catalytic suspension) flows overflow and flows to the base of the next reactor by simple gravity.
  • the transfer lines passing from one reactor to the next reactor must be designed to have the smoothest possible slope.
  • the liquid phase collected at the outlet of the last reactor is at least partially separated from the catalyst it contains and filtered. It is then discharged through line 110.
  • the catalyst which remains in suspension in a residual liquid phase (concentrated catalytic suspension) is recycled with this liquid phase to the first reactor by the line shown in dashed lines.
  • Such a circulation mode can also be implemented in cases where separating devices and in particular disengaging the gas phase are used at the outlet of each of the reactors as illustrated in Examples 2, 3 and 4. .
  • FIGS. 6 and 7 present two circulation arrangement schemes for use in the process according to the invention or in other methods of the state of the art.
  • These reactors comprise an internal exchanger, for example consisting of preferably tubular cooling beams.
  • These arrangement schemes are usable according to the invention, but the invention is not related to this or these uses.
  • reactors have a supply and an outlet, the water entering through line 1 and the generated steam exiting through line 2.
  • a system for dispersing the charge 4 is also disposed inside the reactor. It can be a distributor plate of the gaseous feedstock (synthesis gas) fed by line 3.
  • the supply of liquid comprising the catalyst in suspension can optionally be carried out by the same line, the gas / liquid / solid mixture being produced upstream, like this is the case on Figures 6 and 7 . It is also possible to use separate power supplies, only the gas feeding the dispersion system 4. In the figure 7 internal recirculation is favored by the design of the reactor.
  • the figure 8 more particularly represents a mode of arrangement of reactors according to the invention of claim 1 with particular circulation of the catalyst.
  • the plant comprises two (first) reactors R1, R2 operating in parallel with synthesis gas supplied by lines 100 and 102, and a reactor R3 operating in series with R1, R2, using the gas non-converted residual synthesis from reactors R1 and R2 by lines 101 and 104.
  • This residual synthesis gas, or first stage is (advantageously) treated in unit S1, to substantially eliminate water, and possibly the carbon dioxide before supplying the reactor R3 via line 112.
  • the section S1 can thus correspond to the equipment C1 and S4 of the figure 3 , possibly with the addition of the processing section T1 represented in this same figure.
  • the particular layout of the installation of the figure 8 compared to the installation of the figure 3 relates to the circulation of the catalyst, that is to say the catalytic suspension of at least one solid catalyst in a liquid phase typically composed of products of the reaction.
  • This catalytic suspension circulates at least partly countercurrently between the different reactors, a catalytic suspension stream circulating from the last reactor R3 (last with respect to the circulation of synthesis gas) to a first reactor R2 via line 221.
  • Another catalytic suspension stream flows from the reactor R2 to the reactor R1 via the line 222.
  • a third catalytic suspension stream flows from the reactor R1 to the reactor R3, via the line 223, the separation section SC, then the line 109 in FIG. which circulates a catalytic suspension (relatively more) concentrated, a stream of purified liquid having been discharged through the line 110.
  • the reactor R1 is not fed by a catalytic suspension from R2, but by a catalytic suspension from R3, flowing in the beginning of the line 221 and in the dotted line 224, the flow of Catalytic suspension discharged from the reactor R2 is, in this alternative, sent to the section SC via the line 222, then the dashed line 225, then the line 223.
  • a suspension stream circulates (directly, that is to say without crossing a separation section) of the (or a) last reactor R3, to a previous or first reactor R1 or R2 (relative to to the circulation of the synthesis gas), and a relatively concentrated suspension stream, from a separation section SC, feeds the last reactor or R3.
  • the synthesis gas is depleted in reagents (H2 / CO) in the reactors R1, R2, and enriched in inerts produced by the reaction, in particular methane. Therefore, because of these two phenomena, the partial pressure of reagents (H2 / CO) is significantly lower in the (or a) last reactor R3 than in a previous or first reactor R1, R2.
  • the use of a relatively higher catalytic concentration in the (or a) last reactor makes it possible to compensate for the influence of this lower partial pressure and to be able to maintain a high conversion in the last step.
  • the mass percentage of catalyst may for example be between 20 and 35% by weight, especially between 25 and 32% by weight in the first reactors R1, R2.
  • the mass percentage of catalyst may be multiplied by a factor K of between 1.03 and 1.25, in particular between 1.06 and 1.20 and for example between 1.08 and 1.18 with respect to (x) percentage (s) of one (or more) first reactors R1, R2.
  • At least one reactor (R1, R2, or R3) is fed (typically directly, that is to say without intermediate fractionation of the type of a liquid separation / catalytic suspension) by a catalytic suspension stream from another reactor.
  • an installation for implementing the method according to the invention (according to the configuration of the figure 8 ), at least one reactor is fed with a catalytic suspension stream directly from another reactor, and at least one catalytic suspension stream from a reactor is at least partly separated to obtain a substantially free liquid product of catalyst and catalytic suspension catalyst-enriched (concentrated), which is recycled.
  • Each of the reactors is in communication with at least one other reactor, via a suspension stream sent directly to this other reactor or coming directly from this reactor.
  • the catalyst-enriched catalyst suspension is recycled to the last reactor (for example R3), so as to enrich the catalytic suspension of the latter reactor relative to that of the other reactors, by example of one or more reactors (R1, R2).
  • the method may in particular comprise a first reaction stage carried out in several first reactors operating in parallel, in which the gaseous fractions leaving these first reactors are combined, treated and sent to the inlet of a last reactor.
  • the conversion carried out in the first reactors can be determined so that all the reactors are of identical size.
  • first reactors or “last reactor (s)” may be different, for example between 1 and 8.
  • the number of reaction steps may be between 1 and 5.
  • the reactors R1, R2 , R3 previously described may be replaced by reaction zones, possibly integrated in a smaller number of reactors etc ...
  • This example presents a material balance illustrating the possible use of several reactors substantially perfectly mixed in a synthesis gas conversion process, and shows the relevance of this technical option.
  • a flow rate of 713t / h of synthesis gas is obtained, the molar composition of which is as follows: Water : 0.004 Hydrogen : 0.672 CO : 0.311 Methane : 0.013
  • the process used comprises 3 reactors R1, R2, R3 substantially perfectly mixed and having the Peclet numbers between 0.02 and 0.03.
  • the reactor R1 operates at a temperature of 236 ° C.
  • 200.66 t / h of liquid products are collected via the conduit, comprising 87% of mole fraction of constituents, the molecule of which comprises at least 10 carbon atoms.
  • 234 t / h of water (conduit 210), 67 t / h of condensed hydrocarbons (conduit 211) and 347 t / h of synthesis gas are recovered at a pressure of 2.8 MPa , which is sent to the reactor R2 via the conduit 113 being mixed with 327 t / h of synthesis gas arriving via the conduit 102.
  • the overall conversion yield is 91%.

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  • Chemical & Material Sciences (AREA)
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  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
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  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Claims (10)

  1. Verfahren zum Umwandeln eines Synthesegases in flüssige Kohlenwasserstoffe, das in mindestens zwei Reaktoren in Serie, die eine katalytische Suspension aus mindestens einem festen Katalysator in Suspension in einer flüssigen Phase enthalten, ausgeführt wird, bei dem die Reaktoren im Wesentlichen vollkommen durchmischt werden, der letzte Reaktor zumindest teilweise von mindestens einem Teil mindestens einer der Gasfraktionen gespeist wird, die am Auslass von mindestens einem der anderen Reaktoren aufgefangen werden, mindestens ein Reaktor von einem Strom einer katalytischen Suspension gespeist wird, der direkt von einem anderen Reaktor kommt, mindestens ein Strom einer katalytischen Suspension, der von einem Reaktor kommt, zumindest teilweise entmischt wird, um ein flüssiges Produkt, das im Wesentlichen katalysatorfrei ist, und eine katalytische Suspension, die mit Katalysator angereichert ist und rückgeführt wird, zu erhalten,
    bei dem jeder der Reaktoren mit mindestens einem weiteren Reaktor in Verbindung ist, und zwar über einen Suspensionsstrom, der direkt zu diesem weiteren Reaktor geschickt wird oder direkt von diesem Reaktor kommt, und bei dem die mit Katalysator angereicherte katalytische Suspension zum letzten Reaktor (R3) rückgeführt wird, um die katalytische Suspension dieses letzten Reaktors in Bezug auf jene der übrigen Reaktoren, beispielsweise eines oder mehrerer der Reaktoren (R1, R2), anzureichern.
  2. Verfahren nach Anspruch 1, das einen ersten Reaktionsschritt umfasst, der in mehreren ersten Reaktoren, die parallel arbeiten, ausgeführt wird, bei dem die Gasfraktionen, die diese ersten Reaktoren verlassen, zusammengeführt, behandelt und zum Einlass eines letzten Reaktors geschickt werden.
  3. Verfahren nach Anspruch 2, bei dem die Umwandlung, die in den ersten Reaktoren ausgeführt wird, so festgelegt ist, dass alle Reaktoren von identischer Größe sind.
  4. Verfahren nach einem der Ansprüche 1 oder 2, bei dem die Péclet-Zahl für die Flüssigkeit kleiner als 8 ist.
  5. Verfahren nach einem der Ansprüche 1 bis 4, bei dem die Péclet-Zahl des Gases kleiner als 0,2 ist.
  6. Verfahren nach einem der Ansprüche 1 bis 3, bei dem die Péclet-Zahl des Gases kleiner als 0,1 ist.
  7. Verfahren nach einem der Ansprüche 1 bis 5, bei dem am Auslass jedes Reaktors die Gasphase von der Flüssigkeitsphase, die den in Suspension befindlichen Katalysator enthält, getrennt wird.
  8. Verfahren nach einem der Ansprüche 1 bis 7, bei dem der Katalysator auf einem porösen, mineralischen Träger ausgebildet ist und mindestens ein Metall auf diesem Träger abgelagert ist, wobei der Katalysator in Form von Partikeln mit einem Durchmesser, der kleiner als 200 Mikrometer ist, in die flüssige Phase in Suspension gebracht wird.
  9. Verfahren nach einem der Ansprüche 1 bis 8, bei dem die Aufteilung des Eintrags an Synthesegas am Einlass der Reaktoren in Serie so festgelegt ist, dass die Verwendung von Reaktoren von identischer Größe möglich ist.
  10. Verfahren nach einem der Ansprüche 1 bis 9, bei dem die Gasfraktion, die den letzten Reaktor verlässt, zu einem Schritt der Produktion von Synthesegas für die Speisung der Reaktoren rückgeführt wird.
EP02790546A 2001-11-20 2002-10-28 Verfahren zur umwandlung in serien-reaktoren Expired - Fee Related EP1448749B1 (de)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
FR0115023A FR2832415B1 (fr) 2001-11-20 2001-11-20 Procede de conversion de gaz de synthese dans des reacteurs en serie
FR0115023 2001-11-20
FR0212043 2002-09-27
FR0212043A FR2832416B1 (fr) 2001-11-20 2002-09-27 Procede de conversion de gaz de synthese dans des reacteurs en serie
PCT/FR2002/003695 WO2003044127A1 (fr) 2001-11-20 2002-10-28 Procede de conversion de gaz de synthese dans des reacteurs en serie

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EP1448749A1 EP1448749A1 (de) 2004-08-25
EP1448749B1 true EP1448749B1 (de) 2008-02-27

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US (1) US6921778B2 (de)
EP (1) EP1448749B1 (de)
CN (1) CN100354392C (de)
AU (1) AU2002365951A1 (de)
CA (1) CA2466938C (de)
FR (1) FR2832416B1 (de)
NO (1) NO20042077L (de)
RU (1) RU2294913C2 (de)
WO (1) WO2003044127A1 (de)

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CA2466938C (fr) 2011-01-04
CA2466938A1 (fr) 2003-05-30
CN1612924A (zh) 2005-05-04
AU2002365951A1 (en) 2003-06-10
FR2832416B1 (fr) 2004-09-03
NO20042077L (no) 2004-05-19
US20030096881A1 (en) 2003-05-22
WO2003044127A1 (fr) 2003-05-30
RU2004118604A (ru) 2005-05-10
CN100354392C (zh) 2007-12-12
FR2832416A1 (fr) 2003-05-23
US6921778B2 (en) 2005-07-26
EP1448749A1 (de) 2004-08-25

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