EP1496099B1 - Verbessertes Isomerisierungsverfahren eines C7-Schnitts mit Öffnung der Naphtenringe - Google Patents

Verbessertes Isomerisierungsverfahren eines C7-Schnitts mit Öffnung der Naphtenringe Download PDF

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EP1496099B1
EP1496099B1 EP04291494.5A EP04291494A EP1496099B1 EP 1496099 B1 EP1496099 B1 EP 1496099B1 EP 04291494 A EP04291494 A EP 04291494A EP 1496099 B1 EP1496099 B1 EP 1496099B1
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unit
isomerization
paraffins
distillation column
stream
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French (fr)
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EP1496099A1 (de
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Laurent Bournay
Dominique Casanave
Elsa Jolimaître
Jean-Francois Joly
Paul Broutin
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IFP Energies Nouvelles IFPEN
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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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
    • C10G45/62—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing platinum group metals or compounds thereof
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline

Definitions

  • the product of the isomerization (or isomerate) is free of aromatic compounds in contrast to the reformate which usually contains a significant amount due to dehydrocyclization reactions.
  • Isomerate and reformate are usually sent to the gasoline pool in which other bases such as gasoline resulting from fluidized catalytic cracking (FCC) or additives such as methyl tertiary butyl ether (MTBE) can also be used.
  • FCC fluidized catalytic cracking
  • MTBE methyl tertiary butyl ether
  • Aromatics have high octane numbers that are suitable for use in spark-ignition engines, but for environmental reasons, increasingly stringent specifications result in reduced total aromatics content in gasolines.
  • the process described in the French patent application FR-A-2828205 relates to a process for isomerizing a C 5 -C 8 filler, the C 8+ cut of the naphtha being sent to reforming.
  • the charge C 5 -C 8 is preliminarily separated into two fractions, a first fraction rich in C 5 -C 6 and a second fraction rich in C 7 -C 8 , these two fractions being treated separately in separate reaction zones.
  • the present invention relates more particularly to the isomerization of the second C 7 -C 8 rich fraction which in practice will essentially be a C 7 cut.
  • isomers with only one branch or mono-branched have insufficient octane numbers (42 for 2-methylhexane, 52 for 3-methylhexane) to be mixed with the gasoline pool.
  • These compounds should be as much as possible converted into di- and / or tribranched paraffins in the isomerization process.
  • normal-heptane the problem is even stronger: its octane number being zero, it must imperatively be converted to exhaustion in the isomerization process. Up to 1% by weight of nC7 can be tolerated in the isomerate but if possible less than 0.5% wt.
  • the toluene present in the fresh feedstock is totally hydrogenated to methylcyclohexane either in a specific hydrogenation unit or in the paraffin isomerization unit.
  • the methyl-cyclohexane which is also present in the charge in significant amount is very little affected by the isomerization, the isomerization catalysts very little promoting the opening of naphthenic rings in their usual conditions of implementation.
  • the isomerate C 7 obtained can contain up to 30% by weight of methyl-cyclohexane: this compound whose RON is less than 75 significantly reduces the RON of this isomerization C 7 .
  • the patent US5,382,731 describes a sequence of a naphthenic ring opening reactor followed by an isomerization reactor in the presence of hydrogen and chlorine, this set of reactions being applied to a charge of 6 carbon atoms containing 50% by weight of normal hexane 14.5% by weight of methylcyclopentane, 32% by weight of cyclohexane and 3.9% by weight of benzene.
  • Licences US5,463,155 and US 5,770,042 describe a sequence of a naphthenic ring opening reactor followed by an isomerization reactor supplemented by normal separation of paraffins / isoparaffins in the patent US 5,770,042 .
  • the filler used is a naphtha defined as a petroleum fraction having from 4 to 7 carbon atoms, with a concentration of C 7 preferably limited to 20% by weight.
  • the problem which the present invention seeks to solve is that of the production of gasoline bases from a C 7 fraction which have a search octane number (RON) of at least 80, with a content of aromatic compounds limited to 1% wt, which makes it possible to anticipate the new regulation on the specifications of the gasoline pool.
  • RON search octane number
  • the solution proposed in the present invention consists of a combination of known units, namely at least one isomerization unit and at least one opening unit of the naphthenic rings, the combination having the characteristic of producing a depletion of methylcyclohexane, and normal and mono branched C 7 paraffins responsible for lowering the octane number.
  • exhaustion is meant converting said compounds by systematic recycling into an appropriate unit of the combination of units integrated in the process according to the invention, said compounds having been previously isolated in at least one separation unit.
  • the toluene present in the fresh feed is totally hydrogenated, which makes it possible to limit the aromatic content in the isomerate produced.
  • This C 7 fraction is thus composed of C 7 paraffins, approximately equally distributed in mono-branched and normal paraffins, of C 7 naphthenes, the principal representative of which is methylcyclohexane and of C 7 aromatics, of which unique representative is toluene.
  • the objective of the method which is the subject of the present invention is to transform this C 7 cut into a cut containing predominantly, that is to say at least 70% by weight, preferably at least 85% by weight, of paraffins in C 7 multi -branched, that is to say having a degree of connection greater than or equal to two.
  • the invention relates more specifically to the treatment of the 7-carbon cut and makes it possible to convert the said C 7 cut from the naphtha of first distillation into a 7-carbon cut composed of a majority of di and tribranched paraffins. that is to say containing at least 70% by weight, preferably at least 85% by weight of multi-branched paraffins.
  • the process uses at least one isomerization unit, an opening unit of the naphthenic rings and a separation step comprising at least one distillation column, possibly supplemented by a unit allowing the separation to be carried out.
  • normal and mono-paraffins on the one hand and paraffins di- and tribranched on the other hand.
  • These units are combined to recycle methylcyclohexane, toluene and normal and mono-branched paraffins until exhaustion.
  • a unit may comprise one or more reactors.
  • the present invention therefore relates to the treatment of the 7-carbon fraction resulting from the fractionation described above, but given the performance of the naphtha fractionation unit, it will be possible to find in said C 7 cut to 10% lighter compounds having 6 carbon atoms or less, and up to 10% heavier compounds having 8 or more carbon atoms.
  • the subject of the present invention is a process for producing an isomerization of RON at least equal to 80 and containing less than 1% by weight of aromatics from a cut predominantly consisting of hydrocarbons containing 7 carbon atoms, and containing of the paraffins, naphthenes and aromatics, said process comprising at least one isomerisation unit, at least one naphthenic ring opening unit and at least one separation unit, characterized in that said units are combined in such a way that recycle until exhausted methylcyclohexane, toluene and normal and mono-branched paraffins.
  • the initial section consisting mainly of hydrocarbons with 7 carbon atoms, paraffins, naphthenes and aromatics are in any proportion.
  • exhaustion is meant the conversion of methylcyclohexane, toluene and normal and mono-branched paraffins by systematic recycling into an appropriate unit of the combination of units integrated in the process according to the invention, said compounds having been previously isolated in at least a separation unit.
  • At least one of the separation units is a distillation column supplied with a mixture of different streams, at least one of which comes from the fresh feed, and from which a) a head stream is extracted which, after any further separation, gives the isomerate produced, b) a side stream, which feeds alone or in mixture one of the isomerization units, from which the normal and mono-branched paraffins are converted to exhaustion, and c) a bottom stream from which is recycled to exhaustion toluene and methylcyclohexane contained in the fresh load.
  • nC7 Up to 1% by weight of nC7 can be tolerated in the isomerate constituting the head flow but if possible less than 0.5% by weight.
  • a first isomerization unit is fed by the side withdrawal from the distillation column, the isomerization effluent, after stabilization, being returned to the distillation column on a tray above the draw plate lateral, fresh load feeds the distillation column, and the cycle opening unit is fed by the bottom flow of said column, the effluent of the ring opening unit being recycled to the inlet of the isomerization unit , in mixture with the lateral withdrawal stream from said column.
  • an isomerization unit is fed by the lateral withdrawal from the distillation column, the effluent of the isomerization after stabilization being returned to the distillation column on a plateau located above of the side withdrawal tray, the fresh feed feeds the distillation column and the cycle opening unit is fed by the bottom flow of said column, the effluent of the cycle opening unit being recycled to mixing with the fresh charge at the inlet of said column.
  • one of the isomerization units is fed by the lateral withdrawal from the distillation column, the effluent of this first isomerization after stabilization being returned to the column.
  • the fresh feed feeds a second isomerization unit distinct from the first isomerization unit, the effluent of this second isomerization unit being, after stabilization, sent as feed to the distillation column and the cycle opening unit being fed by the bottom stream of the distillation column, the effluent of the ring opening unit being recycled in admixture with the fresh feed to the entry of the second isomerization unit.
  • one of the isomerization units is fed by the lateral withdrawal from the distillation column, the effluent of this first isomerization after stabilization being returned to the column.
  • the fresh feed feeds the ring opening unit
  • the effluent of this ring opening unit feeds a second isomerization unit distinct from the first isomerization
  • the effluent of this second isomerization unit after stabilization, feeds the distillation column, the bottom flow of the distillation column feeding in mixture with the fresh charge the ring opening unit.
  • one of the isomerization units is fed by the lateral withdrawal from the distillation column, the effluent of this first isomerization after stabilization being returned to the distillation column on a plate located above the lateral withdrawal tray, the fresh feed feeds the distillation column, and the bottom flow of the distillation column feeds the opening unit of cycles, the effluent of this unit
  • the opening of the cycles feeds a second isomerization unit distinct from the first isomerization, the effluent of this second isomerization, after stabilization, feeds the distillation column in a mixture with the fresh feedstock.
  • the overhead stream of the distillation column is sent to a separation unit from which the normal and mono-paraffins which are recycled either at the inlet of the column, on the one hand, are extracted on the one hand.
  • the separation unit used may be based on any technique known to those skilled in the art, for example a molecular sieve adsorption unit such as that described in the patent application. US2002 / 0045793 A1 .
  • the adsorbent used in said unit may be any adsorbent known to those skilled in the art to make this separation, for example the adsorbents described in the patent US 6,353,144 , the patent application FR 02/09841 (Non-homogeneous adsorbent consisting of at least one crystal formed of a core and a continuous outer layer having a diffusional selectivity greater than 5) and the patent application US2002 / 0045793 A1 . It is also conceivable to use one or more membrane modules for this separation, as described for example in the patent application. EP-A1-0192274 .
  • the distillation column may optionally be of the type column-inner wall (divided-wall column in English terminology), which is a technology that applies well in case one has a side racking.
  • one of the separation units involved is supplied with a mixture of different streams, at least one of which comes from the fresh feedstock, and this separation unit is extracted from a feedstock.
  • the normal and mono-paraffins which are recycled at the inlet of an isomerisation unit, and secondly a stream rich in di- and tribranched paraffins and naphthenic which feeds a distillation column which is extracted a) a flow of head which is the isomerate produced, and b) a bottom stream from which the toluene and methylcyclohexane contained in the fresh feed are exhaustively recycled.
  • nC7 can be tolerated in the isomerate constituting the head flow but if possible less than 0.5% by weight.
  • the fresh feed feeds an isomerization unit, the isomerization effluent, after stabilization, feeds the separation unit from which on the one hand the normal and mono are extracted.
  • paraffins which are recycled to the input of the isomerization unit, mixed with the fresh feed, and secondly a rich flow of di- and tribranched paraffins and naphthenic rings which feeds the distillation column, the top flow of which constitutes the isomerate, and whose naphthenic rich bottom stream is fed to the ring opening unit, the effluent of which is recycled to the inlet of the isomerization unit in admixture with the fresh feed and the feedstock. recycle from the separation unit.
  • the fresh feed feeds after stabilization, the separation unit from which are extracted on the one hand the normal and mono-paraffins which are recycled to the input of an isomerization unit and on the other hand, a stream rich in di- and tribranched paraffins and in naphthenic rings which feeds the distillation column, the top flow of which constitutes the isomerate, and whose rich naphthenic bottom flow is fed into the feed.
  • a ring opening unit the effluent of which is recycled mixed with the fresh feedstock and the effluent of the isomerization unit at the inlet of the stabilization.
  • the fresh feed feeds a unit for opening cycles
  • the effluent of said unit feeds an isomerization unit
  • the effluent of the isomerization unit after stabilization feeds the separation unit from which are extracted on the one hand the normal and mono-paraffins which are recycled to the input of the isomerization unit mixed with the effluent of the ring-opening unit, and on the other hand, a stream rich in di- and tribranched paraffins and in naphthenic rings which feeds the distillation column, the top flow of which constitutes the isomerate, and whose rich naphthenic bottom stream is recycled in charge of the daphthenic unit. opening cycles in mixture with the fresh load.
  • one of the separation units involved is a distillation column fed by a mixture of different streams, at least one of which is derived from the fresh feed, from which a flow is extracted.
  • head which feeds a second separation unit which is extracted on the one hand normal and mono-paraffins which are recycled to the input of one of the isomerization units, and secondly a rich flow of di and tribranched paraffins which is the isomerate produced, and b) a bottom stream from which the toluene and methylcyclohexane contained in the fresh feed are exhaustively recycled.
  • the fresh feed feeds an isomerization unit, the isomerization effluent, after stabilization, feeds the distillation column whose feed stream feeds the separation unit of which one extracts on the one hand the normal and mono-paraffins which are recycled at the input of the isomerization unit, mixed with the fresh feedstock, and on the other hand a stream rich in di- and tribranched paraffins which constitutes the isomerate, the bottom stream of the naphthenic rich distillation column is fed to a ring opening unit whose effluent is recycled to the inlet of the isomerization unit in admixture with the fresh feedstock and the recycle from the separation unit.
  • the fresh feed feeds a unit of opening of cycles
  • the effluent of said unit feeds an isomerization unit
  • the effluent of this isomerization unit after stabilization , feeds the distillation column whose head flow feeds the separation unit from which one extracts on the one hand the normal and mono-paraffins which are recycled to the input of the isomerisation unit, in mixing with the effluent of the ring opening unit and secondly a rich flow of di- and tribranched paraffins which constitutes the isomerate, the bottom flow of the column is recycled in charge of the unit of opening of cycles mixed with fresh feed.
  • the fresh feed feeds a unit for opening cycles, the effluent of said unit, after stabilization, feeds the distillation column, the feed of which feeds the feed unit. separation from which are extracted on the one hand the normal and mono-paraffins which are sent as input to a first isomerization unit whose effluent is recycled to the stabilization inlet mixed with the effluent of the opening unit of cycles and on the other hand a flow rich in di- and tribranched paraffins which constitutes the isomerate, the bottom flow of the column feeds a second isomerization unit, whose effluent is recycled in charge of the unit of opening of cycles mixed with fresh feed.
  • the term "rich" stream is understood to mean a stream whose weight composition is such that said compound represents at least 50% by weight, preferably at least 65% by weight and even more preferably at least 80% by weight of the total composition.
  • the hydrogenation of toluene can be carried out in a specific hydrogenation unit. This unit can be placed to process the entire fresh feed, or to process only the feed of the ring opening unit or one of the isomerization units.
  • the charge to be treated (1) is introduced into a distillation column (A) comprising 88 actual trays at the plateau 50.
  • the fresh batch (1) has in the example considered the following composition (in% by weight) and a mass flow rate given below:% by weight dimethyl 2-3 butane 0.01 2-methyl pentane 0.10 methyl-3 pentane 0.14 n-hexane 1.41 methyl-cyclopentane 0.79 cyclohexane 1.64 benzene 0.18 trimethyl 2-2-3 butane 0.06 dimethyl 2-2 pentane 0.15 dimethyl 2-3 pentane 3.66 dimethyl 2-4 pentane 0.42 dimethyl 3-3 pentane 0.24 2-methyl hexane 9.39 3-methyl hexane 12.68 ethyl-3 pentane 1.16 n-heptane 31,20 1,1-dimethylcyclopentane 0.89 cis-dimethyl-1,3 cyclopentane 2.40 1,
  • a flow (2) which corresponds to the product isomerate and whose weight composition and mass flow rate are as follows: isopentane 4.23 dimethyl 2-2 butane 0.22 dimethyl 2-3 butane 0.18 2-methyl pentane 0.83 methyl-3 pentane 0.53 n-hexane 2.21 methyl-cyclopentane 0.97 cyclohexane 1.93 benzene 0.18 trimethyl 2-2-3 butane 8.12 dimethyl 2-2 pentane 22.04 dimethyl 2-3 pentane 0.88 dimethyl 2-4 pentane 47,23 dimethyl 3-3 pentane 3.07 2-methyl hexane 4.34 3-methyl hexane 1.79 ethyl-3 pentane 0.06 n-heptane 0.50 1,1-dimethylcyclopentane 0.20 cis-dimethyl-1,3 cyclopentane 0.08 1,3-trans-1,3-dimethylcyclopentane 0.07 1,2-trans-1,
  • the RON of this isomerate (stream 2) is 84.2 and its aromatic content is 0.18 wt%.
  • stream (3) containing a majority (at least 70%) of normal-heptane and C 7 paraffins mono-branched.
  • a stream (4) which is a rich flow of methylcyclohexane, toluene and n-heptane.
  • This stream (4) is sent to a toluene-specific hydrogenation unit (B) and then to a ring-opening unit (C) which produces an effluent (5) containing mainly a mixture of paraffins resulting in part from the opening of the rings, as well as unconverted methyl-cyclohexane, toluene being completely hydrogenated.
  • the catalyst used for the ring opening unit may be any catalyst for ring-opening conversion of at least 5% of the methylcyclohexane present in the mixture to be treated.
  • the ring opening unit uses an iridium catalyst deposited on alumina or silica-alumina, such as that described in the patent application. WO 02/07881 .
  • the weight composition and the mass flow rate (excluding hydrogen) of the stream (5) corresponding to the effluent of the ring opening unit are as follows: C 5- 1.82 paraffins C 5 3.69 paraffins C 6 1.72 methyl-cyclopentane 0.00 cyclohexane 0.00 benzene 0.00 paraffins C 7 71.13 1,1-dimethylcyclopentane 0.39 cis-dimethyl-1,3 cyclopentane 0.37 1,3-trans-1,3-dimethylcyclopentane 0.40 1,2-trans-1,2-dimethylcyclopentane 0.40 methyl-cyclohexane 19.18 ethyl-cyclopentane 0.39 toluene 0.00 C 8+ 0.51 total flow (kg / h) 10962
  • the stream (5) is mixed with the stream (3) to give a stream (6) which is introduced into an isomerization unit (D) using a platinum catalyst on chlorinated alumina as described in the application patent US2002 / 0002319 A1 .
  • the weight composition and the mass flow rate (excluding hydrogen) of the stream (7) corresponding to the effluent of the isomerization unit are as follows: C 5- 2.54 isopentane 0.56 dimethyl 2-2 butane 0.03 dimethyl 2-3 butane 0.02 2-methyl pentane 0.10 methyl-3 pentane 0.05 n-hexane 0.12 methyl-cyclopentane 0.04 cyclohexane 0.10 benzene 0.00 trimethyl 2-2-3 butane 1.63 dimethyl 2-2 pentane 3.26 dimethyl 2-3 pentane 4.08 dimethyl 2-4 pentane 8.16 dimethyl 3-3 pentane 4.08 2-methyl hexane 22.04 3-methyl hexane 16.32 ethyl-3 pentane 0.82 n-heptane 21,22 1,1-dimethylcyclopentane 0.33 cis-dimethyl-1,3 cyclopentane 0.32 1,3-trans-1,3-dimethylcyclopentane 0.34 1,
  • the effluent (7) of the isomerization unit is sent to a stabilization column (E) from which a flow (9) comprising the light gases resulting from the cracking reactions within the isomerization unit (C 5- cut) and bottom a flow (8) whose composition is very close to that of the flow (7) and which is reintroduced at the top of the column (A) at the plateau 12 .
  • the mass flow (excluding hydrogen) of the flow (9) amounts to 1800 kg / h.

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Claims (6)

  1. Verfahren zur Herstellung eines Isomerats mit einer RON von wenigstens gleich 80, das aus wenigstens 70 Gew.-% mehrfach verzweigten C7-Paraffinen gebildet ist und weniger als 1 Gew.-% Aromaten enthält, ausgehend von einem Schnitt, der mehrheitlich aus Kohlenwasserstoffen mit 7 Kohlenstoffatomen besteht und Paraffine, Naphtene und Aromaten enthält, wobei wenigstens eine Isomerisierungseinheit, wenigstens eine Einheit zur Öffnung der Naphthenringe und wenigstens eine Trenneinheit einbezogen sind, wobei wenigstens eine der Trenneinheiten eine Destillationssäule ist, die durch ein Gemisch aus verschiedenen Strömen gespeist wird, von denen wenigstens einer aus der frischen Charge stammt und aus dem a) ein Kopfstrom, der nach einer eventuellen zusätzlichen Trennung das Isomerat-Produkt ergibt, b) ein Seitenstrom, der allein oder in einem Gemisch eine der Isomerisierungseinheiten speist, von dem die normalen und einfach verzweigten Paraffine bis zur Erschöpfung umgewandelt werden, und c) ein Sumpfstrom, von dem das in der frischen Charge enthaltene Toluol und Methylcyclohexan bis zur Erschöpfung recycelt werden, abgezogen werden, wobei eine erste Isomerisierungseinheit durch einen aus der Destillationssäule stammenden Seitenabzug gespeist wird, wobei der Isomerisierungs-Abstrom nach der Stabilisierung auf einen über dem Seitenabzugboden befindlichen Boden zu der Destillationssäule zurückgeführt wird, wobei die frische Charge die Destillationssäule speist und wobei die Ringöffnungseinheit durch den Sumpfstrom der Säule gespeist wird, wobei der Abstrom dieser Ringöffnungseinheit entweder am Eingang der ersten Isomerisierungseinheit gemischt mit dem aus der Säule stammenden Seitenabzugstrom oder gemischt mit der frischen Charge am Eingang der Säule recycelt wird.
  2. Verfahren nach Anspruch 1, wobei der Abstrom der Ringöffnungseinheit eine zweite Isomerisierungseinheit speist, anstatt am Eingang der ersten Isomerisierungseinheit recycelt zu werden oder gemischt mit der frischen Charge am Eingang der Destillationssäule recycelt zu werden, und wobei der Abstrom der zweiten Isomerisierungseinheit nach der Stabilisierung gemischt mit der frischen Charge die Destillationssäule speist.
  3. Verfahren nach Anspruch 1 oder 2, wobei der Kopfstrom der Destillationssäule in eine Trenneinheit geleitet wird, von der einerseits die normalen und einfach verzweigten Paraffine, die entweder am Eingang der Säule gemischt mit der frischen Charge oder am Eingang der ersten Isomerisierungseinheit gemischt mit dem Seitenabzugstrom recycelt werden, und andererseits ein Strom extrahiert wird, der reich an zweifach und dreifach verzweigten Paraffinen ist.
  4. Verfahren nach einem der Ansprüche 1 bis 3, wobei die Destillationssäule vom Typ Säule mit Innenwand ist.
  5. Verfahren nach einem der Ansprüche 1 bis 4, wobei das Toluol in einer spezifischen Hydrierungseinheit hydriert wird, wobei diese Einheit derart angeordnet wird, dass entweder die Gesamtheit der frischen Charge behandelt wird, oder derart, dass nur die Charge der Ringöffnungseinheit oder einer der Isomerisierungseinheiten behandelt wird.
  6. Verfahren zur Herstellung eines Isomerats nach einem der Ansprüche 1 bis 5, wobei das Isomerat aus wenigstens 85 Gew.-% mehrfach verzweigten C7-Paraffinen gebildet ist.
EP04291494.5A 2003-07-11 2004-06-14 Verbessertes Isomerisierungsverfahren eines C7-Schnitts mit Öffnung der Naphtenringe Active EP1496099B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0308570 2003-07-11
FR0308570A FR2857371B1 (fr) 2003-07-11 2003-07-11 Procede ameliore d'isomerisation d'une coupe c7 avec ouverture des cycles naphteniques

Publications (2)

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EP1496099A1 EP1496099A1 (de) 2005-01-12
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FR2875507B1 (fr) * 2004-09-22 2008-10-31 Inst Francais Du Petrole Procede ameliore d'isomerisation d'une coupe c7 avec coproduction d'une coupe riche en molecules cycliques
US20150166438A1 (en) * 2013-12-12 2015-06-18 Uop Llc Processes and apparatuses for isomerizing hydrocarbons
FR3042190B1 (fr) * 2015-10-09 2019-12-27 IFP Energies Nouvelles Procede de production de bases essence
US11318452B2 (en) 2019-07-24 2022-05-03 Council Of Scientific & Industrial Research Single step process for the simultaneous production of aromatics, naphthenics and isoparaffins using transition metal functionalized zeolite based catalyst

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US2915571A (en) * 1957-11-13 1959-12-01 Universal Oil Prod Co Isomerization of saturated hydrocarbons
US5055633A (en) 1988-10-06 1991-10-08 Uop Adsorption and isomerization of normal and mono-methyl paraffins
US4956521A (en) * 1988-10-06 1990-09-11 Uop Adsorption and isomerization of normal and mono-methyl paraffins
US5334792A (en) * 1992-10-09 1994-08-02 Mobil Oil Corporation Combined paraffin isomerization/ring opening process for c5+naphtha
US5382731A (en) * 1993-07-22 1995-01-17 Mobil Oil Corp. Combined paraffin isomerization/ring opening process
US5463155A (en) * 1993-11-15 1995-10-31 Uop Upgrading of cyclic naphthas
FR2769622B1 (fr) * 1997-10-14 1999-12-24 Inst Francais Du Petrole Procede d'isomerisation des composes aromatiques a huit atomes de carbone
FR2771418B1 (fr) * 1997-11-25 2001-02-02 Inst Francais Du Petrole Procede de separation d'une charge c5-c8 ou d'une charge intermediaire, en trois effluents respectivement riches en paraffines lineaires, monobranchees et multibranchees
FR2828205B1 (fr) * 2001-08-06 2004-07-30 Inst Francais Du Petrole Procede d'isomerisation d'une coupe c5-c8 mettant en oeuvre deux reacteurs en parallele

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FR2857371A1 (fr) 2005-01-14
EP1496099A1 (de) 2005-01-12
US20050043576A1 (en) 2005-02-24
US7273958B2 (en) 2007-09-25
FR2857371B1 (fr) 2007-08-24

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