EP3137583B1 - Benzinherstellungsverfahren mit einem isomerisierungsschritt gefolgt von mindestens zwei trennungsschritten - Google Patents

Benzinherstellungsverfahren mit einem isomerisierungsschritt gefolgt von mindestens zwei trennungsschritten Download PDF

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EP3137583B1
EP3137583B1 EP15719168.5A EP15719168A EP3137583B1 EP 3137583 B1 EP3137583 B1 EP 3137583B1 EP 15719168 A EP15719168 A EP 15719168A EP 3137583 B1 EP3137583 B1 EP 3137583B1
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column
separation
isomerization
enriched
section
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French (fr)
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EP3137583A1 (de
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Jérôme PIGOURIER
Isabelle Prevost
Laurent Watripont
Pierre-Yves Martin
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Axens SA
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Axens SA
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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
    • C10G61/00—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen
    • C10G61/02—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen plural serial stages only
    • 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
    • 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
    • C10G7/00—Distillation of hydrocarbon oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/104—Light gasoline having a boiling range of about 20 - 100 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2200/00—Components of fuel compositions
    • C10L2200/04—Organic compounds
    • C10L2200/0407—Specifically defined hydrocarbon fractions as obtained from, e.g. a distillation column
    • C10L2200/0415—Light distillates, e.g. LPG, naphtha
    • C10L2200/0423—Gasoline
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/543—Distillation, fractionation or rectification for separating fractions, components or impurities during preparation or upgrading of a fuel

Definitions

  • Naphtha from the atmospheric distillation of petroleum usually consists mainly of hydrocarbons comprising from 5 to 10 carbon atoms (C5-C10 cuts). These naphthas are generally divided into a light naphtha cut (C5-C6 cut) and a heavy naphtha cut (C7-C10). The heavy naphtha cut is usually sent in a catalytic reforming process.
  • the light naphtha cut which essentially comprises hydrocarbons with 5 or 6 carbon atoms (C5 and C6) but can additionally comprise hydrocarbons with 4 or 7 or even 8 carbon atoms (C4, C7, C8) is generally isomerized in order to increase the proportion of branched hydrocarbons which have a higher octane number than linear hydrocarbons.
  • the isomerate and reformate obtained are then sent to the petrol pool with other bases or additives (catalytic cracking petrol, alkylates, etc.).
  • bases or additives catalytic cracking petrol, alkylates, etc.
  • the patent FR 2 828 205 describes a process for isomerizing a C5-C8 section in which said section is divided into a C5-C6 section and a C7-C8 section which are each isomerized separately under conditions specific to each section.
  • the patent GB 1,056,517 describes a process for isomerizing a C5-C6 section comprising a deisopentanizer (DiP), isomerizing the isopentane-depleted section (ISOM), separating the isomerized effluent making it possible to recover the n-pentane (DP) which is recycled with the feedstock at the inlet of the deisopentanizer and a separation of the branched C6 hydrocarbons (deisohexanizer, DiH) making it possible to recover branched C6 hydrocarbons with a high octane number, the remainder being recycled to the isomerization reactor.
  • This DiP / ISOM / DP / DiH scheme corresponds to the figure 1 (according to the prior art of this request.
  • Naphtha from atmospheric petroleum distillation usually consists mainly of hydrocarbons containing from 5 to 10 carbon atoms (cut C5-C10).
  • the method according to the present invention treats a charge of light naphtha type and preferably a C5 and C6 cut (cut of hydrocarbons comprising 5 or 6 carbon atoms), and aims to maximize the branched molecules compared to the linear (or normal) molecules .
  • these charges may optionally include other hydrocarbons, for example hydrocarbons comprising 4 or 7, or even 8 carbon atoms (cuts C4, C7, C8).
  • it will preferably be sought to limit the amount of these hydrocarbons, for example by prior separation.
  • the method according to the invention applies more particularly to fillers whose iso pentane content is less than 25% and preferably less than 20%.
  • the method according to the invention comprises an isomerization section [1], a stabilization of the isomerized effluent [2] (denoted STAB), a separation of iso-pentane (denoted DiP), a separation of n-pentane (denoted DP), (represented by block 3 + 4) and a separation of the remaining products, in particular of branched compounds in C6 (denoted DiH) (represented by block 5), according to the sequence ISOM / ST AB / DiP / DP / DiH.
  • the separation of iso-pentane and of n-pentane can also be carried out in the same column allowing a fractionation into 3 sections according to the sequence ISOM / STAB / DiP / DiH according to the figure 4 .
  • the process according to the invention therefore differs from the process according to the prior art ( figure 1 ) in that it comprises the successive separation of iso-pentane, of n-pentane and of the branched compounds in C6 in this order according to the figure 3 , or the simultaneous separation of n-pentane and iso-pentane in the same fractionation column according to the figure 4 , followed by the separation of the C6 branched compounds, or else the separation of a C5 cut, then that of the n-pentane and of the iso-pentane and that of the C6 branched compounds according to the figure 5 .
  • said separations are all located downstream of the isomerization section [1], and more precisely downstream of the stabilization column [2], unlike the processes of the prior art which do not have only one DiH column (de-isohexanizer), or 3 fractionation columns, but with the DiP column (de-isopentanizer) located upstream of the isomerization section according to the diagram of the figure 1 .
  • the present invention can be described as a process for isomerizing a light naphtha, or preferably a substantially C5-C6 cut, said process comprising the separation steps as described in claim 1.
  • the cut enriched with iso-pentane (15) from the first separation step as well as the head (19) and bottom (18) flows from the second separation step can optionally then be mixed to provide the product (s) of the process.
  • the figures 1 shows the process diagram according to the prior art which can be considered as closest to the present invention.
  • the charge (10) is brought into a de-isopentanizer [3] which allows an isopentane flow (15) to exit at the head.
  • the bottom flow (14) of the de-isopentanizer [3] is sent to the isomerization reaction section [1] via line 14.
  • the operating conditions of the reaction section [1] are chosen so as to promote the transformation of n-paraffins of low octane number (n-pentane, n-hexane) to iso-paraffins of higher octane numbers (isopentane, 2,2-dimethylbutane, 2,3-dimethylbutane, 2-methylpentane, 3-methylpentane).
  • the isomerization reaction section [1] is generally carried out in the presence of an acid catalyst.
  • the effluent from the isomerization section [1], once stabilized by separation of the light compounds (13) in the stabilization column [2] is directed via the line (12) to a de-pentanizer [4].
  • the head flow (16) of the de-pentanizer [4] is recycled to the column [3] of the de-isopentanizer.
  • the flux (16) can be recycled to the de-isopentanizer [3], or by introducing it alone directly into the de-isopentanizer [3] (depending on the figure 1 ), or mixed with the load 10 (not shown).
  • the stream (16) also contains isopentane formed in the isomerization section which is separated in the de-isopentanizer [3].
  • the products (18) and (19) originate respectively from the bottom and from the head of the de-isohexanizer [5] which is supplied by the bottom flow (17) from the de-pentanizer [4]. Isopentane is substantially absent from these two flows, being essentially present in flow 15.
  • the process of figure 1 has the drawback of mixing a fluid enriched in isopentane recycled via line (16) with the load (10) coming from line 10, either before its admission into the de-isopentanizer [3], or, as shown in the figure 1 , inside said de-isopentanizer [3].
  • a second p e eta separation [5], which is performed by means of a die-isohexaniseur consisting of a separation column with the overhead product (19) is rich in branched C6 compounds, and including an intermediate section (20 ) enriched in n-hexane, taken by lateral racking, is recycled to the reaction section [1].
  • the stream enriched in iso-pentane (14), the bottom product (18) and the top product (19) can be mixed to constitute the product or products of the process.
  • the isomerization reaction is carried out on catalysts consisting of a high purity alumina support preferably containing 2 to 10% by weight of chlorine, 0.1 to 0.40% by weight of platinum, and optionally other metals. These catalysts are implemented with a space speed of 1 to 4 h -1 .
  • Maintaining the chlorination rate of the catalyst generally requires the continuous addition of a chlorinated compound such as carbon tetrachloride injected in mixture with the feed at a concentration ranging from 50 to 600 parts per million by weight.
  • a chlorinated compound such as carbon tetrachloride
  • the catalysts consist of a high purity alumina support containing from 2 to 10% by weight of chlorine, from 0.1 to 0.40% by weight of platinum and possibly other metals.
  • They can be implemented with a space speed between 1 to 4 h -1.
  • Maintaining the chlorination rate of the catalyst generally requires the continuous addition of a chlorinated compound such as carbon tetrachloride injected in mixture with the feed at a concentration preferably of between 50 and 600 parts per million by weight.
  • a chlorinated compound such as carbon tetrachloride
  • the charge is sent to the isomerization section [1] via line 10.
  • the conditions of the isomerization section [1] are chosen so as to favor the transformation of n-paraffins of low octane number (n-pentane, n-hexane) to iso-paraffins of octane numbers more high (isopentane, 2,2-dimethylbutane, 2,3-dimethylbutane, 2-methylpentane, 3-methylpentane).
  • the effluent from the isomerization section (11), once stabilized by separation of the light compounds in the stabilization column [2] is then directed via the line (12) to a de-isopentanizer [3] so as to recover at the head, via line (15), a stream enriched in isopentane and at the bottom via line (14) a fluid depleted in isopentane.
  • the conditions for fractionating the de-isopentanizer [3] are preferably such that the recovery rate of isopentane at the top (flow of isopentane at the top of the de-isopentanizer divided by the flow of isopentane in the charge of the de-isopentanizer ) is typically greater than 70%.
  • the content of n-pentane in the top product (15) is then typically less than 15% by weight, preferably less than 10% by weight.
  • the bottom of the de-isopentanizer [3] is directed via the line (14) to a de-pentanizer [4] so as to recover at the top (flow 16) a fluid enriched in n-pentane and containing little isopentane, which is recycled to the isomerization reaction section [1] via line (16).
  • the bottom is recovered via the pipe (17), a stream (17) containing mainly hydrocarbons with 6 or more carbon atoms (C6 + cut) which feeds the de-isohexanizer [5].
  • the de-isohexanizer [5] consists of a separation column, the top product (19) of which is rich in branched C6 compounds, and of which an intermediate section (20) enriched in n-hexane, sampled by lateral withdrawal, is recycled to the reaction section [1].
  • the stream enriched in iso-pentane (14), the bottom product of the de-isohexanizer [5], and the top product of the de-isohexanizer (19) can be mixed to constitute the product or products of the process.
  • the dimensioning of the fractionation column [4] and the fractionation conditions are preferably such that the overall recovery rate in n-pentane (flow of n-pentane at the top of de-pentanizer [4] divided by the flow of n -pentane at the outlet of the isomerization reaction section [1] is typically greater than 80%.
  • the content of hydrocarbons containing 6 or more carbon atoms at the top of the de-pentanizer [4] is typically less than 15%, preferably less than 10% by weight.
  • this first variant reduces the energy consumption of the process because the isopentane produced in the isomerization reactor [1] is vaporized only once before being exported, and the de-isopentanizer [3] splits a section C5 enriched in iC5, which facilitates said separation.
  • the effluent from the isomerization reaction section [1], once stabilized by separation of the light compounds in the stabilization column [2] is directed via line (12) to the de-pentanizer [4] of so as to recover at the head, via line (21), a cut C5 depleted in C6, and at the bottom via line (17), a fluid containing mainly hydrocarbons with 6 or more carbon atoms, which feeds the de-isohexanizer [5].
  • the second separation step in the de-isohexanizer is carried out in an identical manner to the first variant according to the invention.
  • Cut C5 feeds via line (21), the de-isopentanizer [3] which makes it possible to extract the iso-pentane (15) at the head of the column, and at the bottom the n-pentane (16) which is recycled to the reaction section [1].
  • the invention has other variants according to various thermal integrations.
  • the principle of these thermal integrations consists in choosing the operating pressure of a first column so that the condensation temperature at the top of this column is higher than the reboiling temperature of one or more other columns of the process.
  • the heat exchange between the head condenser of the first column to be cooled and the bottom reboiler of another column to be heated then replaces at least part, if not all, of the utility consumption. cold used at the head of the first column to ensure its cooling, and to the hot utility used at the bottom of the second column to ensure its heating.
  • first column and “other column” are generic since it is the choice of the column having the highest condenser temperature which defines it as the first column.
  • FIG 6 presents an example of a thermal integration mode between the de-pentanizer [4], considered as the first column and the de-isopentanizer [3] considered as the other column, according to the first variant (represented by figure 3 ) of the process according to the invention.
  • the figure 6 thus presents a heat exchange between the condenser of column [4] (depentaniser) and the reboiler of the other column [3] (de-isopentanizer).
  • Any other pair of columns could be envisaged, for example an integration between the condenser of the de-isohexanizer [5] and the reboiler of the depentanizer [4] or even between the condenser of the de-isohexanizer [5] and the reboiler of the de- isopentanizer [3] or between the condenser of the deisohexanizer [5] and the two reboilers of the depentanizer [4] and the de-isopentanizer [3].
  • One of these columns can also include an intermediate racking (fractionation column in 3 sections).
  • the first separation step comprises two columns, a de-isopentanizer [3] and a de-pentanizer [4] arranged in series, that is to say that the bottom flow (14) of the de-isopentanizer [3] feeds the de-pentanizer [4], the stream of isopentane (15) leaves at the top of the column [3], a stream enriched in heavier hydrocarbons than the pentanes (17) leaves at the bottom of the column [4] and feeds the de-isohexanizer [5], and the overhead flow (16) of the column [4] is recycled to the isomerization unit [1].
  • the first separation step comprises only a single column [3], in which the flow of isopentane (15) leaves at the top of the column [3] , the stream enriched in heavier hydrocarbons than the pentanes (17) leaving the bottom of the said column [3] feeds the column of the de-isohexanizer [5], and the intermediate withdrawal (stream 16) is recycled to the unit of isomerization [1].
  • the first separation step comprises the two columns [4] and [3] arranged in series in this order, in which the stream (12) from the column of stabilization [2] feeds the de-pentanizer [4] from which the flow (21) comes out at the head which feeds the de-isopentanizer [3], and in which the bottom flow enriched with heavier hydrocarbons than pentanes (17) of the de-pentanizer [4] feeds the de-isohexanizer [5], the de-isopentanizer [3] producing at the head the stream (15), rich in isopentane, and at the bottom the stream (16), rich in normal pentane, which is recycled to the isomerization unit [1].
  • a heat exchange is carried out between the condenser of one of the columns [3], [4] or [5] and the reboiler of one of the columns [3], [4] or [5].
  • the heat exchange is carried out between the condenser of the de-isohexanizer [5] and either the reboiler of the de-pentanizer [4], or the reboiler of the de-isopentanizer [3], either both.
  • the heat exchange is carried out between the condenser of the de-pentanizer [4] and the reboiler of the de-isopentanizer [3].
  • the reaction section consists of 2 isomerization reactors operating in series.
  • the inlet temperature of the 2 reactors is 120 ° C.
  • the inlet pressure of reactor 1 is 35 bar absolute.
  • the inlet pressure of the second reactor is 33 bar absolute.
  • the catalyst used consists of an alumina support containing 7% by weight of chlorine, and 0.23% by weight of platinum and possibly other metals.
  • the space speed is 2.2h -1 .
  • the hydrogen to hydrocarbon molar ratio is 0.1 / 1.
  • the operating pressures of the columns are chosen so that the head temperature is compatible with the usually available cooling means (cooling water or air at room temperature).
  • the pentane recycling rate is defined as the flow rate of the fluid enriched in n-pentane recycled to the isomerization reaction section divided by the flow rate of fresh feed.
  • the hexane recycling rate is defined as the flow rate of the fluid enriched in n-hexane recycled to the isomerization reaction section divided by the flow rate of fresh charge.
  • the products (or outputs) of the processes are defined as the mixture of the top products (19) and at the bottom (18) of the de-isohexanizer [5], and the top product (15) of the de-isopentanizer [3] enriched in isopentane.
  • compositions of the products obtained are summarized in Tables 2 to 4 which follow: ⁇ b> Table 2: ⁇ /b> composition of the product from stream 19 (DiH head) Figure 1 Figure 3 Figure 4 Mass flow kg / hr 21890 21855 21875 i-pentane % wt 0 0 0 n-pentane % wt 2 2 1 2,2-dimethylbutane % wt 56 58 55 2,3-dimethylbutane % wt 12 12 13 2-methyl-pentane % wt 23 22 24 2-methyl-hexane % wt 4 4 5 cycloPentane % wt 2 2 2 Figure 1 Figure 3 Figure 4 Mass flow kg / hr 3166 3166 3166 n-hexane % wt 5 5 5 methyl-cyclopentane % wt 10 10 10 cyclohexane % wt 50 51 52 C7 + % wt 35 34
  • Table 6 presents the results of a thermal integration between the de-isohexanizer [5] and the de-isopentanizer [3] and de-pentanizer [4] according to the invention.
  • the de-isohexanizer [5] is operated at a pressure of 8 bar absolute, the condensation temperature of the column head is then 127 ° C. A heat exchange is then possible between this column head and the reboiler of the de-pentanizer [4] operated at 87 ° C and the reboiler of the de-isopentanizer [3] operated at 109 ° C.
  • reaction section [1] The operating conditions of the reaction section [1] are unchanged compared to example 1.
  • the process diagram is that of figure 3 supplemented by detailed thermal integration on the figure 6 .
  • the de-pentanizer [4] is operated at a pressure of 11 bar absolute, the condensation temperature of the column head is then 123 ° C. A heat exchange is then possible between this column head and the reboiler of the isopentanizer [3] operated at 109 ° C. Table 7 details the results obtained.

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Claims (1)

  1. Verfahren zur Isomerisierung eines leichten Naphthas, wobei das Verfahren einen Reaktionsschritt zum Isomerisieren [1] umfasst, wobei der Schritt unter den folgenden Bedingungen abläuft:
    - Temperatur im Bereich zwischen 110 und 240 °C,
    - Druck von 2 bis 35 bar (1 bar = 0,1 MPa), und
    - Molverhältnis Wasserstoff/Kohlenwasserstoffe, im Bereich zwischen 0,1/1 und 1/1,
    - Raumgeschwindigkeit von 1 bis 4 h-1.
    wobei die verwendeten Katalysatoren aus einem Träger aus hochreinem Aluminiumoxid bestehen, der vorzugsweise 2 bis 10 Gew.-% Chlor, 0,1 bis 0,40 Gew.-% Platin und gegebenenfalls weitere Metalle enthält, wobei dem Isomerisierungsschritt ein Schritt [2] zur Stabilisierung der Reaktionsabströme und zwei Schritte zur destillativen Trennung des Sumpfstroms folgen, der aus dem Stabilisierungsschritt [2] stammt, der stromabwärts des Stabilisierungsschritts (2) angeordnet ist:
    1- ein erster Schritt zur destillativen Trennung (Block 3+4), um die Kohlenwasserstoffe mit 5 Kohlenstoffatomen von schwereren Verbindungen zu trennen, die zur destillativen Trennung [5] in den zweiten Abschnitt geschickt werden, wobei der erste Trennungsschritt zwei Säulen umfasst, einen Entisopentanisierer [3] und einen Entpentanisierer [4], die in Reihe angeordnet sind, das heißt, dass der Sumpfstrom (14) des Entisopentanisierers [3] dem Entpentanisierer [4] zugeführt wird, der Isopentanstrom (15) tritt am Kopf der Säule [3] aus, ein mit Kohlenwasserstoffen angereicherter Strom, der schwerer als die Pentane (17) ist, tritt am Boden der Säule [4] aus und wird dem Entisohexanisierer [5] zugeführt, und der Kopfstrom (16) aus der Säule [4] wird in die Isomerisierungseinheit [1] zurückgeführt, wobei sie die 3 folgenden Schnitte erzeugen: a) einen Schnitt, der mit Isopentan (15) angereichert ist, das ein Produkt des Verfahrens ist, b) einen Schnitt, der mit n-Pentan (16) angereichert ist, das in den Reaktionsabschnitt [1] zurückgeführt wird, und c) einen Schnitt, der mit Kohlenwasserstoffen angereichert ist, die schwerer sind als die Pentane (17), der in einen zweiten Trennungsschritt [5] geleitet wird,
    2- einen zweiten Trennungsschritt [5], der aus einer Trennungssäule besteht, in der das Kopfprodukt und das Sumpfprodukt die Produkte der Einheit sind, nämlich ein Kopfstrom (19), das reich an verzweigten C6-Verbindungen ist, ein Sumpfstrom (18) und ein Intermediärschnitt (20), der mit n-Hexan angereichert ist, der als Nebenstrom entnommen wird, der in den Reaktionsabschnitt [1] zurückgeführt wird, Verfahren zur Isomerisierung, wobei ein Wärmeaustausch durchgeführt wird:
    - zwischen dem Kondensator des Entisohexanisierers [5] und entweder dem Verdampfer des Entpentanisierers [4] oder dem Verdampfer des Entisopentanisierers [3] oder beiden und,
    - zwischen dem Kondensator des Entpentanisierers [4] und dem Verdampfer des Entisopentanisierers [3].
EP15719168.5A 2014-04-29 2015-04-20 Benzinherstellungsverfahren mit einem isomerisierungsschritt gefolgt von mindestens zwei trennungsschritten Active EP3137583B1 (de)

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FR1453841A FR3020374B1 (fr) 2014-04-29 2014-04-29 Procede de production d'essence comprenant une etape d'isomerisation suivie d'au moins deux etapes de separation.
PCT/EP2015/058498 WO2015165763A1 (fr) 2014-04-29 2015-04-20 Procede de production d'essence comprenant une etape d'isomerisation suivie d'au moins deux etapes de separation

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US5741906A (en) * 1996-11-15 1998-04-21 Air Products And Chemicals, Inc. Production of triethylenediamine using surface acidity deactivated zeolite catalysts
EP3768803A4 (de) * 2018-04-30 2021-12-08 Sulzer Management AG Netzwerk von trennwandkolonnen in komplexen prozesseinheiten
WO2021137083A1 (en) * 2019-12-30 2021-07-08 Sabic Global Technologies B.V. Methods and systems for processing pentanes
US11648519B2 (en) * 2020-01-22 2023-05-16 Phillips 66 Company Systems for converting light paraffins to alcohols
GB2609807A (en) * 2020-04-16 2023-02-15 Kellogg Brown & Root Inc Integrated stabilizer in deisobutanizer for isomerization of hydrocarbons and product separation
CN111500317A (zh) * 2020-04-24 2020-08-07 河北新启元能源技术开发股份有限公司 一种异构化汽油生产工艺
US20220372382A1 (en) 2021-05-19 2022-11-24 Indian Oil Corporation Limited Process for isomerization of c5-c7 hydrocarbons in light naphtha range

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US2905619A (en) * 1956-06-28 1959-09-22 Universal Oil Prod Co Upgrading gasoline
US3060116A (en) * 1959-11-06 1962-10-23 Socony Mobil Oil Co Inc Combination reforming and cracking process
US3131235A (en) * 1960-11-23 1964-04-28 Universal Oil Prod Co Simultaneous isomerization of pentane and hexane with selective fractionation
JPS5490122A (en) * 1977-12-27 1979-07-17 Chiyoda Chem Eng & Constr Co Ltd Distillation of multi-component hydrocarbon composition
US5994607A (en) * 1996-02-05 1999-11-30 Institut Francais Du Petrole Paraffin isomerization process comprising fractionation having at least two draw-off levels associated with at least two isomerization zones
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
US20100025221A1 (en) * 2008-07-31 2010-02-04 Purdue Research Foundation Process for distillation of multicomponent mixtures into five product streams

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MX2016013897A (es) 2017-03-09
CN106661460B (zh) 2020-04-03
FR3020374A1 (fr) 2015-10-30
FR3020374B1 (fr) 2017-10-27
US10113121B2 (en) 2018-10-30
WO2015165763A1 (fr) 2015-11-05
US20170044447A1 (en) 2017-02-16
CN106661460A (zh) 2017-05-10
SA516380157B1 (ar) 2020-11-18

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