EP2930226A1 - Method for producing light olefins and btx using an ncc catalytic cracking unit treating a naphtha feedstock, with a catalytic reformer unit and an aromatic complex - Google Patents

Method for producing light olefins and btx using an ncc catalytic cracking unit treating a naphtha feedstock, with a catalytic reformer unit and an aromatic complex Download PDF

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EP2930226A1
EP2930226A1 EP15305502.5A EP15305502A EP2930226A1 EP 2930226 A1 EP2930226 A1 EP 2930226A1 EP 15305502 A EP15305502 A EP 15305502A EP 2930226 A1 EP2930226 A1 EP 2930226A1
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European Patent Office
Prior art keywords
ncc
unit
naphtha
light
fraction
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German (de)
French (fr)
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EP2930226B1 (en
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Bertrand Fanget
Abdelhakim Koudil
Romain Corroyer
Alexandre Pagot
Joana Fernandez
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IFP Energies Nouvelles IFPEN
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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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/08—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of reforming naphtha
    • 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
    • C10G63/00—Treatment of naphtha by at least one reforming process and at least one other conversion process
    • C10G63/02—Treatment of naphtha by at least one reforming process and at least one other conversion process plural serial stages only
    • C10G63/04—Treatment of naphtha by at least one reforming process and at least one other conversion process plural serial stages only including at least one cracking step
    • 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • 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
    • 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
    • C10G63/00—Treatment of naphtha by at least one reforming process and at least one other conversion process
    • C10G63/06—Treatment of naphtha by at least one reforming process and at least one other conversion process plural parallel stages only
    • C10G63/08—Treatment of naphtha by at least one reforming process and at least one other conversion process plural parallel stages only including at least one cracking step

Definitions

  • This new type of FCC unit is commonly called NCC for "Naphtha Catalytic Craking" that can be translated by catalytic cracking of naphtha.
  • the present invention provides an original solution to solve this problem by exchange of flux with the aromatic complex.
  • the invention proposes recycling to the reactor of the NCC unit a coking cutoff from the aromatic complex itself.
  • the NCC unit is also recycled to a non-aromatic raffinate to increase the production of light olefins.
  • the catalytic cracking of a naphtha-type fraction allows an increase in the yields of light olefins compared to an FCC working on conventional charges, and the problem of the closure of the thermal balance of the NCC is solved by the use of a heavy aromatics cut from the aromatic complex.
  • the present invention describes a refinery and petrochemical process scheme that achieves integration between three units: the FCC processes a light naphtha-type feedstock, referred to as NCC, catalytic reforming that processes heavy naphtha, and the aromatic complex (CA) producing of BTX.
  • NCC light naphtha-type feedstock
  • CA aromatic complex
  • the NCC unit benefits from the proximity of a very high charge to compensate for the coke deficit of the light naphtha charge, and an additional charge in the form of the raffinate from the aromatic complex, to produce more light olefins. .
  • the "heavy aromatics" flow of the aromatic complex (CA) is thus reduced to the maximum, or even eliminated, to the advantage of coke produced during the catalytic cracking reaction, and burned at the regenerator of the NCC to ensure the thermal balance.
  • the raffinate stream (12) from the aromatic complex is also minimized or eliminated to the benefit of light olefins produced by cracking in the NCC.
  • the load of the NCC is preheated by the furnaces of the catalytic reforming unit (FREF), preferably in the convection zone of the latter, which makes it possible to better balance the thermal balance of the NCC deficient in coke.
  • FREF catalytic reforming unit
  • the present invention describes a process scheme for the simultaneous production of light olefins (mainly ethylene and propylene) and BTX using three synergistically operating units: one FCC unit treating a naphtha-type feedstock. NCC light, catalytic reforming (REF) of the heavy naphtha fraction, and an aromatic complex (CA) producing BTX.
  • FCC unit treating a naphtha-type feedstock.
  • NCC light catalytic reforming (REF) of the heavy naphtha fraction
  • CA aromatic complex
  • the process feedstock is a naphtha cut, the broadest definition of which is initial point cutting at least 30 ° C and end point at most 220 ° C. Any cut having a distillation range within the wide range of 30 ° C-220 ° C is, in the context of the present invention, considered a naphtha.
  • the naphtha feed (1) distillation range 30 ° C-220 ° C is sent to a hydrotreatment unit (HDT) that removes the sulfur compounds and nitrogen contained in it.
  • HDT hydrotreatment unit
  • the hydrotreated naphtha feedstock (2) is sent to a separating unit (SPLIT1) which makes it possible to separate a light fraction called light naphtha, with a distillation range of 30 ° C, M ° C, and a heavy fraction called heavy naphtha, from distillation range T M ° C-220 ° C.
  • SPLIT1 separating unit
  • the value of the cutting point T M ° C can vary depending on the desired yields of final products (ethylene and propylene and BTX).
  • the temperature T M is between 80 and 160 ° C, and preferably between 100 ° C and 150 ° C, and even more preferably between 110 ° C and 140 ° C.
  • the light naphtha (3) is sent as a load of the NCC.
  • the heavy naphtha (4) is sent as a feed to the catalytic reforming unit (REF).
  • REF catalytic reforming unit
  • FRAC fractionation unit
  • SBF cold box separation
  • the heavy fraction (7) from the separator (FRAC) is sent in admixture with the effluents (5) of the catalytic reforming (REF) as feed (10) of the aromatic complex (CA).
  • the raffinate effluent (12) of the aromatic complex (CA) is sent to a separation unit (SPLIT2) which separates a light fraction (13) which is mixed with the light naphtha feed (3) to the catalytic cracking unit (NCC), and a heavy fraction (14) which is mixed with the heavy naphtha feedstock (4) to the catalytic reforming unit (REF).
  • SPLIT2 separation unit
  • NCC catalytic cracking unit
  • REF catalytic reforming unit
  • a second variant of the process according to the invention represented by the figure 3 variant which can be combined with the first variant, light paraffins from C2 to C5 produced as effluents of the catalytic cracking unit (NCC) from the separation box (SBF), are mixed with the naphtha feedstock light (3) to the catalytic cracking unit (NCC) to increase the yield of light olefins, ethylene and propylene and improve transport and fluidization.
  • the light molecules C4 and C5 from the separation box (SBF) are sent to an oligomerization unit (OLG), and the effluents of said oligomerization unit (OLG ) are mixed with the light naphtha feedstock (3) in the catalytic cracking unit (NCC).
  • OOG oligomerization unit
  • NCC catalytic cracking unit
  • the fractional naphtha fraction (3) resulting from the fractionation is preferably preheated in the convection zone of the catalytic reforming furnaces (FREF) before being introduced as a feedstock. of the catalytic cracking unit (NCC).
  • the process for producing light olefins and BTX according to the present invention preferably operates the NCC unit under severe cracking conditions, i.e. a reactor outlet temperature (ROT) of between 500 ° C. and 750 ° C, and a mass flow rate ratio of catalyst to mass flow rate (C / O) of between 5 and 40.
  • ROT reactor outlet temperature
  • C / O mass flow rate ratio of catalyst to mass flow rate
  • the process for the production of light olefins and BTX according to the present invention uses, for the NCC unit, a catalyst comprising a proportion of zeolite at least equal to 20%, and more particularly a proportion of ZSM-5 zeolite with less than 10% by weight relative to the total catalyst.
  • An FCC unit generally processes a heavy fraction from the vacuum distillation unit such as VGO (abbreviation of the English terminology Vacuum Gas Oil), or a vacuum residue, taken alone or as a mixture, or an atmospheric residue taken alone or in mixture.
  • VGO abbreviation of the English terminology Vacuum Gas Oil
  • the charge to the FCC may be lighter due to prior pretreatment of the VGO, for example, or because it comes from a conversion unit in which the initial charge has been enriched in hydrogen. and got rid of some impurities.
  • a recent adaptation of the FCC to even lighter loads, like gasoline, also known as naphtha, aims to convert these streams into light olefins (ethylene and propylene), high value-added products and starting points for the market. petrochemicals.
  • NCC An FCC unit dealing with naphtha type feeds is then called NCC.
  • the major problem of cracking these naphtha type feeds is the low coke yield of the feed which makes it necessary to rethink the heat balance of the unit.
  • the figure 1 schematically describes the aromatic complex with integration of a NCC unit, object of the present invention.
  • the naphtha feed is a gasoline cut whose initial boiling point is greater than or equal to 30 ° C, and the final boiling point is generally less than or equal to 220 ° C. It is previously treated in a hydrotreatment unit (HDT) to rid it of sulfur compounds and nitrogen compounds likely to poison the downstream catalysts.
  • HDT hydrotreatment unit
  • the desulphurized / denitrogenated naphtha effluent is sent to a fractionation unit (SPLIT1).
  • the light part resulting from this fractionation (stream 3) is sent to the NCC unit, while the heavy part (stream 4) is sent to the catalytic reforming unit (REF) after having been heated to the required level in a furnace. reforming (FREF).
  • the downstream fractionation of the NCC unit is represented by the unit (FRAC) and can be adjusted to direct the production to more light olefins, or to more aromatics.
  • the heavy stream (7) leaving the fractionation unit (FRAC) is directed to the aromatic complex (CA).
  • the light stream (8) leaving the fractionation unit (FRAC) is directed to a separation unit (SBF) for separating the light olefins ethylene and propylene, hydrogen and methane, and propane and butane.
  • SBF separation unit
  • the FRAC (FRAC) is mixed with the effluents of the catalytic reforming unit (5) to form the feed (10) of the aromatic complex (CA) from which the BTX is extracted, and a further aromatic cut. heavy corresponding to the flow (11).
  • the non-aromatic fraction called raffinate corresponds to the flow (12) and, in the basic version of the scheme according to the invention, is mixed with the light fraction of the naphtha (3) as a feedstock of the NCC unit.
  • NCC catalytic reforming
  • CA aromatic complex
  • the aromatic complex (CA) is used to produce benzene, toluene and xylenes (globally noted BTX), including para-xylene, the petrochemical base product.
  • the heavy aromatics stream (stream 11) is recycled at least in part to the NCC as an additional feed, mixed with the light naphtha feedstock (3), and ensures the heat balance of the NCC.
  • the flux called raffinate (12) corresponding to the non-aromatic portion of the aromatic complex (CA), is recycled at least in part to the NCC as an additional charge producing light olefins.
  • the raffinate (12) can be separated into two fractions in a separation unit noted (SPLIT2), the light portion (13) going to the NCC to produce essentially olefins and a few aromatics, and the heavy part (14). going to reforming (REF) to produce additional aromatics.
  • SPLIT2 separation unit noted
  • the light portion (13) going to the NCC to produce essentially olefins and a few aromatics
  • the heavy part (14) going to reforming (REF) to produce additional aromatics.
  • the non-aromatic fraction of the aromatic complex (AC) effluents referred to as the raffinate (stream 12), is returned, in whole or in part, to the NCC forming an additional charge to the main charge (3) of the NCC.
  • NCC products other than ethylene or propylene can be recycled in this unit. It is also possible to use the so-called “dry gas” part, excluding ethylene, and the so-called “LPG” part, excluding propylene, as fuel gas in the catalytic reforming furnaces (FREF).
  • dry gas excluding ethylene
  • LPG so-called propylene
  • the reforming heat exchange train is used to increase the temperature of the light naphtha (3) going to the NCC. This preheating of the NCC load saves the calories needed for the thermal balance of the NCC.
  • the thermal balance of the NCC is ensured by the recycle of the heavy aromatics (HA) section, flow noted (11), leaving the aromatic complex (CA).
  • This section of heavy aromatics can be defined as consisting of compounds with a carbon number greater than 8.
  • This highly aromatic cut is a strongly cokantic cut which will make it possible to generate the quantity of coke necessary for the closure of the thermal balance of the carbon dioxide. NCC unit.
  • the NCC unit is a naphtha catalytic cracking (NCC) unit having at least one main reactor operating either in riser flow or down flow.
  • NCC naphtha catalytic cracking
  • the NCC unit may have a secondary reactor, type "riser” or “downer” to crack recycles or additional flows separately.
  • It furthermore has a regeneration section of the catalyst in which the coke formed in the reaction and deposited on the catalyst is burned in order to recover in the form of sensible heat from the catalyst part of the heat required in the reactor.
  • the NCC unit has its own hydrocarbon effluent treatment section including a gas treatment section allowing a separation of light olefins (ethylene, propylene) from other gases: hydrogen, methane, ethane, propane.
  • This separation section is represented by the assembly formed by the fractionation of the effluents (FRAC) and the cold box of separation of the light compounds (that is to say less than 5 carbon atoms) noted SBF.
  • the heavier portion of the hydrocarbon effluents is treated in a separation section (FRAC) comprising at least one fractionation unit for recovering the C6 + cut (stream 7) which is sent to the aromatic complex (CA).
  • FRAC separation section
  • CA aromatic complex
  • the intermediate portion comprising the hydrocarbons with 4 and 5 carbon atoms can be either recycled directly to the NCC, or sent to an oligomerization unit (OLG) to obtain polyC4 / C5 type cuts whose crackability (c '). that is, the cracking potential) in the NCC is significantly higher than that of the non-oligomerized compounds, or still be upgraded to dedicated pools.
  • OLG oligomerization unit
  • the NCC unit is operated preferably at high severity, that is to say with a high reactor output temperature (ROT) and a high C / O ratio (ratio of the catalyst flow rate to the feed rate entering the NCC the two flow rates being mass).
  • ROT reactor output temperature
  • C / O ratio ratio of the catalyst flow rate to the feed rate entering the NCC the two flow rates being mass
  • the catalyst may be any type of acid catalyst, with a preference for a catalyst containing a certain proportion of zeolite, preferably greater than 20% by weight of the total catalyst.
  • a typical FCC catalyst comprising alumina, zeolite Y, and zeolite ZSM-5 is an example of a catalyst that could be used.
  • the tests were carried out with high severity (temperature> 650 ° C and C / O> 15) in order to simulate as closely as possible the operating conditions of the NCC.
  • the first example makes it possible to justify the interest of the proximity of the aromatic complex and the NCC unit in order to extract the aromatics produced during the cracking of a straight-run gasoline type feedstock.
  • Table 2 describes the chemical family structure of a paraffinic naphtha whose distillation range is between 55 ° C and 115 ° C.
  • Table 3 provides the yield structure of the products resulting from the cracking of this charge on a pilot unit in simulated riser with low contact time and with a high severity.
  • Table 2 - Composition of FCC Naphtha by Hydrocarbon Family.
  • the yields of ethylene and propylene are significantly higher than for a conventional VGO FCC.
  • the coke yield is much lower than for a conventional FCC. With this lower coke yield, an external supply of heat to the regenerator is necessary, it even represents 95% of the heat necessary to ensure a balance between the reactor and the regenerator.
  • Example 2 NCC unit coupled to an aromatic complex with a large cut naphtha cut at 50-50.
  • the distilled fraction corresponding to the first 50% by weight, and whose properties are given in Table 2, is sent to the NCC under the conditions of severity described in Example 1, while the 115 ° C + portion represents approximately 50% by weight. of the total, is sent to a catalytic reforming unit.
  • the coke yield of the NCC is very much increased.
  • Example 3 NCC unit coupled to an aromatic complex with a large cut naphtha cut at 40-60.
  • the yields of aromatics are markedly increased by the fact that more charge has been sent to the reforming and the aromatic complex. NCC coke continues to increase as more heavy aromatics are sent to the reactor.

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Abstract

La présente invention concerne un procédé de production d'oléfines légères et de BTX faisant appel à une unité de craquage catalytique NCC traitant une charge de type naphta, et à un complexe aromatique. Elle permet d'exploiter des synergies entre ces deux unités. Le bilan thermique du NCC intrinsèquement déficitaire en coke, est résolu par l'utilisation optimale de la chaleur des fours de reformage afin de préchauffer la charge du NCC, et par l'introduction en mélange avec le naphta d'une partie au moins du raffinat issu du complexe aromatique.The present invention relates to a process for the production of light olefins and BTX using a catalytic cracking unit NCC treating a naphtha feed, and an aromatic complex. It makes it possible to exploit synergies between these two units. The thermal balance of the NCC, which is intrinsically deficient in coke, is solved by the optimal use of the heat of the reforming furnaces in order to preheat the load of the NCC, and by the introduction in mixture with the naphtha of at least a part of the raffinate. derived from the aromatic complex.

Description

DOMAINE DE L'INVENTIONFIELD OF THE INVENTION

L'intérêt pour le craquage de charges paraffiniques de type essence de distillation directe dans des unités de FCC afin de les valoriser en propylène et éthylène est relativement récent. Cet intérêt provient de la nécessité de disposer d'oléfines légères, éthylène et propylène pour la pétrochimie, en plus de la source traditionnelle que constitue le vapocraquage. Le craquage de coupe de type essence ou naphta conduit à une modification des conditions opératoires du FCC, et à l'utilisation de zéolithe de type ZSM-5. Actuellement, le différentiel de prix de marché entre les oléfines légères et l'essence incite au moins en partie, à tirer un meilleur profit de l'essence en la transformant en ces oléfines légères. De plus, l'amélioration des catalyseurs zéolitiques permet des rendements plus intéressants dans cette transformation en oléfines légères.The interest in cracking paraffinic feedstock of the straight-run gasoline type in FCC units in order to upgrade them to propylene and ethylene is relatively recent. This interest stems from the need for light olefins, ethylene and propylene for petrochemicals, in addition to the traditional source of steam cracking. Gasoline or naphtha type cracking leads to a modification of the operating conditions of the FCC, and to the use of ZSM-5 type zeolite. Currently, the market price differential between light olefins and gasoline is at least partly an incentive to take better advantage of gasoline by turning it into these light olefins. In addition, the improvement of zeolitic catalysts allows more interesting yields in this transformation to light olefins.

Ce nouveau type d'unités FCC est couramment appelé NCC pour « Naphtha Catalytic Craking » qu'on peut traduire par craquage catalytique de naphta.This new type of FCC unit is commonly called NCC for "Naphtha Catalytic Craking" that can be translated by catalytic cracking of naphtha.

Les réactions de craquage, en plus de produire des oléfines, s'accompagnent de la formation de molécules aromatiques qui n'étaient généralement pas valorisées en tant que telles, car le coût de leur séparation s'avèrerait peu ou pas rentable.The cracking reactions, in addition to producing olefins, are accompanied by the formation of aromatic molecules which were generally not valued as such, since the cost of their separation would prove to be of little or no profit.

Par ailleurs, le craquage de coupes légères dans le procédé FCC pose un problème car ce type de charge ne produit pas suffisamment de coke dans les conditions du FCC, et la balance thermique du FCC ne peut être atteinte que par un apport de chaleur externe au procédé.In addition, the cracking of light cuts in the FCC process poses a problem because this type of charge does not produce enough coke under the conditions of the FCC, and the thermal balance of the FCC can be reached only by an external heat input to the FCC. process.

La présente invention propose une solution originale pour résoudre ce problème par échange de flux avec le complexe aromatique.The present invention provides an original solution to solve this problem by exchange of flux with the aromatic complex.

EXAMEN DE L'ART ANTERIEUREXAMINATION OF THE PRIOR ART

Il est courant de trouver des documents qui proposent de recycler au régénérateur d'une unité de craquage catalytique (FCC) des coupes à fort potentiel de coke du type « slurry ».It is common to find documents that propose to recycle to the regenerator of a catalytic cracking unit (FCC) cuts with high potential of coke of the "slurry" type.

D'autres documents décrivent le recycle de coupe cokante dans le stripeur du FCC, ou dans une capacité en dérivation du stripeur. L'invention propose de recycler au réacteur de l'unité NCC une coupe cokante issue du complexe aromatique lui-même. On recycle aussi dans le réacteur de l'unité NCC un raffinat non aromatique pour augmenter la production d'oléfines légères.Other documents describe the cokant cutting recycle in the FCC stripper, or in a bypass capability of the stripper. The invention proposes recycling to the reactor of the NCC unit a coking cutoff from the aromatic complex itself. The NCC unit is also recycled to a non-aromatic raffinate to increase the production of light olefins.

En résumé le craquage catalytique d'une coupe de type naphta permet une augmentation des rendements en oléfines légères par rapport à un FCC travaillant sur des charges conventionnelles, et le problème du bouclage du bilan thermique du NCC est résolu par l'utilisation d'une coupe d'aromatiques lourds issue du complexe aromatique.In summary, the catalytic cracking of a naphtha-type fraction allows an increase in the yields of light olefins compared to an FCC working on conventional charges, and the problem of the closure of the thermal balance of the NCC is solved by the use of a heavy aromatics cut from the aromatic complex.

DESCRIPTION SOMMAIRE DES FIGURESSUMMARY DESCRIPTION OF THE FIGURES

  • La figure 1 présente le schéma du procédé selon l'invention dans sa version de base. Dans cette version le raffinat issu du complexe aromatique (CA) est directement envoyé, au moins en partie, en mélange avec le naphta léger issu de l'unité de séparation (SPLIT1) placée en amont du NCC pour alimenter l'unité NCC. Le fractionnement placé en amont de l'unité NCC et noté (SPLIT1) permet de séparer la coupe naphta de départ en une fraction légère dite « naphta léger » qui alimente le NCC, et une fraction lourde dite « naphta lourd » qui alimente le reformage catalytique.The figure 1 presents the diagram of the method according to the invention in its basic version. In this version the raffinate from the aromatic complex (CA) is directly sent, at least in part, in mixture with the light naphtha from the separation unit (SPLIT1) placed upstream of the NCC to supply the NCC unit. Fractionation placed upstream of the NCC unit and noted (SPLIT1) makes it possible to separate the starting naphtha fraction into a light fraction called "light naphtha" which feeds the NCC, and a heavy fraction called "heavy naphtha" which feeds the reforming catalytic.
  • La figure 2 représente une première variante du schéma de procédé selon la présente invention dans laquelle le raffinat issu du complexe aromatique est envoyé dans une colonne de séparation (SPLIT 2) qui permet de séparer un premier raffinat plus léger (flux 13) qui est introduit en mélange avec la charge naphta léger à l'unité NCC, et un second raffinat plus lourd (flux 14) qui est dirigé vers l'unité de reformage catalytique.The figure 2 represents a first variant of the process scheme according to the present invention in which the raffinate from the aromatic complex is sent to a separation column (SPLIT 2) which makes it possible to separate a first lighter raffinate (stream 13) which is introduced in admixture with the light naphtha feedstock to the NCC unit, and a second heavier raffinate (feed 14) which is directed to the catalytic reforming unit.
  • La figure 3 représente une seconde variante du schéma de procédé selon l'invention qui en plus de la modification de la première variante, introduit un recyclage d'hydrocarbures paraffinique légers du type éthane, propane et butane en mélange avec la charge naphta léger du NCC (flux 15).The figure 3 represents a second variant of the process scheme according to the invention which, in addition to the modification of the first variant, introduces a recycling of light paraffinic hydrocarbons of the ethane, propane and butane type mixed with the light naphtha feedstock of the NCC (stream 15). ).
  • La figure 4 représente une troisième variante du schéma de procédé selon l'invention qui, en plus des unités déjà présentes dans les variantes précédentes, introduit une unité d'oligomérisation (OLG) des coupes C4 et C5, de façon à produire des oligomères plus facilement craquables, et susceptible de produire encore plus de propylène et de l'éthylène.The figure 4 represents a third variant of the process scheme according to the invention which, in addition to the units already present in the preceding variants, introduces an oligomerization unit (OLG) of the C4 and C5 cuts, so as to produce oligomers which are more easily crackable, and likely to produce even more propylene and ethylene.
DESCRIPTION SOMMAIRE DE L'INVENTIONSUMMARY DESCRIPTION OF THE INVENTION

La présente invention décrit un schéma de procédé de raffinage et pétrochimie qui réalise une intégration entre trois unités : le FCC traitant une charge de type naphta léger, appelé NCC, le reformage catalytique qui traite le naphta lourd, et le complexe aromatique (CA) producteur de BTX.The present invention describes a refinery and petrochemical process scheme that achieves integration between three units: the FCC processes a light naphtha-type feedstock, referred to as NCC, catalytic reforming that processes heavy naphtha, and the aromatic complex (CA) producing of BTX.

L'intégration entre ces trois unités se réalise à la fois par des échanges de flux de matière, et aussi par l'utilisation de la zone de convection des fours de reformage pour assurer la préchauffe de la charge naphta du NCC.The integration between these three units is carried out both by exchanges of material flows, and also by the use of the convection zone of the reforming furnaces to ensure the preheating of the naphtha feedstock of the NCC.

Les avantages de l'intégration entre l'unité NCC et le complexe aromatique (CA) peuvent se résumer par les points suivants :The advantages of integration between the NCC unit and the aromatic complex (CA) can be summarized by the following points:

La production simultanée d'oléfines légères et d'aromatiques à partir d'une charge naphta de départ.The simultaneous production of light olefins and aromatics from a starting naphtha feedstock.

L'unité NCC bénéficie de la proximité d'une charge très cokante pour compenser le déficit en coke de la charge naphta léger, et d'un surcroit de charge sous forme du raffïnat en provenance du complexe aromatique, pour produire plus d'oléfines légères.The NCC unit benefits from the proximity of a very high charge to compensate for the coke deficit of the light naphtha charge, and an additional charge in the form of the raffinate from the aromatic complex, to produce more light olefins. .

L'intégration du NCC au complexe aromatique permet d'obtenir un schéma de procédé qui réduit finalement les sorties à du fuel-gas (H2 et C1 essentiellement), des oléfines légères (C2= et C3=) et des BTX.The integration of the NCC into the aromatic complex makes it possible to obtain a process scheme that ultimately reduces the outputs to fuel gas (H2 and C1 essentially), light olefins (C2 = and C3 =) and BTX.

Le recycle à épuisement des autres effluents, tels que le raffinat et la fraction aromatiques lourds issues du complexe aromatique (CA), permet à la fois d'augmenter la production d'oléfines légères, éthylène et propylène, et d'assurer le bilan thermique du NCC. C'est en ce sens qu'on peut parler d'une véritable synergie entre le NCC et le complexe aromatique.The exhaustion cycle of other effluents, such as the raffinate and the aromatic heavy fraction derived from the aromatic complex (CA), makes it possible both to increase the production of light olefins, ethylene and propylene, and to ensure the thermal balance of the NCC. It is in this sense that we can speak of a real synergy between the NCC and the aromatic complex.

Le flux "aromatiques lourds" du complexe aromatique (CA) est ainsi diminué au maximum, voire éliminé, au bénéfice de coke produit lors de la réaction de craquage catalytique, et brûlé au régénérateur du NCC pour en assurer le bilan thermique.The "heavy aromatics" flow of the aromatic complex (CA) is thus reduced to the maximum, or even eliminated, to the advantage of coke produced during the catalytic cracking reaction, and burned at the regenerator of the NCC to ensure the thermal balance.

Le flux de raffinat (12) en provenance du complexe aromatique est également diminué au maximum, voire éliminé, au bénéfice d'oléfines légères produites par le craquage dans le NCC.The raffinate stream (12) from the aromatic complex is also minimized or eliminated to the benefit of light olefins produced by cracking in the NCC.

La charge du NCC est préchauffée par les fours de l'unité de reformage catalytique (FREF), préférentiellement dans la zone de convection de ces derniers, ce qui permet de mieux équilibrer la balance thermique du NCC déficitaire en coke.The load of the NCC is preheated by the furnaces of the catalytic reforming unit (FREF), preferably in the convection zone of the latter, which makes it possible to better balance the thermal balance of the NCC deficient in coke.

De façon plus précise, la présente invention décrit un schéma de procédé permettant la production simultanée d'oléfines légères (principalement éthylène et propylène) et de BTX en faisant appel à trois unités fonctionnant en synergie : une unité de FCC traitant une charge de type naphta léger dite NCC, un reformage catalytique (REF) de la coupe naphta lourd, et un complexe aromatique (CA) producteur de BTX.More specifically, the present invention describes a process scheme for the simultaneous production of light olefins (mainly ethylene and propylene) and BTX using three synergistically operating units: one FCC unit treating a naphtha-type feedstock. NCC light, catalytic reforming (REF) of the heavy naphtha fraction, and an aromatic complex (CA) producing BTX.

Le schéma du procédé selon la présente invention peut se décrire de la façon suivante :The scheme of the process according to the present invention can be described as follows:

La charge du procédé est une coupe naphta dont la définition la plus large est celle d'une coupe de point initial au moins 30°C et de point final au plus 220°C. Toute coupe ayant un intervalle de distillation compris à l'intérieur de la fourchette large 30°C-220°C est, dans le cadre de la présente invention, considérée comme un naphta.The process feedstock is a naphtha cut, the broadest definition of which is initial point cutting at least 30 ° C and end point at most 220 ° C. Any cut having a distillation range within the wide range of 30 ° C-220 ° C is, in the context of the present invention, considered a naphtha.

Par simplification on conservera 30°C et 220°C comme les points initial et final typiques d'une coupe naphta.For simplicity we will keep 30 ° C and 220 ° C as the initial and final points typical of a naphtha cut.

La charge naphta (1) d'intervalle de distillation 30°C-220°C est envoyée dans une unité d'hydrotraitement (HDT) qui permet d'éliminer les composés soufrés et azotés qu'elle contient.The naphtha feed (1) distillation range 30 ° C-220 ° C is sent to a hydrotreatment unit (HDT) that removes the sulfur compounds and nitrogen contained in it.

La charge naphta hydrotraitée (2) est envoyée dans une unité de séparation (SPLIT1) qui permet de séparer une fraction légère dite naphta léger, d'intervalle de distillation 30°C-TM°C, et une fraction lourde dite naphta lourd, d'intervalle de distillation TM°C-220°C.The hydrotreated naphtha feedstock (2) is sent to a separating unit (SPLIT1) which makes it possible to separate a light fraction called light naphtha, with a distillation range of 30 ° C, M ° C, and a heavy fraction called heavy naphtha, from distillation range T M ° C-220 ° C.

La valeur du point de coupe TM°C peut varier en fonction des rendements souhaités en produits finaux (éthylène et propylène et BTX).The value of the cutting point T M ° C can vary depending on the desired yields of final products (ethylene and propylene and BTX).

Généralement la température TM est comprise entre 80 et 160°C, et préférentiellement comprise entre 100°C et 150°C, et encore plus préférentiellement comprise entre 110°C et 140°C.Generally the temperature T M is between 80 and 160 ° C, and preferably between 100 ° C and 150 ° C, and even more preferably between 110 ° C and 140 ° C.

Le naphta léger (3) est envoyé comme charge du NCC.The light naphtha (3) is sent as a load of the NCC.

Le naphta lourd (4) est envoyé comme charge de l'unité de reformage catalytique (REF).The heavy naphtha (4) is sent as a feed to the catalytic reforming unit (REF).

Les effluents (6) du NCC sont séparés dans une unité de fractionnement ( FRAC) qui permet de séparer une fraction légère (8) qui est envoyée dans une séparation dite boite froide (SBF) qui permet d'isoler l'H2, le CH4 et les paraffines légères en C2, C3, C4, C5, et l'éthylène (C2=) et le propylène ( C3=).The effluents (6) of the NCC are separated in a fractionation unit (FRAC) which makes it possible to separate a light fraction (8) which is sent into a so-called cold box separation (SBF) which makes it possible to isolate the H2, the CH4 and C2, C3, C4, C5 light paraffins and ethylene (C2 =) and propylene (C3 =).

La fraction lourde (7) issue du séparateur (FRAC) est envoyée en mélange avec les effluents (5) du reformage catalytique (REF) comme charge (10) du complexe aromatique (CA).The heavy fraction (7) from the separator (FRAC) is sent in admixture with the effluents (5) of the catalytic reforming (REF) as feed (10) of the aromatic complex (CA).

Le complexe aromatique (CA) permet d'extraire les BTX, un raffinat (12), correspondant à la partie non aromatique des effluents, qui est envoyé au moins en partie en mélange avec le naphta léger (3) comme charge du NCC, et une fraction dite aromatiques lourds (11) qui est également envoyée en mélange avec le naphta léger (3) comme charge du NCC pour assurer par son pouvoir cokant le bilan thermique de ce dernier.The aromatic complex (CA) extracts BTX, a raffinate (12), corresponding to the non-aromatic part of the effluents, which is sent at least partly in a mixture with the light naphtha (3) as the NCC feed, and a so-called heavy aromatic fraction (11) which is also mixed with the light naphtha (3) as a feedstock of the NCC to ensure by its coking power the heat balance of the latter.

Dans une première variante du procédé selon l'invention, représentée par la figure 2, l'effluent raffinat (12) du complexe aromatique (CA) est envoyé dans une unité de séparation (SPLIT2) qui permet de séparer une fraction légère (13) qui est envoyée en mélange avec la charge naphta léger (3) à l'unité de craquage catalytique (NCC), et une fraction lourde (14) qui est envoyée en mélange avec la charge naphta lourd (4) à l'unité de reformage catalytique (REF).In a first variant of the method according to the invention, represented by the figure 2 , the raffinate effluent (12) of the aromatic complex (CA) is sent to a separation unit (SPLIT2) which separates a light fraction (13) which is mixed with the light naphtha feed (3) to the catalytic cracking unit (NCC), and a heavy fraction (14) which is mixed with the heavy naphtha feedstock (4) to the catalytic reforming unit (REF).

Dans une seconde variante du procédé selon l'invention représentée par la figure 3, variante qui peut se combiner à la première variante, les paraffines légères de C2 à C5 produites comme effluents de l'unité de craquage catalytique ( NCC) à partir de la boite de séparation (SBF), sont envoyées en mélange avec la charge naphta léger (3) vers l'unité de craquage catalytique (NCC) afin d'augmenter le rendement en oléfines légères, éthylène et propylène et améliorer le transport et la fluidisation.In a second variant of the process according to the invention represented by the figure 3 , variant which can be combined with the first variant, light paraffins from C2 to C5 produced as effluents of the catalytic cracking unit (NCC) from the separation box (SBF), are mixed with the naphtha feedstock light (3) to the catalytic cracking unit (NCC) to increase the yield of light olefins, ethylene and propylene and improve transport and fluidization.

Dans une troisième variante du procédé selon l'invention représentée par la figure 4, variante qui peut parfaitement se combiner aux variantes précédentes, les molécules légères en C4 et C5 issues de la boite de séparation (SBF) sont envoyées dans une unité d'oligomérisation (OLG), et les effluents de ladite unité d'oligomérisation (OLG) sont envoyés en mélange avec la charge naphta léger (3) dans l'unité de craquage catalytique (NCC).In a third variant of the method according to the invention represented by the figure 4 , variant which can perfectly combine with the previous variants, the light molecules C4 and C5 from the separation box (SBF) are sent to an oligomerization unit (OLG), and the effluents of said oligomerization unit (OLG ) are mixed with the light naphtha feedstock (3) in the catalytic cracking unit (NCC).

Enfin dans toutes les variantes du procédé selon la présente invention, la coupe naphta léger (3) issue du fractionnement (SPLIT1) est de manière préférée préchauffée dans la zone de convection des fours de reformage catalytique (FREF) avant d'être introduite comme charge de l'unité de craquage catalytique (NCC).Finally, in all the variants of the process according to the present invention, the fractional naphtha fraction (3) resulting from the fractionation (SPLIT1) is preferably preheated in the convection zone of the catalytic reforming furnaces (FREF) before being introduced as a feedstock. of the catalytic cracking unit (NCC).

Le procédé de production d'oléfines légères et de BTX selon la présente invention fait préférentiellement fonctionner l'unité NCC dans des conditions de craquage sévères, c'est-à-dire une température de sortie du réacteur (ROT) comprise entre 500°C et 750°C, et un rapport du débit massique de catalyseur sur le débit massique de charge (C/O) compris entre 5 et 40.The process for producing light olefins and BTX according to the present invention preferably operates the NCC unit under severe cracking conditions, i.e. a reactor outlet temperature (ROT) of between 500 ° C. and 750 ° C, and a mass flow rate ratio of catalyst to mass flow rate (C / O) of between 5 and 40.

Le procédé de production d'oléfines légères et de BTX selon la présente invention fait appel, pour l'unité NCC, à un catalyseur comprenant une proportion de zéolithe au moins égal à 20%, et plus particulièrement une proportion de zéolithe ZSM-5 au moins égal à 10% en poids par rapport au catalyseur total.The process for the production of light olefins and BTX according to the present invention uses, for the NCC unit, a catalyst comprising a proportion of zeolite at least equal to 20%, and more particularly a proportion of ZSM-5 zeolite with less than 10% by weight relative to the total catalyst.

DESCRIPTION DETAILLEE DE L'INVENTIONDETAILED DESCRIPTION OF THE INVENTION

Une unité FCC traite généralement une coupe lourde issue de l'unité de distillation sous vide comme le VGO (abréviation de la terminologie anglo saxonne Vacuum Gas Oil), ou un résidu sous vide, pris seul ou en mélange, ou encore un résidu atmosphérique pris seul ou en mélange.An FCC unit generally processes a heavy fraction from the vacuum distillation unit such as VGO (abbreviation of the English terminology Vacuum Gas Oil), or a vacuum residue, taken alone or as a mixture, or an atmospheric residue taken alone or in mixture.

Il arrive cependant que la charge arrivant au FCC puisse être plus légère du fait d'un prétraitement préalable du VGO par exemple, ou bien du fait qu'elle provienne d'une unité de conversion dans laquelle la charge initiale s'est enrichie en hydrogène et a été débarrassée de certaines impuretés.However, it is possible that the charge to the FCC may be lighter due to prior pretreatment of the VGO, for example, or because it comes from a conversion unit in which the initial charge has been enriched in hydrogen. and got rid of some impurities.

Une adaptation récente du FCC à des charges encore plus légères, de type essences, appelées aussi naphta, a pour but de convertir ces flux en oléfines légères (éthylène et propylène), produits à forte valeur ajoutée et points de départ pour le marché de la pétrochimie.A recent adaptation of the FCC to even lighter loads, like gasoline, also known as naphtha, aims to convert these streams into light olefins (ethylene and propylene), high value-added products and starting points for the market. petrochemicals.

Une unité de FCC traitant des charges de type naphta est alors appelé NCC. Le problème majeur du craquage de ces charges de type naphta provient du faible rendement en coke de la charge qui oblige à repenser le bilan thermique de l'unité.An FCC unit dealing with naphtha type feeds is then called NCC. The major problem of cracking these naphtha type feeds is the low coke yield of the feed which makes it necessary to rethink the heat balance of the unit.

Dans la présente invention, ce problème de bilan thermique du NCC est résolu par synergie avec un complexe aromatique (CA).In the present invention, this thermal balance problem of NCC is solved by synergy with an aromatic complex (CA).

La figure 1 décrit schématiquement le complexe aromatique avec intégration d'une unité NCC, objet de la présente invention.The figure 1 schematically describes the aromatic complex with integration of a NCC unit, object of the present invention.

La charge naphta est une coupe essence dont le point d'ébullition initial est supérieur ou égal à 30°C, et le point d'ébullition final est généralement inférieur ou égal à 220°C. Elle est préalablement traitée dans une unité d'hydrotraitement (HDT) afin de la débarrasser des composés soufrés et azotés susceptibles d'empoisonner les catalyseurs en aval.The naphtha feed is a gasoline cut whose initial boiling point is greater than or equal to 30 ° C, and the final boiling point is generally less than or equal to 220 ° C. It is previously treated in a hydrotreatment unit (HDT) to rid it of sulfur compounds and nitrogen compounds likely to poison the downstream catalysts.

L'effluent naphta désulfurisé/déazotée est envoyé dans une unité de fractionnement (SPLIT1). La partie légère issue de ce fractionnement (flux 3) est envoyée à l'unité NCC, alors que la partie lourde (flux 4) est envoyée à l'unité de reformage catalytique (REF) après avoir été chauffée au niveau requis dans un four de reformage (FREF).The desulphurized / denitrogenated naphtha effluent is sent to a fractionation unit (SPLIT1). The light part resulting from this fractionation (stream 3) is sent to the NCC unit, while the heavy part (stream 4) is sent to the catalytic reforming unit (REF) after having been heated to the required level in a furnace. reforming (FREF).

Le fractionnement en aval de l'unité NCC est représenté par l'unité (FRAC) et peut être réglé de façon à orienter la production vers plus d'oléfines légères, ou vers plus d'aromatiques.The downstream fractionation of the NCC unit is represented by the unit (FRAC) and can be adjusted to direct the production to more light olefins, or to more aromatics.

Le flux lourd (7) sortant de l'unité de fractionnement (FRAC) est dirigé vers le complexe aromatique (CA).The heavy stream (7) leaving the fractionation unit (FRAC) is directed to the aromatic complex (CA).

Le flux léger (8) sortant de l'unité de fractionnement (FRAC) est dirigé vers une unité de séparation (SBF) permettant de séparer les oléfines légères éthylène et propylène, l'hydrogène et le méthane, et le propane et le butane.The light stream (8) leaving the fractionation unit (FRAC) is directed to a separation unit (SBF) for separating the light olefins ethylene and propylene, hydrogen and methane, and propane and butane.

Le flux lourd (7) issu du fractionnement (FRAC) est mélangé aux effluents de l'unité de reformage catalytique (5) pour former la charge (10) du complexe aromatique (CA) duquel on extrait les BTX, et une coupe aromatique plus lourde correspondant au flux (11).The FRAC (FRAC) is mixed with the effluents of the catalytic reforming unit (5) to form the feed (10) of the aromatic complex (CA) from which the BTX is extracted, and a further aromatic cut. heavy corresponding to the flow (11).

La coupe non aromatique dite raffinat correspond au flux (12) et, dans la version de base du schéma selon l'invention, est envoyée en mélange avec la fraction légère du naphta (3) comme charge de l'unité NCC.The non-aromatic fraction called raffinate corresponds to the flow (12) and, in the basic version of the scheme according to the invention, is mixed with the light fraction of the naphtha (3) as a feedstock of the NCC unit.

Les unités mises enjeu dans le présent schéma, c'est-à-dire le NCC, le reformage catalytique (REF) et le complexe aromatique (CA) permettent de produire à partir d'un naphta de départ, de l'éthylène et du propylène, et des BTX. Certaines variantes du schéma de base permettent de produire plus de propylène ou d'éthylène.The units involved in the present scheme, ie NCC, catalytic reforming (REF) and aromatic complex (CA), make it possible to produce from ethylene starting material a starting naphtha. propylene, and BTX. Some variants of the basic scheme can produce more propylene or ethylene.

Le complexe aromatiques (CA) permet de produire du benzène, du toluène et des xylènes (notés globalement BTX), et notamment du para-xylène, produit de base de la pétrochimie. Le flux d'aromatiques lourds (flux 11) est recyclé au moins en partie au NCC en tant que charge additionnelle, en mélange avec la charge naphta léger (3), et permet d'assurer le bilan thermique du NCC.The aromatic complex (CA) is used to produce benzene, toluene and xylenes (globally noted BTX), including para-xylene, the petrochemical base product. The heavy aromatics stream (stream 11) is recycled at least in part to the NCC as an additional feed, mixed with the light naphtha feedstock (3), and ensures the heat balance of the NCC.

Le flux appelé raffinat (12) correspondant à la partie non aromatique du complexe aromatique (CA), est recyclé au moins en partie au NCC en tant que charge additionnelle productrice d'oléfines légères.The flux called raffinate (12) corresponding to the non-aromatic portion of the aromatic complex (CA), is recycled at least in part to the NCC as an additional charge producing light olefins.

Selon le schéma représenté en figure 2, le raffinat (12) peut être séparé en deux fractions dans une unité de séparation notée (SPLIT2), la partie légère (13) allant au NCC pour produire essentiellement des oléfines et un peu d'aromatiques, et la partie lourde (14) allant au reformage (REF) pour produire des aromatiques supplémentaires.According to the diagram represented in figure 2 , the raffinate (12) can be separated into two fractions in a separation unit noted (SPLIT2), the light portion (13) going to the NCC to produce essentially olefins and a few aromatics, and the heavy part (14). going to reforming (REF) to produce additional aromatics.

L'unité (NCC) après séparation dans le fractionnement (FRAC) et la boite froide (SBF) produit un flux en C6+ (noté 9) contenant une quantité appréciable d'aromatiques qui sont introduits en mélange avec la fraction lourde du fractionnement (FRAC) pour former le flux (7) alimentant le complexe aromatique (CA) en mélange avec les effluents (10) du reformage catalytique (REF).The unit (NCC) after fractionation separation (FRAC) and the cold box (SBF) produces a C6 + flux (denoted 9) containing an appreciable quantity of aromatics which are introduced in admixture with the heavy fractionation fraction (FRAC). ) to form the flow (7) supplying the aromatic complex (CA) mixed with the effluents (10) of the catalytic reforming (REF).

La fraction non aromatique des effluents du complexe aromatique (CA), dit raffinat (flux 12) est renvoyée, en totalité ou en partie, au NCC formant une charge additionnelle à la charge principale (3) du NCC. Cette charge additionnelle permet d'augmenter les rendements finaux en oléfines légères C2= et C3=.The non-aromatic fraction of the aromatic complex (AC) effluents, referred to as the raffinate (stream 12), is returned, in whole or in part, to the NCC forming an additional charge to the main charge (3) of the NCC. This additional charge makes it possible to increase the final yields of light olefins C2 = and C3 =.

Les produits du NCC autre que l'éthylène ou le propylène, peuvent être recyclés dans cette même unité. On peut aussi utiliser la partie dite « dry gas », à l'exclusion de l'éthylène, et la partie dite « LPG », à l'exclusion du propylène, comme fuel gaz dans les fours du reformage catalytique (FREF).NCC products other than ethylene or propylene can be recycled in this unit. It is also possible to use the so-called "dry gas" part, excluding ethylene, and the so-called "LPG" part, excluding propylene, as fuel gas in the catalytic reforming furnaces (FREF).

Dans la figure 3, on considère une autre variante dans laquelle on recycle les paraffines en C2 et C3 ainsi que les coupes C4 et C5 issues de la séparation par boite froide (SBF) au NCC, en mélange ou séparément.In the figure 3 another variant is considered in which the C2 and C3 paraffins and the C4 and C5 cuts resulting from the cold box separation (SBF) are recycled to the NCC, in a mixture or separately.

Une autre façon de recycler les coupes C4 et C5 issues du NCC est de passer d'abord par une unité d'oligomérisation (OLG) de façon à produire des oligomères plus facilement craquables, et susceptible de produire encore plus de propylène et de l'éthylène. Cette variante est illustrée par la figure 4.Another way to recycle C4 and C5 cuts from NCC is to first pass through an oligomerization unit (OLG) to produce oligomers more easily crackable, and likely to produce even more propylene and ethylene. This variant is illustrated by the figure 4 .

Dans tous ces schémas, le train d'échange de chaleur du reforming est mis à profit pour augmenter la température du naphta léger (3) allant au NCC. Cette préchauffe de la charge du NCC permet de gagner des calories nécessaires à la balance thermique du NCC.In all these schemes, the reforming heat exchange train is used to increase the temperature of the light naphtha (3) going to the NCC. This preheating of the NCC load saves the calories needed for the thermal balance of the NCC.

Le bilan thermique du NCC est assuré par le recycle de la coupe des aromatiques lourds (HA), flux noté (11), sortant du complexe aromatique (CA). On peut définir cette coupe d'aromatiques lourds comme formée des composés à nombre d'atome de carbone supérieur à 8. Cette coupe très aromatique est une coupe fortement cokante qui va permettre de générer la quantité de coke nécessaire au bouclage du bilan thermique de l'unité NCC.The thermal balance of the NCC is ensured by the recycle of the heavy aromatics (HA) section, flow noted (11), leaving the aromatic complex (CA). This section of heavy aromatics can be defined as consisting of compounds with a carbon number greater than 8. This highly aromatic cut is a strongly cokantic cut which will make it possible to generate the quantity of coke necessary for the closure of the thermal balance of the carbon dioxide. NCC unit.

L'unité de NCC est une unité de craquage catalytique de naphta (NCC) possédant au moins un réacteur principal fonctionnant soit en flux ascendant (« riser »), soit en flux descendant (« downer »).The NCC unit is a naphtha catalytic cracking (NCC) unit having at least one main reactor operating either in riser flow or down flow.

Dans la suite on parlera de réacteur sans préciser le type d'écoulement puisque la présente invention couvre les deux modes d'écoulement possibles. Alternativement, l'unité NCC peut disposer d'un réacteur secondaire, de type « riser » ou « downer », pour craquer les recycles ou les flux additionnels séparément.In the following we will talk about reactor without specifying the type of flow since the present invention covers the two possible flow modes. Alternatively, the NCC unit may have a secondary reactor, type "riser" or "downer" to crack recycles or additional flows separately.

Elle possède une section de séparation-strippage dans laquelle le catalyseur est séparé des effluents hydrocarbonés.It has a separation-stripping section in which the catalyst is separated from the hydrocarbon effluents.

Elle possède en outre une section régénération du catalyseur dans laquelle le coke formé dans la réaction et déposé sur le catalyseur est brûlé afin de récupérer sous forme de chaleur sensible du catalyseur, une partie de la chaleur nécessaire dans le réacteur.It furthermore has a regeneration section of the catalyst in which the coke formed in the reaction and deposited on the catalyst is burned in order to recover in the form of sensible heat from the catalyst part of the heat required in the reactor.

L'unité de NCC possède sa propre section de traitement des effluents hydrocarbonés avec notamment une section de traitement des gaz permettant une séparation des oléfines légères (éthylène, propylène) des autres gaz : hydrogène, méthane, éthane, propane. Cette section de séparation est représentée par l'ensemble formé par le fractionnement des effluents (FRAC) et la boite froide de séparation des composés légers (c'est-à-dire à moins de 5 atomes de carbone) noté SBF.The NCC unit has its own hydrocarbon effluent treatment section including a gas treatment section allowing a separation of light olefins (ethylene, propylene) from other gases: hydrogen, methane, ethane, propane. This separation section is represented by the assembly formed by the fractionation of the effluents (FRAC) and the cold box of separation of the light compounds (that is to say less than 5 carbon atoms) noted SBF.

On ne décrira pas en détail cet ensemble d'unité de fractionnement bien connu de l'homme du métier.This set of fractionation unit well known to those skilled in the art will not be described in detail.

La partie plus lourde des effluents hydrocarbonés est traitée dans une section de séparation (FRAC) comprenant au moins une unité de fractionnement permettant de récupérer la coupe C6+ (flux 7) qui est envoyée au complexe aromatique (CA).The heavier portion of the hydrocarbon effluents is treated in a separation section (FRAC) comprising at least one fractionation unit for recovering the C6 + cut (stream 7) which is sent to the aromatic complex (CA).

La partie intermédiaire comprenant les hydrocarbures à 4 et 5 atomes de carbone peut être soit recyclée directement au NCC, soit être envoyée à une unité d'oligomérisation (OLG) afin d'obtenir des coupes de type polyC4/C5 dont la craquabilité (c'est-à-dire le potentiel de craquage) dans le NCC est nettement supérieure à celle des composés non oligomérisés, soit encore être valorisée vers des pools dédiés.The intermediate portion comprising the hydrocarbons with 4 and 5 carbon atoms can be either recycled directly to the NCC, or sent to an oligomerization unit (OLG) to obtain polyC4 / C5 type cuts whose crackability (c '). that is, the cracking potential) in the NCC is significantly higher than that of the non-oligomerized compounds, or still be upgraded to dedicated pools.

L'unité NCC est opérée de préférence à haute sévérité, c'est-à-dire à température de sortie réacteur élevée (ROT) et à fort rapport C/O (ratio du débit de catalyseur sur le débit de charge entrant au NCC les deux débits étant massiques).The NCC unit is operated preferably at high severity, that is to say with a high reactor output temperature (ROT) and a high C / O ratio (ratio of the catalyst flow rate to the feed rate entering the NCC the two flow rates being mass).

La gamme de conditions opératoires est donnée dans le Tableau 1 ci-dessous. Tableau 1 - Gamme des conditions opératoires de l'unité de FCC (NCC) Condition Min Max ROT, °C 500 750 C/O 5 40 The range of operating conditions is given in Table 1 below. <b> Table 1 - Operating Environment Range of the FCC Unit (NCC) </ b> Condition Low Max ROT, ° C 500 750 CO 5 40

Le catalyseur peut être tout type de catalyseur acide, avec une préférence pour un catalyseur contenant une certaine proportion de zéolithe, préférentiellement supérieure à 20% en masse du catalyseur total.The catalyst may be any type of acid catalyst, with a preference for a catalyst containing a certain proportion of zeolite, preferably greater than 20% by weight of the total catalyst.

Un catalyseur de FCC typique comportant de l'alumine, de la zéolithe Y, et de la zéolithe ZSM-5 est un exemple de catalyseur qui pourrait être utilisé.A typical FCC catalyst comprising alumina, zeolite Y, and zeolite ZSM-5 is an example of a catalyst that could be used.

EXEMPLES SELON L'INVENTIONEXAMPLES ACCORDING TO THE INVENTION

Des essais en laboratoire sur une unité simulant le NCC ont été conduits sur une coupe naphta légère très paraffinique, sur une coupe légère prélevée en sortie de l'unité de reformage catalytique, et sur une coupe aromatique représentative du flux dit "aromatiques lourds" (noté HA) provenant du complexe aromatique.Laboratory tests on a unit simulating NCC were conducted on a very paraffinic light naphtha section, on a light section taken at the outlet of the catalytic reforming unit, and on an aromatic section representative of the so-called "heavy aromatic" stream ( denoted HA) from the aromatic complex.

Les essais ont été réalisés à forte sévérité (température > 650°C et C/O > 15) afin de simuler au plus près les conditions opératoires du NCC.The tests were carried out with high severity (temperature> 650 ° C and C / O> 15) in order to simulate as closely as possible the operating conditions of the NCC.

Ces essais permettent d'établir des structures de rendement pour le craquage d'une charge de NCC.These tests make it possible to establish yield structures for cracking a load of NCC.

Pour le reformage du naphta, des conditions de sévérité permettant d'obtenir un RON autour de 95 ont été utilisées.For the reforming of naphtha, severity conditions allowing to obtain an RON around 95 were used.

Exemple 1 : Unité de FCC de Naphta (selon l'art antérieur))Example 1: FCC unit of Naphtha (according to the prior art)

Le premier exemple permet de justifier l'intérêt de la proximité du complexe aromatique et de l'unité de NCC afin d'extraire les aromatiques produits lors du craquage d'une charge type essence de distillation directe.The first example makes it possible to justify the interest of the proximity of the aromatic complex and the NCC unit in order to extract the aromatics produced during the cracking of a straight-run gasoline type feedstock.

Le Tableau 2 ci-dessous décrit la structure par famille chimique d'un naphta paraffinique dont l'intervalle de distillation est compris entre 55°C et 115°C.Table 2 below describes the chemical family structure of a paraffinic naphtha whose distillation range is between 55 ° C and 115 ° C.

Le tableau 3 suivant fournit la structure de rendement des produits issus du craquage de cette charge sur une unité pilote en riser simulé à faible temps de contact et à forte sévérité. Tableau 2 - Composition du Naphta FCC par famille d'hydrocarbures. Composition (% pds) N-Paraffines 28,10 1-Paraffines 29,98 Naphtènes 33,67 Oléfines 1,03 Di-Oléfines 0,13 Aromatiques 7,08 The following table 3 provides the yield structure of the products resulting from the cracking of this charge on a pilot unit in simulated riser with low contact time and with a high severity. <b> Table 2 - Composition of FCC Naphtha by Hydrocarbon Family. </ b> Composition (% wt) N-Paraffin 28,10 1-Paraffins 29.98 naphthenes 33.67 olefins 1.03 Di-Olefins 0.13 aromatic 7.08

Le craquage de ce naphta à haute sévérité (T=650°C, C/O=15) conduit aux rendements massiques suivants pour les molécules d'intérêt dans notre cas : Tableau 3 - Rendement principaux du craquage. Rendement (% pds) Éthylène 12,63 Propylène 18,01 Butènes 8,51 C6 Aromatique 4,31 C7 Aromatique 7,13 C8 Aromatique 2,25 Coke 0,14 The cracking of this high-grade naphtha (T = 650 ° C, C / O = 15) leads to the following mass yields for the molecules of interest in our case: <b> Table 3 - Main crack yield. </ b> Yield (% wt) Ethylene 12.63 propylene 18,01 butene 8.51 C6 Aromatic 4.31 C7 Aromatic 7.13 C8 Aromatic 2.25 Coke 0.14

Les rendements en éthylène et propylène sont nettement plus importants que pour un FCC de VGO classique. Par contre le rendement en coke et beaucoup plus faible que pour un FCC classique. Avec ce rendement plus faible en coke, un apport extérieur de chaleur au régénérateur est nécessaire, il représente même 95% de la chaleur nécessaire pour assurer un équilibre entre le réacteur et le régénérateur.The yields of ethylene and propylene are significantly higher than for a conventional VGO FCC. On the other hand, the coke yield is much lower than for a conventional FCC. With this lower coke yield, an external supply of heat to the regenerator is necessary, it even represents 95% of the heat necessary to ensure a balance between the reactor and the regenerator.

Pour un débit de charge naphta (tableau 2) de 5000 tonne/heure, les débits des différents effluents de craquage sont donnés dans le tableau 4 ci-dessous. Tableau 4 - Débits des principaux composés du NCC pour une capacité de 5000 tonne/heure. Débit (tonne/heure) Éthylène 631 Propylène 900 Butènes 426 C6 Aromatique 215 C7 Aromatique 357 C8 Aromatique 112 Coke 7 For a naphtha feedstock flow rate (Table 2) of 5000 ton / hour, the flow rates of the various cracking effluents are given in Table 4 below. <b> Table 4 - Flow rates of the main NCC compounds for a capacity of 5000 tonnes / hour. </ b> Flow rate (ton / hour) Ethylene 631 propylene 900 butene 426 C6 Aromatic 215 C7 Aromatic 357 C8 Aromatic 112 Coke 7

Exemple 2 : Unité NCC couplé à un complexe aromatique avec coupe naphta large coupée à 50-50. Example 2 : NCC unit coupled to an aromatic complex with a large cut naphtha cut at 50-50.

Afin d'illustrer les avantages de la présente invention, nous avons considéré un naphta total de point initial 55 °C, et de point final 160 °C.In order to illustrate the advantages of the present invention, we considered a total naphtha of initial point 55 ° C, and of end point 160 ° C.

La fraction distillée correspondant aux premiers 50% en poids, et dont les propriétés sont données dans le tableau 2, est envoyée au NCC dans les conditions de sévérité décrite dans l'exemple 1, alors que la partie 115 °C+ représentant environ 50% poids du total, est envoyée dans une unité de reformage catalytique.The distilled fraction corresponding to the first 50% by weight, and whose properties are given in Table 2, is sent to the NCC under the conditions of severity described in Example 1, while the 115 ° C + portion represents approximately 50% by weight. of the total, is sent to a catalytic reforming unit.

Les effluents des deux unités sont disposés tel que décrit dans la figure de l'invention 1.The effluents of the two units are arranged as described in the figure of the invention 1.

Les débits sortant des unités NCC et du complexe aromatique (CA) pour un débit total de naphta de 10000 tonne/heure sont donnés dans le tableau 5 ci-dessous. Tableau 5 - Débits des principaux composés du NCC +complexe aromatique pour une capacité de 10000 tonne/heure (5000 tonne/heure NCC, et 5000 tonne/heure pour le reforming. Débit (tonne/heure) Éthylène 717 Propylène 1110 Butènes 515 C6 Aromatique 674 C7 Aromatique 1382 C8 Aromatique 1199 Coke 98 The outflows from the NCC units and the aromatic complex (CA) for a total naphtha flow rate of 10,000 tons / hour are given in Table 5 below. <b> Table 5 - Flow rates of the main NCC compounds + aromatic complex for a capacity of 10,000 tons / hour (5000 tons / hour NCC, and 5000 tons / hour for reforming. </ b> Flow rate (ton / hour) Ethylene 717 propylene 1110 butene 515 C6 Aromatic 674 C7 Aromatic 1382 C8 Aromatic 1199 Coke 98

Par rapport à la situation de l'exemple 1 (craquage de naphta seul), les débits des oléfines légères sont nettement améliorés :

  • Ethylène augmente de 631 à 717 tonne/heure,
  • Propylène augmente de 900 à 1110 tonne/heure,
  • Butènes augmentent de 426 à 674 tonne/heure.
Compared to the situation of Example 1 (cracking of naphtha alone), the flow rates of light olefins are significantly improved:
  • Ethylene increases from 631 to 717 ton / hour,
  • Propylene increases from 900 to 1110 ton / hour,
  • Butenes increase from 426 to 674 tons / hour.

Le rendement coke du NCC est lui très nettement augmenté.The coke yield of the NCC is very much increased.

Il passe de 7 à 98 tonne/heure. Ce rendement coke permet presque d'équilibrer le bilan thermique du NCC puisque l'on passe de 95% du bouclage thermique apporté par une source extérieure au régénérateur à seulement 17%.It goes from 7 to 98 ton / hour. This coke yield almost equilibrates the thermal balance of the NCC since we go from 95% of the thermal looping brought by an external source to the regenerator to only 17%.

ExempleExample 3 : Unité NCC couplé à un complexe aromatique avec coupe naphta large coupée à 40-60.3: NCC unit coupled to an aromatic complex with a large cut naphtha cut at 40-60.

Si l'on veut établir l'équilibre thermique du NCC et augmenter la production d'aromatiques, on peut envoyer 40% du naphta totale (55 °C - 160 °C) au NCC et les 60% restant au reformage (REF).In order to establish the thermal equilibrium of the NCC and increase the production of aromatics, 40% of the total naphtha (55 ° C - 160 ° C) can be sent to the NCC and the remaining 60% to reforming (REF).

Les débits de sortie sont alors les suivants : Tableau 6 - Débits des principaux composés du NCC+complexe aromatique pour une capacité de 10000 tonne/heure (4000 tonne/heure NCC, et 6000 tonne/heure pour le reforming. Débit (tonne/heure) Éthylène 608 Propylène 972 Butènes 447 C6 Aromatique 723 C7 Aromatique 1516 C8 Aromatique 1394 Coke 115 The output rates are then as follows: <b> Table 6 - Flow rates of the main NCC + aromatic complex compounds for a capacity of 10,000 tonnes / hour (4000 tonnes / hour NCC, and 6000 tonnes / hour for reforming. </ b> Flow rate (ton / hour) Ethylene 608 propylene 972 butene 447 C6 Aromatic 723 C7 Aromatic 1516 C8 Aromatic 1394 Coke 115

Le rendement en oléfines légères (éthylène, propylène, butènes) a baissé par rapport au cas précédent (tableau 5), mais reste plus élevé que dans le cas du NCC seul (tableau 4), sauf pour l'éthylène ou l'on constate une légère baisse.The yield of light olefins (ethylene, propylene, butenes) has decreased compared to the previous case (Table 5), but remains higher than in the case of NCC alone (Table 4), except for ethylene or it is found a slight decline.

Les rendements en aromatiques sont nettement augmentés du fait que l'on a envoyé plus de charge au reforming et au complexe aromatique. Le coke du NCC continue d'augmenter puisque plus d'aromatiques lourds sont envoyés au réacteur.The yields of aromatics are markedly increased by the fact that more charge has been sent to the reforming and the aromatic complex. NCC coke continues to increase as more heavy aromatics are sent to the reactor.

Avec le rendement coke obtenu, le bilan thermique du NCC boucle sans avoir recours à une source de chaleur extérieure, ce qui représente un avantage très appréciable du point de vue du coût opératoire du procédé.With the coke yield obtained, the heat balance of the NCC loop without using an external heat source, which represents a very significant advantage from the point of view of the operating cost of the process.

Claims (7)

Procédé de production d'oléfines légères et de BTX à partir d'une coupe naphta de point initial d'ébullition supérieur à 30°C et de point final d'ébullition inférieur à 220°C, ledit procédé comprenant une unité de craquage catalytique (NCC) traitant une charge de type naphta léger (30-TM°C), une unité de reformage catalytique (REF) traitant une charge dite naphta lourd (TM°C-220°C), et d'un complexe aromatique (CA) alimenté par les effluents du reformage catalytique (REF) et la fraction 60+ des effluents du NCC, ledit procédé comportant la suite d'opérations suivantes : - On envoie la charge naphta (1) de point initial d'ébullition au moins égal à 30°C et de point final d'ébullition au moins égal à 220°C dans une unité d'hydrotraitement (HDT) qui permet d'éliminer les composés soufrés et azotés qu'elle contient, - On envoie la charge naphta hydrotraitée (2) est dans une unité de séparation (SPLIT 1) qui permet de séparer une fraction légère dite naphta léger, d'intervalle de distillation 40-TM°C, et une fraction lourde dite naphta lourd d'intervalle de distillation TM-220°C avec TM°C compris entre 80°C et 160°C, préférentiellement compris entre 100°C et 150°C, et très préférentiellement compris entre 110°C et 140°C, - On envoie le naphta léger (3) comme charge du NCC, - On envoie le naphta lourd (4) comme charge de l'unité de reformage catalytique (REF), - On sépare les effluents (6) du NCC dans une unité de fractionnement ( FRAC) qui permet de séparer une fraction légère (8) qui est envoyée dans une séparation dite boite froide (SBF) qui permet d'isoler l'H2, le CH4 et les paraffines légères en C2, C3 et C4 d'une part, et l'éthylène et le propylène d'autre part, - On envoie la fraction lourde (7) issue du séparateur (FRAC) en mélange avec les effluents (5) du reformage catalytique (REF) comme charge (10) du complexe aromatique (CA), - On extrait du complexe aromatique (CA) les BTX, un raffinat (12) défini comme la partie non aromatique des effluents, qui est envoyé au moins en partie en mélange avec le naphta léger (3) comme charge du NCC, et une fraction dite aromatiques lourds (11) qui est également envoyée en mélange avec le naphta léger (3) comme charge du NCC. A process for the production of light olefins and BTX from a boiling point naphtha section greater than 30 ° C and a boiling point of less than 220 ° C, said process comprising a catalytic cracking unit ( NCC) treating a light naphtha feedstock (30-TM ° C), a catalytic reforming unit (REF) treating a so-called heavy naphtha feedstock (TM ° C-220 ° C), and an aromatic complex (CA) supplied by the catalytic reforming effluents (REF) and the fraction 60+ of the NCC effluents, said process comprising the following sequence of operations: The naphtha feedstock (1) with an initial boiling point of at least 30 ° C. and a final boiling point of at least 220 ° C. is sent to a hydrotreating unit (HDT) which makes it possible to eliminate the sulfur and nitrogen compounds it contains, - The hydrotreated naphtha feedstock (2) is sent to a separation unit (SPLIT 1) which makes it possible to separate a light fraction called light naphtha, from a distillation interval 40-T M ° C, and a heavy fraction called heavy naphtha distillation interval T M -220 ° C with T M ° C between 80 ° C and 160 ° C, preferably between 100 ° C and 150 ° C, and very preferably between 110 ° C and 140 ° C, - The light naphtha (3) is sent as a load of the NCC, The heavy naphtha (4) is sent as a feedstock of the catalytic reforming unit (REF), - The effluents (6) are separated from the NCC in a fractionation unit (FRAC) which makes it possible to separate a light fraction (8) which is sent into a so-called cold box separation (SBF) which makes it possible to isolate the H2, the CH4 and C 2, C 3 and C 4 light paraffins on the one hand, and ethylene and propylene on the other hand, The heavy fraction (7) from the separator (FRAC) is sent in admixture with the effluents (5) of the catalytic reforming (REF) as charge (10) of the aromatic complex (CA), - The aromatic complex (CA) is extracted from the BTX, a raffinate (12) defined as the non-aromatic part of the effluents, which is sent at least partly in a mixture with the light naphtha (3) as a NCC feed, and a fraction so-called heavy aromatics (11) which is also sent as a mixture with the light naphtha (3) as the NCC feedstock. Procédé de production d'oléfines légères et de BTX à partir d'une unité de craquage catalytique (NCC) traitant une charge de type naphta léger (30-TM°C), d'une unité de reformage catalytique (REF) traitant une charge dite naphta lourd (TM°C-220°C), et d'un complexe aromatique (CA) alimenté par les effluents du reformage catalytique (REF) et la fraction 60+ des effluents du NCC, selon la revendication 1, dans lequel l'effluent raffinat (12) du complexe aromatique est envoyé dans une unité de séparation (SPLIT2) qui permet de séparer une fraction légère (13) qui est envoyée en mélange avec la charge naphta léger (3) à l'unité de craquage catalytique (NCC), et une fraction lourde (14) qui est envoyée en mélange avec la charge naphta lourd (4) à l'unité de reformage catalytique (REF).Process for producing light olefins and BTX from a catalytic cracking unit (NCC) treating a light naphtha feedstock (30-TM ° C), a catalytic reforming unit (REF) treating a feedstock so-called heavy naphtha (TM ° C-220 ° C), and an aromatic complex (CA) fed by the catalytic reforming effluents (REF) and the fraction 60+ of the NCC effluents, according to claim 1, wherein effluent raffinate (12) from the aromatic complex is fed to a separation unit (SPLIT2) which separates a light fraction (13) which is mixed with the light naphtha feedstock (3) to the catalytic cracking unit ( NCC), and a heavy fraction (14) which is mixed with the heavy naphtha feed (4) to the catalytic reforming unit (REF). Procédé de production d'oléfines légères et de BTX à partir d'une unité de craquage catalytique (NCC) selon la revendication 2, dans lequel les paraffines légères de C2 à C5 produite comme effluents du NCC à partir de la boite de séparation (BF) sont envoyées en mélange avec la charge naphta léger (3) vers l'unité de craquage catalytique NCC.A process for producing light olefins and BTX from a catalytic cracking unit (NCC) according to claim 2, wherein the C2 to C5 light paraffins produced as NCC effluents from the separation box (BF) ) are mixed with the light naphtha feedstock (3) to the NCC catalytic cracking unit. Procédé de production d'oléfines légères et de BTX à partir d'une unité de craquage catalytique (NCC) selon la revendication 3, dans lequel les oléfines légères en C4 et C5 sont envoyées dans une unité d'oligomérisation (OLG), et les effluents de ladite unité d'oligomérisation sont envoyés en mélange avec la charge naphta léger (3) dans l'unité de craquage catalytique (NCC).A process for producing light olefins and BTX from a catalytic cracking unit (NCC) according to claim 3, wherein the C4 and C5 light olefins are sent to an oligomerization unit (OLG), and the Effluents of said oligomerization unit are mixed with the light naphtha feedstock (3) in the catalytic cracking unit (NCC). Procédé de production d'oléfines légères et de BTX à partir d'une unité de craquage catalytique (NCC) traitant une charge naphta léger (30-TM°C), d'une unité de reformage catalytique (REF) traitant une charge dite naphta lourd (TM°C-220°C), et d'un complexe aromatique (CA) alimenté par les effluents du reformage catalytique et la fraction 60+ des effluents du NCC, selon l'une quelconque des revendications 1 à 4, dans lequel la coupe naphta léger (3) issue du fractionnement (SPLIT1) est préchauffée dans la zone de convection des fours de reformage catalytique (FREF) avant d'être introduite comme charge de l'unité de craquage catalytique (NCC).Process for the production of light olefins and BTX from a catalytic cracking unit (NCC) treating a light naphtha feed (30-T M ° C), a catalytic reforming unit (REF) treating a so-called heavy naphtha (T M ° C-220 ° C), and an aromatic complex (CA) fed by the catalytic reforming effluents and the fraction 60+ of the NCC effluents, according to any one of claims 1 to 4, wherein the light fraction naphtha fraction (3) from the fractionation (SPLIT1) is preheated in the convection zone of the catalytic reforming furnaces (FREF) before being introduced as a feedstock of the catalytic cracking unit (NCC). Procédé de production d'oléfines légères et de BTX à partir d'une unité de craquage catalytique (NCC), selon l'une quelconque des revendications 1 à 5, dans lequel les conditions opératoires du NCC sont les suivantes ; température de sortie du réacteur comprise entre 500°C et 750°C, et rapport du débit massique de catalyseur sur le débit massique de charge (C/O) est compris entre 5 et 40.A process for producing light olefins and BTX from a catalytic cracking unit (NCC) according to any one of claims 1 to 5, wherein the operating conditions of the NCC are as follows; reactor outlet temperature of between 500 ° C and 750 ° C, and ratio of mass flow rate of catalyst to mass flow rate (C / O) is between 5 and 40. Procédé de production d'oléfines légères et de BTX à partir d'une unité de craquage catalytique (NCC), selon l'une quelconque des revendications 1 à 6, dans lequel le catalyseur utilisé dans l'unité NCC comprend une proportion de zéolithe ZSM-5 au moins égal à 10% en poids par rapport au catalyseur total.A process for the production of light olefins and BTX from a catalytic cracking unit (NCC) according to any one of claims 1 to 6, wherein the catalyst used in the NCC unit comprises a proportion of zeolite ZSM At least equal to 10% by weight relative to the total catalyst.
EP15305502.5A 2014-04-07 2015-04-03 Method for producing light olefins and btx using an ncc catalytic cracking unit treating a naphtha feedstock, with a catalytic reformer unit and an aromatic complex Active EP2930226B1 (en)

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