Catalytic reforming process with recovery of non-aromatic effluents

Abstract

According to a first aspect, the present invention relates to a process and apparatus for the production of aromatic compounds, in which the raffinate (16) from an aromatic extraction unit (14) is sent to a dedicated catalytic reforming unit (17) to produce a reformate effluent (18), which is successively treated by: a recontacting section (4) to separate hydrogen (5); a stabilization section (7) to separate C1-C2 hydrocarbon compounds (8) and C3-C4 or C3-C5 hydrocarbon compounds (9); and a reformate separation column (11) to separate a C6-C8 fraction (12) and a C8+ fraction (13), the C6-C8 fraction (12) being sent back to the aromatic extraction unit (14). The present invention also relates to a method for modifying an existing apparatus for the production of aromatic compounds, comprising installing the process according to the first aspect in the existing apparatus. Figure 1 to be published

Description

Title of the invention: Catalytic reforming process with recovery of non-aromatic effluents technical field

[0001] The present invention relates to the field of processes for the production of aromatic compounds, and more particularly, aromatic compounds of the benzene, toluene and xylene type by catalytic reforming of a hydrocarbon feedstock of the naphtha type. Previous technique

[0002] Generally, the objective of a catalytic reforming unit is to convert naphthenic and paraffinic compounds (n-paraffins and iso-paraffins) into aromatic compounds. The main reactions involved are the dehydrogenation of naphthenes and the dehydrocyclization of paraffins into aromatics, and the isomerization of paraffins and naphthenes. Other so-called "side" reactions can also occur, such as the hydrocracking and hydrogenolysis of paraffins and naphthenes, the hydro-dealkylation of alkyl-aromatics giving rise to lighter compounds and lighter aromatics, as well as the formation of coke on the surface of the catalysts.

[0003] The feedstocks typically sent to a catalytic reforming unit are rich in paraffinic and naphthenic compounds and relatively poor in aromatic compounds. They are generally naphthas from crude oil distillation or natural gas condensates. Other feedstocks may also be available, containing varying levels of aromatics, namely heavy naphthas from catalytic cracking, coking, hydrocracking, or steam cracking.

[0004] For a petrochemical application, the desired performance characteristics are the aromatic yield and the distribution of the aromatics produced. Aromatic compounds are generally processed in an aromatic complex to promote the production of one or more aromatic compounds, most often xylenes (in particular paraxylene) and benzene. An aromatic complex is an aromatic production unit comprising, for example, separation sections (e.g., distillation, adsorption / desorption, crystallization) and optionally transformation sections (e.g., isomerization, transalkylation) for the production of aromatic compounds, particularly paraxylene. Toluene and heavier aromatics can be used in the formation of gasoline base oils or in the production of xylene blends.The production of C6-C7 aromatic compounds allows, in particular, for the improvement of gasoline octane rating and / or increases the supply of benzene, toluene, and xylenes. In order to maximize the production of aro compounds... C6-C7 matics by catalytic reforming, the presence of a specific catalytic system generally comprising a catalytically active metal (usually platinum) and a non-acidic zeolite is used.

[0005] A conventional catalytic reforming scheme for the production of aromatics, without valorization of the raffinate from the extraction of aromatics, from a naphtha-type feedstock, comprises the following steps: - a stream of naphtha is sent into a reforming unit, generating an effluent; - the effluent is sent into a reformat separation column, thus creating a headflow and a bottomflow; - the head stream is sent into an aromatic compound purification unit, creating a purified aromatics stream including C6 and C7 aromatic compounds, and a raffinate stream.

[0006] There are many other known processes aimed at increasing the production of C6-C7 aromatic compounds from the conventional process. For example, US patent application 2012 / 0277505 describes the conventional process mentioned above in which the raffinate stream is recycled in the reforming unit.

[0007] US patent application US2012 / 0277505 also describes a process for improving the production of benzene and toluene from a naphtha-type feedstock comprising the following steps: - a stream of naphtha is sent into a fractionation unit, generating a first stream comprising C7 and lighter hydrocarbons, and a second stream comprising heavier hydrocarbons; - the first stream is sent to a first reforming unit generating a first effluent; - the second stream is sent to a second reforming unit, at a temperature higher than the temperature applied in the first reforming unit, generating a second effluent; - the first effluent and the second effluent are sent into a reformat separation column, thus creating a headflow and a bottomflow; - the head stream is sent into an aromatic compound purification unit, creating a purified aromatics stream including C6 and C7 aromatic compounds, and a raffinate stream; - the refining stream is recycled in the first reforming unit.

[0008] Such processes allow for increased production of aromatic hydrocarbons, and in particular benzene and toluene, from a naphtha feed stream. More specifically, the raffinate recycling step and the repositioning of the aromatics extraction unit relative to the catalytic reforming units located in parallel allows to generate a 25% increase in benzene yields and an increase of about 10% in toluene yields.

[0009] However, although these processes aim to increase the production of C6-C7 aromatic compounds, xylene production can be improved. Furthermore, the proposed improvements are often poorly suited for modifying existing units, as the existing aromatic complex lacks sufficient capacity to process new aromatic compounds. Summary of the invention

[0010] In the context described above, a first object of this description is to overcome the problems of the prior art and to provide a catalytic reforming process and device for increasing the production of benzene and toluene. A second object of this description is to provide a catalytic reforming process and device that can be implemented in an existing complex without modifying existing facilities, particularly with a view to increasing the production of benzene and xylenes.

[0011] According to a first aspect, the aforementioned objects, as well as other advantages, are obtained by a process for producing aromatic compounds, such as 6-8 carbon atom aromatics (A6-A8), and in particular xylenes, from a feedstock of hydrocarbon compounds, comprising the following steps: - a first load of C6-C8 hydrocarbon compounds is sent to an aromatics extraction unit to produce an extract comprising aromatic compounds of 6 to 8 carbon atoms and a raffinate comprising aliphatic compounds of 6 to 8 carbon atoms; - the raffinate is sent to a first dedicated catalytic reforming unit to produce a first reformate effluent; - the first reformat effluent is sent to a first recontacting section to separate a first gaseous effluent rich in hydrogen and a first liquid effluent of hydrocarbons; - the first liquid hydrocarbon effluent is sent to a first stabilization section to separate a first gaseous effluent of hydrocarbon compounds including C1-C2 hydrocarbon compounds, a first liquid stream including C3-C4 or C3-C5 hydrocarbon compounds, and a first liquid fraction including hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms; - The first liquid fraction is sent to a first reformat separation column to separate a first C6-C8 fraction comprising C6-C8 hydrocarbon compounds, and a first C8+ fraction comprising hy- compounds drocarbons with at least 8 carbon atoms; - the first C6-C8 fraction is sent at least in part to the aromatics extraction unit.

[0012] According to one or more embodiments, the process includes sending the extract and the first C8+ fraction to an aromatics production unit (aromatic complex).

[0013] According to one or more embodiments, the raffinate is sent to a first dedicated hydrotreatment unit to produce a first hydrotreated effluent sent to the first catalytic reforming unit.

[0014] According to one or more embodiments, the first C6-C8 fraction comprises C5 hydrocarbon compounds, and / or a first head fraction comprising C5 hydrocarbon compounds is separated in the first reformat separation column.

[0015] According to one or more embodiments, the first C6-C8 hydrocarbon compound charge comprises at least 50% by weight, preferably at least 60% by weight, very preferably at least 70% by weight of aromatic compounds.

[0016] According to one or more embodiments, the first catalytic reforming unit comprises at least one reforming reactor used according to at least one of the following operating conditions: - a temperature between 400°C and 600°C, preferably between 470°C and 570°C; - a pressure between 0.1 MPa and 3 MPa, preferably between 0.3 MPa and 2.5 MPa; - a molar ratio between hydrogen and hydrocarbon compounds of between 0.8 and 8 mole / mol; and - a mass flow rate of treated flux per unit mass of catalyst and per hour of between 0.1 h 1 and 10 h1, preferably between 0.5 h 1 and 6 h1. - optional catalyst comprising: an active phase comprising: at least one metal selected from platinum, zinc or molybdenum, preferably platinum; a support comprising a zeolite, preferably a zeolite selected from zeolite L, zeolite X, zeolite Y, zeolite ZSM-5; and optionally a binder selected from aluminosilicate, alumina, silica, clays, silicon carbides, taken alone or in combination.

[0017] According to one or more embodiments, the process comprises the following steps: - a second hydrocarbon feedstock is sent to a second catalytic reforming unit to produce a second reformat effluent; - the second reformat effluent is sent to a second re- section contacting to produce a second hydrogen-rich gaseous effluent and a second liquid hydrocarbon effluent; - the second liquid hydrocarbon effluent is sent to a second stabilization section to separate a second gaseous hydrocarbon compound effluent comprising C1-C2 hydrocarbon compounds, a second liquid stream comprising C3-C4 or C3-C5 hydrocarbon compounds, and a second liquid fraction comprising hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms; - the second liquid fraction is sent to a second reformat separation column to separate a second C6-C8 fraction and a second C8+ fraction comprising hydrocarbon compounds with at least 8 carbon atoms; - the second C6-C8 fraction is sent to the aromatics extraction unit as said first C6-C8 hydrocarbon compound feed.

[0018] According to one or more embodiments, the process comprises the following steps: - a second hydrocarbon feedstock is sent to a second catalytic reforming unit to produce a second reformat effluent; - the second reformat effluent is sent to a second re-contacting section to produce a second hydrogen-rich gaseous effluent and a second liquid hydrocarbon effluent; - the second liquid hydrocarbon effluent is sent to a second stabilization section to separate a second gaseous hydrocarbon compound effluent comprising C1-C2 hydrocarbon compounds, a second liquid stream comprising C3-C4 or C3-C5 hydrocarbon compounds, and a second liquid fraction comprising hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms; - the second liquid fraction is sent to the first reformat separation column.

[0019] According to one or more embodiments, the process comprises the following steps: - a second hydrocarbon feedstock is sent to a second catalytic reforming unit to produce a second reformat effluent; - the second reformat effluent is sent to a second re-contacting section to produce a second hydrogen-rich gaseous effluent and a second liquid hydrocarbon effluent; - the second liquid hydrocarbon effluent is sent to the first stabilization section.

[0020] According to one or more embodiments, the process comprises the steps following: - a second hydrocarbon feedstock is sent to a second catalytic reforming unit to produce a second reformat effluent; - we send the second reformat effluent at least in part into the first recontacting section.

[0021] According to one or more embodiments, the process includes sending the second C8+ fraction at least in part to an aromatics production unit.

[0022] According to one or more embodiments, the second hydrocarbon feed is sent to a second dedicated hydrotreatment unit to produce a second hydrotreated effluent sent to the second catalytic reforming unit.

[0023] According to one or more embodiments, the second hydrocarbon charge comprises naphtha.

[0024] According to a second aspect, the aforementioned objects, as well as other advantages, are obtained by a process of modifying a device for producing aromatic compounds, such as 6-8 carbon atom aromatics (A6-A8), and in particular xylenes, from a feed of hydrocarbon compounds, the aromatic compound production device comprising: - a second catalytic reforming unit adapted to process a second hydrocarbon feedstock and produce a second reformat effluent; - a second recontacting section adapted to treat the second reformat effluent and produce a second hydrogen-rich gaseous effluent and a second liquid hydrocarbon effluent; - a second stabilization section adapted to treat the second liquid hydrocarbon effluent and separate a second gaseous hydrocarbon compound effluent comprising C1-C2 hydrocarbon compounds, a second liquid stream comprising C3-C4 or C3-C5 hydrocarbon compounds, and a second liquid fraction comprising hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms; - a second reformat separation column adapted to process the second liquid fraction and separate a second C6-C8 fraction and a second C8+ fraction comprising hydrocarbon compounds with at least 8 carbon atoms; - an aromatics extraction unit adapted to process the second C6-C8 fraction and produce an extract comprising aromatic compounds of 6 to 8 carbon atoms and a raffinate comprising aliphatic compounds of 6 to 8 carbon atoms, The process includes the following steps: - a first a dedicated catalytic reforming unit adapted to process the raffinate, produce a first reformate effluent, and send the first reformate effluent to the second recontacting section or a dedicated first recontacting section; - optionally, the first dedicated recontacting section adapted to process the first reformate effluent, separate a first hydrogen-rich gaseous effluent and a first liquid hydrocarbon effluent, and send the first liquid hydrocarbon effluent to the second stabilization section or a dedicated first stabilization section is installed in the aromatic compound production device; - optionally, the first dedicated stabilization section adapted to treat the first liquid hydrocarbon effluent is installed in the aromatic compound production device, separating a first gaseous hydrocarbon compound effluent comprising C1-C2 hydrocarbon compounds, a first liquid stream comprising C3-C4 or C3-C5 hydrocarbon compounds, and a first liquid fraction comprising hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms, and sending the first liquid fraction to the second reformat separation column or a dedicated first reformat separation column; - Optionally, the first dedicated reformat separation column adapted to process the first liquid fraction is installed in the aromatic compound production device, separating a first C6-C8 fraction comprising C6-C8 hydrocarbon compounds, and a first C8+ fraction comprising hydrocarbon compounds with at least 8 carbon atoms, and sending at least part of the first C6-C8 fraction to the aromatic extraction unit.

[0025] According to a third aspect, the aforementioned objects, as well as other advantages, are obtained by a device for producing aromatic compounds, such as 6-8 carbon atom aromatics (A6-A8), and in particular xylenes, from a feed of hydrocarbon compounds, the device comprising: an aromatics extraction unit adapted to process a first load of C6-C8 hydrocarbon compounds to produce an extract comprising aromatic compounds of 6 to 8 carbon atoms and a raffinate comprising aliphatic compounds of 6 to 8 carbon atoms; - a first dedicated catalytic reforming unit adapted to treat the raffinate and produce a first reformate effluent; - a first recontacting section adapted to treat the first reformat effluent and separate a first hydrogen-rich gaseous effluent and a first liquid hydrocarbon effluent; - a first stabilization section adapted to treat the first liquid effluent of hydrocarbons and separate a first gaseous effluent of hydrocarbon compounds comprising C1-C2 hydrocarbon compounds, a first liquid stream comprising C3-C4 or C3-C5 hydrocarbon compounds, and a first liquid fraction comprising hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms; - a first reformat separation column adapted to process the first liquid fraction, separate a first C6-C8 fraction comprising C6-C8 hydrocarbon compounds and a first C8+ fraction comprising hydrocarbon compounds with at least 8 carbon atoms, and send the first C6-C8 fraction at least in part to the aromatics extraction unit.

[0026] Embodiments of the invention according to the aforementioned aspects, as well as other features and advantages, will become apparent from the following description, given solely for illustrative purposes and not for limitation, and with reference to the following drawing. List of figures

[0027] Fig. 1 is a simplified schematic representation of the process for producing aromatic compounds according to the invention.

[0028] Fig. 2 is a simplified schematic representation of the process of producing aromatic compounds according to Fig. 1 in parallel with a conventional reforming.

[0029] Fig. 3 is a simplified schematic representation of the aromatic compound production process according to Fig. 2 with a shared reformat separation column.

[0030] Fig. 4 is a simplified schematic representation of the process for producing aromatic compounds according to Fig. 3 with a shared stabilization section.

[0031] Fig. 5 is a simplified schematic representation of the aromatic compound production process according to Fig. 4 with a shared recontacting section. Description of the implementation methods

[0032] The present invention relates to a process for producing aromatic compounds, such as 6-8 carbon atom aromatics (A6-A8), and in particular xylenes, from a feed of hydrocarbon compounds.

[0033] With reference to [Fig. 1], according to the invention, the process comprises the following steps: - a first load of C6-C8 hydrocarbon compounds 24 is sent into an aromatics extraction unit 14 to form an extract 15 comprising (mostly, preferably essentially) aromatic compounds of 6 to 8 carbon atoms, and a raffinate 16 comprising (mostly, preferably essentially) aliphatic compounds of 6 to 8 carbon atoms; - the raffinate 16 is sent to a first dedicated catalytic reforming unit 17 to obtain a first effluent of reformat 18; - the first reformat 18 effluent is sent into a first re-contacting section 4 (optionally dedicated) to obtain a first hydrogen-rich gaseous effluent 5 (richer in hydrogen compared to the first reformat 18 effluent) and a first liquid hydrocarbon effluent 6 (less rich in hydrogen compared to the first reformat 18 effluent); - the first liquid hydrocarbon effluent 6 is sent into a first stabilization section 7 (optionally dedicated) to separate a first gaseous hydrocarbon compound effluent 8 comprising C1-C2 hydrocarbon compounds (relative to the hydrocarbon effluent), a first liquid stream 9 (or LPG for Liquefied Petroleum Gas) comprising (mostly, preferably essentially) C3-C4 or C3-C5 hydrocarbon compounds, and a first liquid fraction 10 (stabilized) comprising (mostly, preferably essentially) hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms; - the first liquid fraction 10 is sent into a first reformat separation column 11 (optionally dedicated) to separate a first C6-C8 fraction 12 comprising (mostly, preferably essentially) C6-C8 hydrocarbon compounds, and a first C8+ fraction 13 comprising (mostly, preferably essentially) C8+ hydrocarbon compounds; - we send the first fraction in C6-C8 12 at least in part to the aromatics extraction unit 14.

[0034] According to one or more embodiments, the raffinate 16 is sent to a first dedicated hydrotreating unit 21 (for example for the removal of sulfur, nitrogen, olefins) to produce a first hydrotreated effluent 22 sent to the first catalytic reforming unit 17 (in place of the raffinate 16).

[0035] According to one or more embodiments, the first reformat separation column 11 is adapted to separate a first head fraction 25 comprising (mostly, preferably essentially) C5 hydrocarbon compounds. According to one or more embodiments, the first reformat separation column 11 is adapted to send the C5 hydrocarbon compounds to the aromatics extraction unit 14 along with the first C6-C8 fraction 12.

[0036] According to one or more embodiments, the process further comprises sending the extract 15 and the first C8+ fraction 13 (preferably separately) to an aromatics production unit (aromatic complex), for example, for the production of xylenes (preferably paraxylene) and optionally benzene. According to one or more embodiments, the extract 15 is sent to a benzene and toluene fractionation section of the aromatic complex, and the first fraction in C8+ 13 in a fractionation section of aromatic compounds in C8 and C9 of the aromatic complex.

[0037] In this description, the term "recontacting section" refers to a section comprising an operation for extracting compounds from a gaseous phase using a liquid phase with absorbing properties, achieved through contact between the two phases. For example, recontacting can be accomplished by direct in-line mixing of the liquid and gaseous phases or in a recontacting device dedicated to this unit operation.

[0038] The term "majority" in this description means that the stream in question comprises, by weight, at least 50% of the components in question. The term "essentially" throughout this text means that the stream in question comprises, by weight, at least 80%, in particular at least 90% or 95%, preferably at least 99% or 99.5% of said components. It may also refer to all of the components in question, excluding the usual impurities.

[0039] The term "dedicated" in this description means that the so-called "dedicated" unit processes only the effluent in question. For example, in the process according to the present invention, the first dedicated catalytic reforming unit 17 processes only the raffinate 16.

[0040] The term "stabilized" in this description means that the liquid fraction has been distilled to remove compounds with 4 or fewer carbon atoms (C4-), for example to contain essentially no C4- compounds.

[0041] In this description, the term "Cn hydrocarbon cut" means a cut comprising hydrocarbons with n carbon atoms. A Cn+ cut means a cut comprising hydrocarbons with at least n carbon atoms. A Cn- cut means a cut comprising hydrocarbons with at most n carbon atoms.

[0042] With reference to [Fig.2], according to one or more embodiments, the process comprises the following steps: - a second hydrocarbon feed 1 is sent into a second catalytic reforming unit 2 (dedicated) to obtain a second reformat effluent 3; - the second reformat effluent 3 is sent into a second recontacting section 26 (optionally dedicated) to obtain a second hydrogen-rich gaseous effluent 27 (relative to the second reformat effluent 3) and a second liquid hydrocarbon effluent 28; - The second liquid hydrocarbon effluent 28 is sent to a second stabilization section 29 (optionally dedicated) to separate a second gaseous hydrocarbon compound effluent 30 comprising C1-C2 hydrocarbon compounds (relative to the hydrocarbon effluent), a second liquid stream 31 (or LPG) for Liquefied Petroleum Gas) comprising (mostly, preferably essentially) C3-C4 or C3-C5 hydrocarbon compounds, and a second liquid fraction 32 (stabilized) comprising (mostly, preferably essentially) hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms; - the second liquid fraction 32 is sent to a second reformat separation column 33 (optionally dedicated) to separate a second C6-C8 fraction 34, and a second C8+ fraction 23 comprising (mostly, preferably essentially) C8+ hydrocarbon compounds; - the second C6-C8 fraction 34 is sent to the aromatics extraction unit 14 as said first C6-C8 hydrocarbon compound load 24.

[0043] It is understood that the terms "first" and "second" used in this description are present simply to differentiate the different units and effluents of the process according to the present invention. For example, when modifying an existing production device ("revamping" according to Anglo-Saxon terminology), the reformat separation column of the existing production device can be considered as the "first" reformat separation column (modification without the addition of an additional reformat separation column) or the "second" reformat separation column (modification with the addition of an additional reformat separation column).The same applies to the stabilization (and optionally re-contacting) section of the existing production device, which can be considered as the "first" stabilization section (modification without adding an additional stabilization section) or the "second" stabilization section (modification with adding an additional stabilization section).

[0044] According to one or more embodiments, the second hydrocarbon feed 1 is sent to a second dedicated hydrotreating unit 19 (dedicated) (for example for removal of sulfur, nitrogen, olefins) to produce a second hydrotreated effluent 20 sent to the second catalytic reforming unit 2 (in place of the second hydrocarbon feed 1).

[0045] According to one or more embodiments, the second reformat separation column 33 is adapted to separate a second head fraction 35 comprising (mostly, preferably essentially) C5 hydrocarbon compounds. According to one or more embodiments, the second reformat separation column 33 is adapted to send the C5 hydrocarbon compounds to the aromatics extraction unit 14 along with the second C6-C8 fraction 34.

[0046] According to one or more embodiments, the method further comprises sending the second C8+ 23 fraction at least partially in the aromatic complex. According to one or more embodiments, the second C8+ 23 fraction is sent to the C8 and C9 aromatic compound fractionation section of the aromatic complex, for example mixed with the first C8+ 13 fraction.

[0047] According to the invention, the first C6-C8 hydrocarbon compound charge comprises (consists of) aromatic compounds of 6 to 8 carbon atoms (e.g., benzene and toluene) and non-aromatic compounds of 6 to 8 carbon atoms (e.g., aliphatic compounds such as paraffinic and naphthenic compounds). In one or more embodiments, the first C6-C8 hydrocarbon compound charge comprises at least 50% by weight, preferably at least 60% by weight, and most preferably at least 70% by weight of aromatic compounds. In one or more embodiments, the first C6-C8 hydrocarbon compound charge comprises between 55% by weight and 95% by weight, preferably between 60% by weight and 90% by weight, such as, for example, between 65% by weight and 85% by weight of aromatic compounds.According to one or more embodiments, the first C6-C8 hydrocarbon compound load comprises less than 50% by weight, preferably less than 60% by weight, and very preferably less than 70% by weight, of non-aromatic compounds. According to one or more embodiments, the first C6-C8 hydrocarbon compound load comprises between 5% by weight and 45% by weight, preferably between 10% by weight and 40% by weight, such as, for example, between 15% by weight and 35% by weight, of non-aromatic compounds. According to one or more embodiments, the first C6-C8 hydrocarbon compound load comprises (mostly, preferably essentially) C6-C7 hydrocarbon compounds and optionally C5 hydrocarbon compounds. According to one or more embodiments, the first C6-C8 hydrocarbon compound load is substantially free of sulfur, nitrogen, and oxygen compounds.

[0048] According to one or more embodiments, the second hydrocarbon feed 1 comprises (consists of) naphtha, for example, naphtha with an initial distillation temperature greater than or equal to 30°C and a final distillation temperature less than or equal to 220°C (at atmospheric pressure). According to one or more embodiments, the second hydrocarbon feed 1 comprises mainly C6 to C10 hydrocarbons and optionally C5 hydrocarbon compounds. According to one or more embodiments, the naphtha cut comprises essentially C6 to C10 hydrocarbons. According to one or more embodiments, the second hydrocarbon feed 1 comprises mainly hydrocarbons with an initial distillation temperature between 70°C and 90°C or between 80°C and 100°C and a final distillation temperature between 150°C and 220°C. According to one or more embodiments, the second hydrocarbon feed 1 comprises essentially hydrocarbons with an initial distillation temperature between 80°C and 100°C and a final distillation temperature between 150°C and 220°C. In one or more embodiments, the second hydrocarbon feed 1 comprises at least 40% paraffinic and / or naphthenic compounds. In one or more embodiments, the second hydrocarbon feed 1 comprises at least 80% paraffinic and / or naphthenic compounds. In one or more embodiments, the second hydrocarbon feed 1 comprises less than 20% aromatic compounds.

[0049] According to one or more embodiments, raffinate 16 comprises predominantly aliphatic compounds of 6 to 8 carbon atoms (e.g., non-aromatic compounds such as paraffinic and naphthenic compounds). According to one or more embodiments, raffinate 16 comprises less than 70% by weight, preferably less than 80% by weight, and very preferably less than 90% by weight of aromatic compounds. According to one or more embodiments, raffinate 16 comprises essentially non-aromatic compounds of 6 to 8 carbon atoms. According to one or more embodiments, raffinate 16 comprises (predominantly, preferably essentially) C6-C7 aliphatic compounds and optionally C5 aliphatic compounds.

[0050] A first, non-limiting example of the process according to the invention is shown in [Fig. 1], wherein the first C6-C8 hydrocarbon compound feedstock 24 is sent to the aromatics extraction unit 14 to form the extract 15 (a stream of aromatic compounds with 6 to 8 carbon atoms) and the raffinate 16 (a stream of aliphatic compounds with 6 to 8 carbon atoms). The raffinate 16 is sent to the first optional hydrotreating unit 21 to produce the first hydrotreated effluent 22, which is sent to the first catalytic reforming unit 17. The first reformate effluent 18 from the first catalytic reforming unit 17 is sent to the first recontacting section 4 to form the first hydrogen-rich gaseous effluent 5 and the first liquid hydrocarbon effluent 6.The first liquid hydrocarbon effluent 6 is sent to the first stabilization section 7 to recover the first gaseous hydrocarbon compound effluent 8 enriched in Cl and C2 hydrocarbons, the first liquid stream 9 comprising liquefied petroleum gas (LPG), and the first liquid fraction 10 containing predominantly hydrocarbons with at least 4 or 5 carbon atoms. The first liquid fraction 10 is sent to the first reformate separation column 11 to obtain the first C6-C8 fraction 12 comprising C6 to C8 compounds, the first C8+ fraction 13 (e.g., bottom stream) comprising C8+ aromatic compounds, and optionally the first overhead fraction 25 (C5 compounds). According to one or more embodiments, the first C6-C8 fraction 12 comprises (predominantly, preferably essentially) hydrocarbon compounds. C6-C7 and possibly C5 hydrocarbon compounds. The first C6-C8 fraction 12 is sent to the aromatics extraction unit 14 and the first C8+ fraction 13 is sent to an aromatic complex.

[0051] A second non-limiting example of the process according to the invention is shown in [Fig.2], in which the second hydrocarbon feed 1 of the naphtha type comprising C6 hydrocarbons with C10 is sent to the second optional hydrotreating unit 19 and then the second hydrotreated effluent 20 is sent to the second catalytic reforming unit 2. The second reformat effluent 3 from the second catalytic reforming unit 2 is sent to the second recontacting section 26 in order to form the second hydrogen-rich gaseous effluent 27, and the second liquid hydrocarbon effluent 28.The second liquid hydrocarbon effluent 28 is sent to the second stabilization section 29 to recover the second gaseous hydrocarbon compound effluent 30 enriched in Cl and C2 hydrocarbons, the second liquid stream 31 comprising liquefied petroleum gas (LPG), and the second liquid fraction 32 containing predominantly hydrocarbons with at least 4 or 5 carbon atoms. The second liquid fraction 32 is sent to the second reformat separation column 33 to obtain the second C6-C8 fraction 34 comprising C6 to C8 compounds and the second C8+ fraction 23 (e.g., bottom stream) comprising C8+ aromatic compounds. According to one or more embodiments, the second C6-C8 fraction 34 comprises (predominantly, preferably essentially) C6-C7 hydrocarbon compounds and optionally C5 hydrocarbon compounds.The second C6-C8 fraction 34 is sent to the aromatics extraction unit 14 in place of the first C6-C8 hydrocarbon compound load 24.

[0052] According to one or more embodiments, the first catalytic reforming unit 17 and / or the second catalytic reforming unit 2 comprises at least one reforming reactor used according to at least one of the following operating conditions: - a temperature between 400°C and 600°C, preferably between 470°C and 570°C; - a pressure between 0.1 MPa and 3 MPa, preferably between 0.3 MPa and 2.5 MPa; - a molar ratio between hydrogen and hydrocarbon compounds of between 0.8 and 8 mole / mol; and - a mass flow rate of treated flux per unit mass of catalyst and per hour of between 0.1 h 1 and 10 h1, preferably between 0.5 h 1 and 6 h1, such as between 1 h 1 and 5 h1.

[0053] According to one or more embodiments, the first catalyst used in the first catalytic reforming unit 17 comprises an active phase comprising at less a metal chosen from platinum, zinc or molybdenum, and a support comprising a zeolite, and possibly a binder. Preferably, the metal is platinum.

[0054] According to one or more embodiments, the first catalyst contains an amount of metal of between 0.02 and 2% by weight, preferably between 0.05 and 1.5% by weight, even more preferably between 0.1 and 0.8% by weight relative to the total weight of the first catalyst.

[0055] According to one or more embodiments, the zeolite of the support of the first catalyst is chosen from an L zeolite, an X zeolite, a Y zeolite, a ZSM-5 zeolite. More preferably, the zeolite is an L zeolite.

[0056] According to one or more embodiments, the binder of the first catalyst is chosen from aluminosilicate, alumina, silica, clays, silicon carbides, taken alone or in combination. More preferably, the binder is silica.

[0057] According to one or more embodiments, the first catalyst comprises an active phase comprising platinum, a support comprising a zeolite L, and optionally a silica-type binder.

[0058] According to one or more embodiments, the second catalyst used in the second catalytic reforming unit 2 comprises an active phase including at least one metal selected from nickel, ruthenium, rhodium, palladium, iridium, or platinum, at least one promoter selected from rhenium, tin, germanium, cobalt, nickel, iridium, rhodium, or ruthenium, and a support based on alumina, silica-alumina, or silica. Preferably, the second catalyst comprises an active phase including platinum and tin.

[0059] According to one or more embodiments, the second catalyst contains an amount of at least one metal (e.g. platinum) of between 0.02 and 2% by weight, preferably between 0.05 and 1.5% by weight, even more preferably between 0.1 and 0.8% by weight relative to the total weight of the second catalyst.

[0060] According to one or more embodiments, the support for the second catalyst is alumina-based. According to one or more embodiments, at least one alumina in the porous support used in the second catalyst is of the chi, eta, gamma, or delta type. Preferably, at least one alumina in the porous support is of the gamma or delta type. Even more preferably, at least one alumina in the porous support is of the gamma type.

[0061] The second catalyst may also include at least one dopant metal selected from the group consisting of gallium, gold, nickel, rhenium, barium, silver, iron, bismuth, indium, yttrium, and the lanthanides (cerium, dysprosium, ytterbium), taken alone or in mixtures. The content of each dopant metal relative to the total weight of the second catalyst is between 0 and 2% by weight, preferably of 0.01 and 1% by weight, preferably between 0.01 and 0.7% by weight relative to the total weight of the second catalyst.

[0062] The second catalyst may also include at least one halogen used to acidify the alumina support. The halogen content may be between 0.1 and 15% by weight relative to the total weight of the second catalyst, preferably between 0.2 and 5% by weight relative to the total weight of the second catalyst. Preferably, a single halogen is used, in particular chlorine or fluorine. When the second catalyst includes a single halogen, which is chlorine or fluorine, the chlorine content is between 0.5 and 2% by weight relative to the total weight of the second catalyst.

[0063] The second catalyst may also comprise an alkali metal in proportions of approximately 0.1 to 3% by weight relative to the total weight of the second catalyst. Preferably, the alkali metal is potassium.

[0064] According to one or more embodiments, the second catalyst comprises an active phase comprising platinum and tin, a promoter comprising tin, and a y-type alumina-based support.

[0065] According to one or more embodiments, a dedicated hydrotreating step (e.g. desulfurization) of the second hydrocarbon feed 1 and / or the raffinate 16 is carried out before the catalytic reforming steps.

[0066] In the example of [Fig. 2], the first reformat separation column 11 and the second reformat separation column 33 are different columns, the former being dedicated to the separation of the first liquid fraction 10 and the latter to the separation of the second liquid fraction 32, respectively. With reference to [Fig. 3], according to one or more embodiments, the first liquid fraction 10 and the second liquid fraction 32 are sent to the first reformat separation column 11. In this or these embodiments, the second reformat separation column 33 is not present / used. It follows that the first C8+ fraction 13 comprises the second C8+ fraction 23, the first head fraction 25 comprises the second head fraction 35, and the first C6-C8 hydrocarbon compound feed 24 comprises the first C6-C8 fraction 12.

[0067] In the example of [Fig. 3], the first stabilization section 7 and the second stabilization section 29 are distinct sections, the former being dedicated to stabilizing the first liquid hydrocarbon effluent 6 and the latter to stabilizing the second liquid hydrocarbon effluent 28, respectively. With reference to [Fig. 4], according to one or more embodiments, the first liquid hydrocarbon effluent 6 and the second liquid hydrocarbon effluent 28 are sent to the first stabilization section 7. In this or these embodiments, the second stabilization section 29 is not present / used. It follows that the first gaseous hydrocarbon compound effluent 8 comprises the second gaseous effluent of hydrocarbon compounds 30, the first liquid stream 9 includes the second liquid stream 31, and the first liquid fraction 10 includes the second liquid fraction 32.

[0068] In the example of [Fig. 4], the first recontacting section 4 and the second recontacting section 26 are different sections, the first being dedicated to the recontacting of the first reformat effluent 18 and the second being dedicated to the recontacting of the second reformat effluent 3, respectively. With reference to [Fig. 5], according to one or more embodiments, the first reformat effluent 18 and the second reformat effluent 3 are sent to the first recontacting section 4. In this or these embodiments, the second recontacting section 26 is not present / used. It follows that the first hydrogen-rich gaseous effluent 5 includes the second hydrogen-rich gaseous effluent 27 and the first hydrocarbon liquid effluent 6 includes the second hydrocarbon liquid effluent 28.

[0069] According to one or more embodiments, the recontacting and stabilization steps (sections 4, 7, 26 and 29) of the process include the following substeps: i) the reformat stream (for example the first reformat effluent 18) is separated into a gaseous phase and a liquid phase containing hydrocarbons; ii) the liquid phase from step i) is cooled to a temperature less than or equal to 45°C, preferably less than 25°C, very preferably less than 15°C, by means of a cooling device; iii) a first re-contacting of the cooled liquid phase with the gaseous phase is carried out in a separation means in order to recover a hydrogen-rich gaseous effluent (for example the first hydrogen-rich gaseous effluent 5) and a liquid hydrocarbon effluent (for example the first liquid hydrocarbon effluent 6); iv) a second recontacting of the liquid hydrocarbon effluent is carried out with a recycle gas and a gaseous effluent rich in hydrocarbon compounds is separated (for example the first gaseous effluent of hydrocarbon compounds 8) and a second liquid hydrocarbon effluent; (v) the second liquid hydrocarbon effluent from step (iv) is fractionated in a fractionation column so as to separate a gaseous fraction and a liquid fraction (for example the first liquid fraction 10); vi) the gaseous fraction from step v) is condensed and a liquid stream (for example the first liquid stream 9) is separated from the recycled gas, which is recycled in step iv). The details of these recontacting and stabilization steps are detailed in patent FR3074175B1.

[0070] According to one or more embodiments, the separating means is a column recontacting system operating in counter-current or a separation tank.

[0071] Advantageously, steps i) to vi) utilize the cooling capacity contained in the gaseous or liquid effluents generated during the recontacting step carried out in a recontacting (or absorption) column to pre-cool the liquid hydrocarbon phase before it undergoes further cooling to reach the desired temperature for the recontacting step. Thermal integration thus significantly reduces the cooling capacity and therefore the overall energy consumption of the process.

[0072] According to one or more embodiments, before step ii) of cooling, the liquid phase from step i) is pre-cooled by heat exchange in a heat exchanger supplied with the hydrogen-rich gaseous effluent and the hydrocarbon liquid effluent from step iii).

[0073] According to one or more embodiments, before the cooling step ii), the liquid phase from step i) undergoes heat exchange in a heat exchanger supplied with the hydrogen-rich gaseous effluent, and the gaseous phase from step i) undergoes heat exchange in a heat exchanger supplied with the liquid hydrocarbon effluent.

[0074] According to one or more embodiments, before the cooling step ii), the liquid phase from step i) undergoes heat exchange in a heat exchanger supplied with the liquid hydrocarbon effluent, and the gaseous phase from step i) undergoes heat exchange in a heat exchanger supplied with the hydrogen-rich gaseous effluent.

[0075] According to one or more embodiments, part or all of the gaseous effluent rich in hydrocarbon compounds is recycled before the first recontacting step.

[0076] According to one or more embodiments, the gaseous effluent rich in hydrocarbon compounds is recycled in a mixture with the gaseous phase from step i). Examples

[0077] Example 1: Classic reforming.

[0078] Example 1 is not in accordance with the invention and corresponds to a classic reforming scheme without valorization of raffinate 16 from the extraction of aromatics.

[0079] Compared to [Fig.2], example 1 does not include the following units: - first dedicated hydrotreatment unit 21; - first dedicated catalytic reforming unit 17; - first recontacting section 4; - first stabilization section 7; - first reformat separation column 11.

[0080] The total input flow rate is 187.2 t / h. 126 t / h are converted into aromatics. 54.2% 13.1 wt% of the second hydrocarbon feedstock 1 is converted to paraxylene and 13.1 wt% to benzene after processing extract 15 and the second C8+ fraction 23 in an aromatic complex for the production of paraxylene and benzene. The inlet and outlet flow rates of the process in Example 1 are listed in Table 1 below.

[0081] [Tables 1] Catalytic reforming (non-compliant) t / h Second hydrocarbon feed 1,187.2 Second hydrogen-rich gaseous effluent 27,10.9 Second hydrocarbon compound gaseous effluent 30,19.5 Second liquid stream 31,4.4 Second head fraction 35,4.8 Refinate 16 (not recycled) 15.8 Extract 15,57.5 Second C8+ fraction 23,74.3 Aromatic complex (downstream process known to those skilled in the art) t / h Benzene 24.6 Paraxylene 101.4 Heavy 5.8

[0082] Example 2: Separation of the feed at the reforming inlet.

[0083] Example 2 is not in accordance with the invention and corresponds to a reforming scheme with separation of the second hydrocarbon feed 1 for the parallel reforming of a light fraction on the one hand and a heavy fraction on the other hand (see [Fig.1] of FR3074175B1).

[0084] Compared to [Fig.2], example 2 does not include the following units: - first dedicated hydrotreatment unit 21; - first dedicated catalytic reforming unit 17; - first recontacting section 4; - first stabilization section 7; - first reformat separation column 11.

[0085] Compared to [Fig.2], the second hydrotreating unit 19 and the second catalytic reforming unit 2 of Example 2 are each divided into two units to treat the light fraction on the one hand and the heavy fraction on the other.

[0086] The total input flow rate is 187.2 t / h. 140.6 t / h are converted into aromatics. 56.4% by weight of the second hydrocarbon feedstock 1 is converted to paraxylene and 18.7% by weight to benzene after processing of extract 15 and the second C8+ fraction 23 in an aromatic complex for the production of paraxylene and benzene. The inlet and outlet flow rates of the process in Example 2 are listed in Table 2 below.

[0087] [Tables2] Catalytic reforming (non-compliant) t / h Second hydrocarbon feed 1,187.2 Second hydrogen-rich gaseous effluent 27,13.4 Second hydrocarbon compound gaseous effluent 30,19.4 Second liquid stream 31,26 Second head fraction 35,4.6 Refinate 16,0 Extract 15,70.4 Second C8+ fraction 23,76.8 Aromatic complex (downstream process known to those skilled in the art) t / h Benzene 35.1 Paraxylene 105.5 Heavy 6.6

[0088] Example 3: Dedicated reforming of the refinery.

[0089] Example 3 conforms to the invention and corresponds to a scheme described in the [Fig.2],

[0090] The 15.8 t / h of raffinate 16 not recovered in Example 1 are sent to the first catalytic reforming unit 17. This increases the production of benzene and paraxylene from 126 t / h to 137.8 t / h, representing an increase of approximately 10% in the total recovered aromatics. The recovered aromatics yield increases from 67.3 wt% to 73.6 wt%. 57.8 wt% of the second hydrocarbon feedstock 1 is converted into paraxylene and 15.9 wt% into benzene.

[0091] Compared to Example 2, slightly less benzene and paraxylene are produced (137.8 t / h vs. 140.6 t / h). However, more paraxylene is advantageously produced (108 t / h vs. 105.5 t / h), which is more valuable than benzene. The selectivity for paraxylene compared to benzene is better in Example 3 compared to Example 2 (78.4 wt. vs. 75.0 wt. paraxylene). The inlet and outlet flow rates of the The methods of Example 3 are listed in the following Table 3.

[0092] [Tables3] Catalytic Reforming (Invention) t / h Second hydrocarbon feed 1 187.2 First hydrogen-rich gaseous effluent 5 0.9 First hydrocarbon compound gaseous effluent 8 1.6 First liquid stream 9 0.3 First head fraction 25 0.4 Second hydrogen-rich gaseous effluent 27 10.9 Second hydrocarbon compound gaseous effluent 30 19.5 Second liquid stream 31 4.4 Second head fraction 35 4.8 Refinate 16 (recycled to first dedicated hydrotreating unit 21) 15.8 Extract 15 68.3 First C8+ fraction 13 5.9 Second C8+ fraction 23 70.2 Aromatic complex (downstream process known to those skilled in the art) t / h Benzene 29.8 Paraxylene 108.0 Heavy 6.6

Claims

Demands

1. A process for producing aromatic compounds from a feed of hydrocarbon compounds, comprising the following steps: - a first feed of C6-C8 hydrocarbon compounds (24) is sent to an aromatics extraction unit (14) to produce an extract (15) comprising aromatic compounds of 6 to 8 carbon atoms and a raffinate (16) comprising aliphatic compounds of 6 to 8 carbon atoms; - the raffinate (16) is sent to a first dedicated catalytic reforming unit (17) to produce a first reformate effluent (18); - the first reformate effluent (18) is sent to a first recontacting section (4) to separate a first hydrogen-rich gaseous effluent (5) and a first liquid hydrocarbon effluent (6);- The first liquid hydrocarbon effluent (6) is sent to a first stabilization section (7) to separate a first gaseous hydrocarbon compound effluent (8) comprising C1-C2 hydrocarbon compounds, a first liquid stream (9) comprising C3-C4 or C3-C5 hydrocarbon compounds, and a first liquid fraction (10) comprising hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms; - The first liquid fraction (10) is sent to a first reformat separation column (11) to separate a first C6-C8 fraction (12) comprising C6-C8 hydrocarbon compounds, and a first C8+ fraction (13) comprising hydrocarbon compounds with at least 8 carbon atoms; - The first C6-C8 fraction (12) is sent, at least in part, to the aromatics extraction unit (14).

2. A method according to claim 1, comprising sending the extract (15) and the first C8+ fraction (13) to an aromatics production unit.

3. A process according to claim 1 or claim 2, wherein the raffinate (16) is sent to a first dedicated hydrotreating unit (21) to produce a first hydrotreated effluent (22) sent to the first catalytic reforming unit (17).

4. A process according to any one of the preceding claims, wherein the first C6-C8 fraction (12) comprises C5 hydrocarbon compounds, and / or a first head fraction (25) comprising C5 hydrocarbon compounds is separated in the first reformat separation column (11).

5. A process according to any one of the preceding claims, wherein the first C6-C8 hydrocarbon compound (24) charge comprises at least 50% by weight, preferably at least 60% by weight, most preferably at least 70% by weight of aromatic compounds.

6. A method according to any one of the preceding claims, wherein the first catalytic reforming unit (17) comprises at least one reforming reactor operated under at least one of the following operating conditions: - a temperature between 400°C and 600°C, preferably between 470°C and 570°C; - a pressure between 0.1 MPa and 3 MPa, preferably between 0.3 MPa and 2.5 MPa; - a molar ratio of hydrogen to hydrocarbon compounds between 0.8 and 8 mole / mole; and - a mass flow rate of treated flux per unit mass of catalyst per hour between 0.1 h₁ and 10 h₁, preferably between 0.5 h₁ and 6 h₁.- optional catalyst comprising: an active phase comprising: at least one metal selected from platinum, zinc or molybdenum, preferably platinum; a support comprising a zeolite, preferably a zeolite selected from zeolite L, zeolite X, zeolite Y, zeolite ZSM-5; and optionally a binder selected from aluminosilicate, alumina, silica, clays, silicon carbides, taken alone or in combination.

7. A process according to any one of the preceding claims, comprising the following steps: - sending a second hydrocarbon feedstock (1) to a second catalytic reforming unit (2) to produce a second reformat effluent (3); - sending the second reformat effluent (3) to a second recontacting section (26) to produce a second hydrogen-rich gaseous effluent (27) and a second liquid hydrocarbon effluent (28); - sending the second liquid hydrocarbon effluent (28) to a

8.

9.

10. second stabilization section (29) for separating a second gaseous effluent of hydrocarbon compounds (30) comprising C1-C2 hydrocarbon compounds, a second liquid stream (31) comprising C3-C4 or C3-C5 hydrocarbon compounds, and a second liquid fraction (32) comprising hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms; - the second liquid fraction (32) is sent to a second reformat separation column (33) to separate a second C6-C8 fraction (34) and a second C8+ fraction (23) comprising hydrocarbon compounds with at least 8 carbon atoms; - the second C6-C8 fraction (34) is sent at least in part to the aromatics extraction unit (14) as said first C6-C8 hydrocarbon compound load (24). A method according to claim 7, comprising sending the second C8+ (23) fraction, at least partially, into an aromatic complex. A method according to any one of claims 1 to 6, comprising the following steps: - a second hydrocarbon feed (1) is sent into a second catalytic reforming unit (2) to produce a second reformat effluent (3); - the second reformat effluent (3) is sent into a second recontacting section (26) to produce a second hydrogen-rich gaseous effluent (27) and a second liquid hydrocarbon effluent (28); - the second liquid hydrocarbon effluent (28) is sent to a second stabilization section (29) to separate a second gaseous hydrocarbon compound effluent (30) comprising C1-C2 hydrocarbon compounds, a second liquid stream (31) comprising C3-C4 or C3-C5 hydrocarbon compounds, and a second liquid fraction (32) comprising hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms; - the second liquid fraction (32) is sent into the first reformat separation column (11). A method according to any one of claims 1 to 6, comprising the following steps: - a second hydrocarbon feed (1) is sent into a second catalytic reforming unit (2) to produce a second reformat effluent (3); - the second reformat effluent (3) is sent into a second recontacting section (26) to produce a second hydrogen-rich gaseous effluent (27) and a second liquid hydrocarbon effluent (28); - the second liquid hydrocarbon effluent (28) is sent into the first stabilization section (7).

11. A process according to any one of claims 1 to 6, comprising the following steps: - sending a second hydrocarbon feed (1) into a second catalytic reforming unit (2) to produce a second reformat effluent (3); - sending the second reformat effluent (3) into the first recontacting section (4).

12. A process according to any one of claims 7 to 11, wherein the second hydrocarbon feed (1) is sent to a second dedicated hydrotreating unit (19) to produce a second hydrotreated effluent (20) sent to the second catalytic reforming unit (2).

13. A method according to any one of claims 7 to 12, wherein the second hydrocarbon feedstock (1) comprises naphtha.

14. A method for modifying a device for producing aromatic compounds from a feedstock of hydrocarbon compounds, the device for producing aromatic compounds comprising: - a second catalytic reforming unit (2) adapted to process a second hydrocarbon feedstock (1) and produce a second reformat effluent (3); - a second recontacting section (26) adapted to process the second reformat effluent (3) and produce a second hydrogen-rich gaseous effluent (27) and a second liquid hydrocarbon effluent (28); - a second stabilization section (29) adapted to process the second liquid hydrocarbon effluent (28) and separate a second gaseous hydrocarbon effluent (30) comprising C1-C2 hydrocarbon compounds, a second liquid stream (31) comprising C3-C4 or C3-C5 hydrocarbon compounds, and a second liquid fraction (32) comprising hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms; - a second reformat separation column (33) adapted to treat the second liquid fraction (32) and separate a second C6-C8 fraction (34) and a second C8+ fraction (23) comprising hydrocarbon compounds with at least 8 carbon atoms; - an aromatics extraction unit (14) adapted to process the second C6-C8 fraction (34) and produce an extract (15) comprising aromatic compounds of 6 to 8 carbon atoms and a raffinate (16) comprising aliphatic compounds of 6 to 8 carbon atoms, the process comprising the following steps: - a first dedicated catalytic reforming unit (17) is installed in the aromatic compound production device, adapted to treat the raffinate (16), produce a first reformate effluent (18), and send the first reformate effluent (18) to the second recontacting section (26) or a first dedicated recontacting section (4); - optionally, a first dedicated recontacting section (4) is installed in the aromatic compound production device, adapted to treat the first reformat effluent (18), separate a first hydrogen-rich gaseous effluent (5) and a first liquid hydrocarbon effluent (6), and send the first liquid hydrocarbon effluent (6) to the second stabilization section (29) or a first dedicated stabilization section (7); - optionally, a first dedicated stabilization section (7) is installed in the aromatic compound production device, adapted to treat the first liquid hydrocarbon effluent (6), separate a first gaseous hydrocarbon compound effluent (8) comprising C1-C2 hydrocarbon compounds, a first liquid stream (9) comprising C3-C4 or C3-C5 hydrocarbon compounds, and a first liquid fraction (10) comprising hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms, and send the first liquid fraction (10) to the second reformat separation column (33) or a dedicated first reformat separation column (11); - Optionally, a first reformat separation column is installed in the aromatic compound production device

15. dedicated (11) adapted to treat the first liquid fraction (10), separate a first C6-C8 fraction (12) comprising C6-C8 hydrocarbon compounds, and a first C8+ fraction (13) comprising hydrocarbon compounds with at least 8 carbon atoms, and send the first C6-C8 fraction (12) at least in part to the aromatics extraction unit (14). Device for the production of aromatic compounds from a feed of hydrocarbon compounds, comprising the following elements: - an aromatic extraction unit (14) adapted to process a first feed of C6-C8 hydrocarbon compounds (24) to produce an extract (15) comprising aromatic compounds of 6 to 8 carbon atoms and a raffinate (16) comprising aliphatic compounds of 6 to 8 carbon atoms; - a first dedicated catalytic reforming unit (17) adapted to treat the raffinate (16) and produce a first reformate effluent (18); - a first recontacting section (4) adapted to treat the first reformat effluent (18) and separate a first hydrogen-rich gaseous effluent (5) and a first liquid hydrocarbon effluent (6); - a first stabilization section (7) adapted to treat the first liquid hydrocarbon effluent (6) and separate a first gaseous effluent of hydrocarbon compounds (8) comprising C1-C2 hydrocarbon compounds, a first liquid stream (9) comprising C3-C4 or C3-C5 hydrocarbon compounds, and a first liquid fraction (10) comprising hydrocarbon compounds having at least 4 or 5 carbon atoms and preferably at least 5 carbon atoms; - a first reformat separation column (11) adapted to treat the first liquid fraction (10), separate a first C6-C8 fraction (12) comprising C6-C8 hydrocarbon compounds and a first C8+ fraction (13) comprising hydrocarbon compounds with at least 8 carbon atoms, and send the first C6-C8 fraction (12) at least in part to the aromatics extraction unit (14).

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