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    • 专利摘要:
    The present invention describes a process for producing paraxylene from a xylenes-containing cup and ethylbenzene using two simulated moving bed adsorption units and two isomerization units.
    公开号:FR3023841A1
    申请号:FR1456941
    申请日:2014-07-18
    公开日:2016-01-22
    发明作者:Heloise Dreux；Philibert Leflaive；Le Cocq Damien Leinekugel
    申请人:IFP Energies Nouvelles IFPEN；
    IPC主号:
    专利说明:

    [0001] FIELD OF THE INVENTION The production of paraxylene has been steadily increasing for thirty years. The main uses of paraxylene are the production of terephthalic acid and polyethylene terephthalate resins, to provide synthetic textiles, bottles, and more generally plastics. To meet the ever-increasing demand for paraxylene, petrochemists have the choice between increasing capacity on existing units or building new units. The present invention makes it possible to respond to these two situations. In particular, it makes it possible to cope with capacity increases of existing units (called debottlenecking) because the modifications involved are relatively modest. In the remainder of the text we speak of a simulated moving bed separation unit (abbreviated as SMB), or a separation unit (SMB). A separation unit (SMB) may contain one or more adsorbers. EXAMINATION OF THE PRIOR ART The production of high purity paraxylene by adsorptive separation is well known in the prior art. In an industrial manner, this operation is performed by a sequence of processes known as "C8-aromatic loop". This "C8-aromatic loop" includes a step of removing heavy compounds (i.e., C9 +) in a distillation column called "xylenes column". The top stream of this column, which contains the C8-aromatic isomers, is then sent to the paraxylene separation process which is very generally a simulated moving bed adsorption separation process. The extract, which contains paraxylene, is then distilled in an extract column and then a so-called "toluene" column to obtain high purity paraxylene.
    [0002] The raffinate, rich in metaxylene, orthoxylene and ethylbenzene, after a step of removing the solvent by distillation is treated in a catalytic isomerization unit which gives a mixture of C8 aromatics, in which the proportion of xylenes (ortho-, meta-, para-xylenes) is practically at thermodynamic equilibrium, and the amount of ethylbenzene diminished. This mixture is again sent to the "xylenes column" with the fresh load. All industrial processes for the isomerization of C8-aromatics make it possible to isomerize xylenes. The conversion of ethylbenzene, on the other hand, depends on the type of process and catalyst chosen. Indeed, the petrochemical complexes will use an isomerization unit called "isomerizing" (ie isomerizing ethylbenzene to a mixture of aromatic C8) or "dealkylating" (dealkylation of ethylbenzene to benzene), in order to favor production respectively or para-xylene alone, ie benzene and para-xylene.
    [0003] The choice of the catalyst used depends on the transformation of the desired ethylbenzene. When the target reaction is the isomerization of ethylbenzene, it requires a bifunctional catalyst having both an acid function and a hydrogenating function. It has been shown that ethylbenzene is first hydrogenated to ethylcyclohexene at the metal sites, then converted to dimethylcyclohexene on acidic sites by contraction then cycle expansion, and finally dehydrogenated to xylenes. When the target reaction is the dealkylation of ethylbenzene, it occurs only on acidic sites. The presence of a hydrogenating phase on the catalyst, however, makes it possible to immediately hydrogenate the ethylene formed and to obtain total dealkylation, thus avoiding any subsequent re-alkylation. In both cases, the incorporation of a metal phase in the catalyst also ensures its stability. The industrial isomerization processes therefore use heterogeneous bifunctional catalysts (acid and metal) used in a fixed bed and operating in the vapor phase under hydrogen pressure, in temperature ranges generally ranging between 380440 ° C. and 10 to 20 bar.
    [0004] The choice of "isomerizing" isomerization makes it possible, as indicated above, to maximize the production of paraxylene, which is the compound with the highest added value at the outlet of the aromatic complex. However, this solution has the disadvantage of generating in the isomerization step losses in aromatic rings by cracking higher than with a dealkylating isomerization, the cycle being transiently at least partially hydrogenated. The choice of the type of isomerization is therefore a compromise between the minimization of the loss of aromatic rings associated with a co-production of benzene, a product with lower added value than paraxylene (dealkylating isomerization), and a maximization of the production of paraxylene which it has the disadvantage of generating losses in aromatic cycles greater (isomerization "isomerization"). There is therefore a need for a process that allows both a maximization of the amount of paraxylene produced with reduced aromatic ring loss. Several solutions are proposed in the prior art in order to achieve this objective, these generally involving isomerization (generally preferably dealkylating), associated with steps of conversion of benzene by transalkylation and / or methylation of toluene or benzene, as described for example in the document US2013 / 0267746. It has surprisingly been found that the combination within an aromatic complex of "isomerizing" isomerization and liquid phase isomerization as described, for example, in patents US2011 / 263918, US7,371,913, US4 , 962,258 and US6180550 allowed to maximize the amount of paraxylene produced while having a reduced aromatic ring loss compared to an aromatic complex according to the prior art. In the remainder of the text we speak of a separation unit for the simulated moving bed separation units, of adsorbers for designating sets of adsorbent beds, a unit 30 which can contain one or more adsorbers.
    [0005] We are talking about isomerization unit and distillation columns to designate the other equipment of the process. SUMMARY DESCRIPTION OF THE FIGURES FIG. 1 is a diagram of the process according to the invention in which the two simulated moving bed separation units, noted (SMB-1) and (SMB-2), have been shown, and the two units of FIG. isomerization (ISOM-1) and (ISOM-2).
    [0006] FIG. 2 represents a variant of the process according to the invention in which the separation unit (SMB-1) uses PDEB as desorbent and the separation unit (SMB-2) uses toluene as an adsorbent. As a result, toluene is recovered at the top of distillation columns (EXT-2) and (RAF-2) because toluene is lighter than aromatic C8s.
    [0007] FIG. 3 represents a diagram according to the prior art and serves to illustrate example 1 which is according to the prior art. SUMMARY DESCRIPTION OF THE INVENTION The present invention can be defined as a process for producing high purity paraxylene from a xylenes cut containing ethylbenzene and C9 + compounds. The method according to the present invention uses two simulated moving bed separation units (SMB-1 and SMB-2), and two isomerization units (ISOM-1 and ISOM-2). Said method 25 consists of following steps: - the charge (2) is sent to a distillation column (S-1), from which a mixture (3) comprising most of the metaxylene is withdrawn at the top, paraxylene, ethylbenzene, and at least a portion of the orthoxylene, and in bottom a stream (4) of C9-C10 hydrocarbons, and the remaining part of the orthoxylene, - a first separation is carried out head mixture (3) in the separation unit (SMB1) comprising at least one adsorber containing a plurality of interconnected beds and working in a closed loop, said unit comprising at least four zones delimited by the injections of the stream (3) and of the desorbent (10) resulting from the mixing of the streams (9) and (7), and the withdrawals of a first extract (5) enriched in paraxylene, and a first raffinate (8) depleted in paraxylene, second separation in the separation unit (SMB-2) of the isomerate (12) from one isomerization unit (ISOM-1), said separation unit (SMB-2) consisting of at least one adsorber containing a plurality of interconnected beds and preferably working in a closed loop, and said unit comprising at least four zones delimited by injections of the charge (12) and desorbent (18) resulting from the streams (17) and (15), and the withdrawals of a second extract (13) enriched in paraxylene, and a second raffinate (16) depleted in paraxylene, the first extract (5) from the separation unit (SMB-1) is distilled in a distillation column (EXT-1) to recover a flux (6) enriched in paraxylene, and a flow ( 7) which is used as desorbent of the separation unit (SMB-1), - the second extract (13) from the separation unit (SMB-2) is distilled in a distillation column (EXT-2). ), to recover a flux (14) enriched in paraxylene, and a stream (15) which is used as desorbent of the separation unit (SMB-2), the raffinate (16) from the separation unit (SMB-2) is distilled in a distillation column (RAF-2), so as to produce a flow (19) which feeds the isomerization unit (ISOM-2), and a stream (17) which is used as desorbent of the separation unit (SMB-2), the raffinate (8) from the separation unit is distilled off (SMB-1) in a distillation column (RAF-1) which produces the stream (11) which feeds the isomerization unit (ISOM-1), and a stream (9) which is used as the desorbent of the separating unit (SMB-1), the isomerization unit (ISOM-1) is fed with the stream (11) to obtain the first isomer (12), and the second (19) feed is fed with the stream (19). isomerization unit (ISOM-2) to obtain a second isomerate (20) which is recycled to the inlet of the distillation column (S-1), said isomerization unit (ISOM-2) operating in the gas phase and under conditions following: - temperature above 300 ° C, preferably from 350 ° C to 480 ° C, 5 - pressure less than 4.0 MPa, and preferably 0.5 to 2.0 MPa, - space velocity less than 10 h -1, preferably 0.5 h-1 and 6 h-1, molar ratio of hydrogen to hydrocarbon of less than 10, and preferably of between 3 and 6, and the catalyst used in said isomerization unit (ISOM-2) comprising at least one zeolite having channels whose opening is defined by a ring with 10 or 12 oxygen atoms (denoted 10 MR or 12 MR), and at least one metal of group VIII with a content of between 0.1 and 0.3% by weight, terminals included. Preferably, in the process for producing high purity paraxylene according to the invention, the isomerization unit (ISOM1) operates in the liquid phase under the following conditions: - Temperature below 300 ° C., preferably between 200 ° C. and 260 ° C., a pressure of less than 4 MPa, preferably of between 2 and 3 MPa, a space velocity of less than 10 h -1, preferably of between 2 h -1 and 4 h -1; minus a zeolite having channels whose opening is defined by a ring with 10 or 12 oxygen atoms (denoted 10 MR or 12 MR), preferentially a zeolite having channels whose opening is defined by a ring with 10 atoms of oxygen (denoted 10 MR), and even more preferably a zeolite of the ZSM-5 type. Preferably, in the process for producing high purity paraxylene according to the invention, the catalyst used for the isomerization unit in the gas phase (ISOM-2) contains a zeolite of structure type EUO or MOR, and preferably preferred is an EU-1 zeolite and platinum.
    [0008] According to a variant of the process for producing high purity paraxylene according to the invention, the separation unit (SMB-1) uses the PDEB as desorbent. According to another variant of the process for producing high purity paraxylene according to the invention, the separation unit (SMB-2) uses toluene as desorbent. According to a variant of the process for producing high purity paraxylene according to the invention, the separation units (SMB-1) and (SMB-2) each contain from 6 to 24 beds, and preferably from 8 to 15 beds distributed on one or more adsorbers, the number of beds being adjusted so that each bed preferably has a height of between 0.70 m and 1.40 m. Preferably, in the process for producing high purity paraxylene according to the invention, the distribution of the amount of adsorbent solid in the separation units (SMB-1) and (SMB-2) is as follows: of solid adsorbent in zone 1 is 17% ± 5%, the amount of solid adsorbent in zone 2 is 42% ± 5%, the amount of solid adsorbent in zone 3 is 25% ± 5%, the amount of solid adsorbent in zone 4 is 17% ± 5%, the zones being defined as follows: Zone 1 being between the injection of the desorbent and the withdrawal of the extract, the zone 2 being between withdrawal of the extract and the injection of the charge, the zone 3 being between the injection of the feedstock and the withdrawal of the raffinate, the zone 4 being between the withdrawal of the raffinate and the injection of the desorbent. According to another preferred variant of the process for the production of high purity paraxylene according to the invention, with regard to the separation unit (SMB-1), the desorbent volumetric ratio on charge is at most 1.7 / 1, and preferably between 1.5 / 1 and 0.4 / 1, inclusive. According to another variant of the method for producing high purity paraxylene according to the invention, with regard to the separation unit (SMB-2), the desorbent volumetric charge ratio is at most 1.7 / 1. and preferably between 1.5 / 1 and 0.4 / 1 inclusive. One of the advantages of the process for the production of high purity paraxylene according to the invention is that it makes it possible to dewater an existing unit consisting of two adsorbers used in series, as follows: the last bed of the first adsorber is connected to the first bed of the first adsorber via a line containing at least one recirculation pump, this first adsorber serving as separation unit (SMB-1) 10 - the last bed of the second adsorber is connected to the first bed of the second adsorber via a line containing at least one recirculation pump, this second adsorber serving as separation unit (SMB-2). In one variant of the process for producing high purity paraxylene according to the invention, the configuration of the two separation units (SMB-1) and (SMB-2) has a fixed number of beds in each of the chromatographic zones of each of the two separation units (SMB1) and (SMB-2). Finally, in another variant of the process for producing high purity paraxylene according to the invention, a fraction of the isomerate (12) is sent to the distillation column (S-1). DETAILED DESCRIPTION OF THE INVENTION The present description is based on FIG. 1. The feedstock (2) is sent to a distillation column (S-1) from which a mixture (3) comprising the most of the metaxylene, paraxylene, ethylbenzene, and at least a portion of the orthoxylene, and from which a stream (4) of C9-C10 hydrocarbons is withdrawn in the bottom and the remaining portion of orthoxylene. A first separation of the overhead mixture (3) in the separation unit (SMB1) is carried out in at least one adsorber containing a plurality of interconnected beds and working in a closed loop, said adsorber comprising at least four zones delimited by the injections of the flow (3) constituting the first charge of the column and desorbent (10), and withdrawals of an extract (5) containing paraxylene and a raffinate (8) containing orthoxylene and metaxylene.
    [0009] The four zones correspond to the following definitions: 1) the zone 1 is between the injection of the desorbent (10) and the withdrawal of the extract (5), 2) the zone 2 is between the withdrawal of the extract ( 5) and the injection of the first adsorption charge (3), 3) the zone 3 is between the injection of the first charge (3) and the withdrawal of the raffinate (8) and 4) the zone 4 is between the raffinate withdrawal (8) and the injection of the desorbent (10). 5) A first extract (5) is preferably distilled in a distillation column (EXT-1) to recover a first fraction (6) enriched in paraxylene. A first raffinate (8) is preferably distilled in a distillation column (RAF-1) to substantially remove all the desorbent and to withdraw a first distilled fraction (11). This first distilled fraction (11) feeds a first isomerization unit (ISOM-1) to obtain a first isomer (12) preferentially supplying the xylenes separation unit (SMB-2) but which can be partially recycled to the input of the distillation column (S-1).
    [0010] A second separation is carried out in the separation unit (SMB-2) of the isomerate (12) from the isomerization unit (ISOM-1), from which all or part of the C9 heavy compounds have been optionally removed. and C10 by distillation (either in a dedicated column or in column S-1), the separation unit (SMB-2) consisting of at least one adsorber containing a plurality of interconnected beds, and preferably working in a loop closed, said column comprising at least four zones defined by the injections of the flow (12) and the desorbent (18), and the withdrawals of a second extract (13) containing paraxylene and a second raffinate (16). The four zones are defined as follows: 1) the zone 1 is between the injection of the desorbent (18) and the withdrawal of the extract (13), 2) the zone 2 is between the withdrawal of the extract (13) and the injection of the second adsorption charge (12), 3) the zone 3 is between the injection of the charge (12) and the withdrawal of the raffinate (16), and 4) the zone 4 is between the raffinate withdrawal (16) and the injection of the desorbent (18). The second extract (13) is preferably distilled in a distillation column (EXT15 2) to recover a second fraction (14) enriched in paraxylene. The two extracts (5) and (13) can also be distilled in a single column of common extract to recover a single fraction enriched in paraxylene. A second raffinate (16) is preferably distilled in a distillation column (RAF-2). to substantially remove all the desorbent (17) and to withdraw a second distilled fraction (19). This second distilled fraction (19) feeds a second isomerization unit (ISOM-2) to obtain a second isomerate (20) recycled at the inlet of the distillation column (S-1). The first isomerization unit (ISOM-1) preferably operating in the liquid phase is generally operated under the following conditions: - Temperature below 300 ° C, preferably 200 ° C to 260 ° C - Pressure less than 4 MPa, preferably 2 to 3 MPa - hourly space velocity (VVH) less than 10h-1 (10 liters per liter per hour), preferably between 2 and 4 h-1. Catalyst comprising at least one zeolite having channels whose opening is defined by a ring with 10 or 12 oxygen atoms (10 MR or 12 MR), preferably a catalyst comprising at least one zeolite having channels whose opening is defined by a ring with 10 oxygen atoms (10 MR), and even more preferably a catalyst comprising a zeolite type ZSM-5.
    [0011] The second isomerization unit (ISOM-2) is characterized in that the catalyst comprises at least one zeolite having channels whose opening is defined by a ring with 10 or 12 oxygen atoms (10 MR or 12 MR) , preferably a catalyst comprising a zeolite of structural type EUO or MOR, and at least one Group VIII metal with a content of between 0.1 and 0.3% inclusive, preferably an EU-1 zeolite and platinum. This isomerization zone working in gaseous phase is generally operated under the following conditions: - Temperature above 300 ° C, preferably 350 ° C to 480 ° C - Pressure less than 4 MPa, preferably 0.5 to 2 MPa - Hourly space velocity (VVH) less than 10 h -1 (10 liters per liter per hour), preferably between 0.5 and 6 h -1. - H2 / hydrocarbon molar ratio of less than 10, preferably between 3 and 6.
    [0012] The desorbents used in the separation units (SMB-1 and SMB-2) are generally chosen from paradiethylbenzene, toluene, paradifluorobenzene or mixed diethylbenzenes. The volume ratio of the desorbent on the charge in the separation units (SMB-1 and SMB-2) is between 0.5 and 2.5, and preferably between 0.8 and 2.
    [0013] The separation units (SMB-1 and SMB-2) are operated at a temperature between 20 ° C and 250 ° C, preferably between 90 ° C and 210 ° C, and more preferably between 140 ° C and 180 ° C ° C, and under a pressure between the bubble pressure of xylenes at the operating temperature and 2 MPa.
    [0014] The operation of the process according to the invention, and in particular the composition of the different flows, is specified below with reference to FIG.
    [0015] The fresh feed is introduced via line (1) into a distillation column (S-1). This fresh feed contains mainly C8-aromatic compounds, xylenes and ethylbenzene, in variable proportion depending on the origin of the cut. It may optionally contain impurities in a variable amount depending on the origin of the feed which will essentially be aromatic compounds C9 and C10 and paraffinic and naphthenic compounds. The content of naphthenic or paraffinic impurities is advantageously less than 1% by weight. Preferably, this content is less than 0.3% by weight and more preferably this content is less than 0.1% by weight. The feed may be from either a reforming unit, a toluene disproportionation unit, a transalkylation unit of toluene and aromatic C9. To the fresh feed is added an isomerate conveyed by a line (20). The bottom effluent (4) of the (S-1) column consists essentially of aromatic C 9 and C 10 compounds and optionally orthoxylene. Optionally, the mixture (4) of orthoxylene and aromatic hydrocarbons C9-C10 withdrawn at the bottom of the distillation column (S1), can be sent to another distillation column from which is extracted at the top a flow of orthoxylene of high purity (at least 98.5%), and in bottom a stream containing C9-C10 hydrocarbons. The overhead effluent (3) from the distillation column (S-1) constitutes the charge of the separation unit (SMB-1). The separation unit (SMB-1) is fed on the one hand by the load conveyed by the line (3), and on the other hand by desorbent conveyed by a line (10). The effluents from the separation unit (SMB-1) are an extract (5) and a raffinate (8). The total number of beds of the separation unit (SMB-1) according to the invention is preferably between 6 and 24 beds, and even more preferably between 8 and 15 beds distributed over one or more adsorbers.
    [0016] The number of beds will be adjusted so that each bed preferably has a height between 0.70 m and 1.40 m. The distribution of the amount of adsorbent solid in each zone is as follows: the amount of adsorbent solid in zone 1 is 17% ± 5%, the amount of adsorbent solid in zone 2 is 42% ± 5%, the quantity of adsorbent solid in zone 1 is solid adsorbent in zone 3 is 25% ± 5%, the amount of solid adsorbent in zone 4 is 17% ± 5%. According to a preferred characteristic of the invention, the desorbent and the charge can be injected into the unit. separation device in a desorbent charge-to-charge ratio of at most 1.7 / 1, and preferably in the range of 1.5 / 1 to 0.4 / 1, inclusive. The extract (5) consists essentially of toluene, paraxylene and desorbent.
    [0017] The raffinate (8) consists essentially of toluene, metaxylene, orthoxylene, ethylbenzene, paraxylene for the unrecovered portion in the extract, and desorbent. The extract (5) is sent to a distillation column (EXT-1).
    [0018] The desorbent (7) returned to the separation unit (SMB-1) is withdrawn from the column (EXT-1) via the line (10), and a paraxylene enriched stream via the line (6). The raffinate (8) is sent to a distillation column (RAF-1). The desorbent (9), which is returned to the separation unit (SMB-1), is withdrawn from the distillation column (RAFF-1) via line (10), and a mixture of metaxylene, orthoxylene, and ethylbenzene via a line (11), which is sent to the isomerization unit (ISOM-1). The isomerization unit (ISOM-1), preferably in the liquid phase, can work under the following conditions: - temperature below 300 ° C., preferably between 200 and 260 ° C., - pressure below 4 MPa, preferably between 2 and 3 MPa, - space velocity of less than 10 h -1, preferably of between 2 h -1 and 4 h -1.
    [0019] Any of the catalysts capable of isomerizing hydrocarbons with 8 carbon atoms are suitable for the isomerization unit (ISOM-1) of the present invention. Preferably, a catalyst containing a ZSM-5 zeolite will be used.
    [0020] The isomerization unit effluent (ISOM-1) is returned via line (12) either to the distillation column (S-1) or directly to the inlet of the separation unit (SMB -2) in the case where the content of compounds other than C8-aromatics is very low, typically of the order of 1% by weight. The C9 content is typically less than 1000 ppm wt.
    [0021] The effluents from the separation unit (SMB-2) are an extract (13) and a raffinate (16). The total number of beds of the separation unit (SMB-2) according to the invention is preferably between 6 and 24 beds, and even more preferably between 8 and 15 beds distributed over one or more adsorbers.
    [0022] The number of beds will be adjusted so that each bed preferably has a height between 0.70 m and 1.40 m. The distribution of the amount of adsorbent solid in each zone is preferentially the following: the amount of adsorbent solid in zone 1 is 17% ± 5%, the quantity of adsorbent solid in zone 2 is 42% ± 5%, the quantity of solid adsorbent in zone 3 is 25% ± 5%, the amount of solid adsorbent in zone 4 is 17% ± 5%. According to a preferred characteristic of the invention, the desorbent and the filler can be injected into the separation unit (SMB-2) in a desorption charge volumetric ratio of at most 1.7 / 1, and preferably between 1.5 / 1 and 0.4 / 1, inclusive.
    [0023] The configuration (average number of beds per zone) of the two separation units (SMB-1 and SMB-2) can be: - with fixed beds in each of the chromatographic zones ("simulated moving bed" mode as defined in patent FR 2 976 501), with a variable number of beds for an adsorber ("VARICOL" mode as defined in patent FR 2 976 501), and fixed for the other, with a variable number of beds for both adsorbers. The extract (13) consists essentially of toluene, paraxylene and desorbent. The raffinate (16) consists essentially of toluene, metaxylene and orthoxylene, ethylbenzene, paraxylene for the unrecovered portion in the extract, and desorbent. The extract (13) is sent to a distillation column (EXT-2). The desorbent (15) which is returned to the separation unit (SMB-2) through the line (18) is withdrawn from the distillation column (EXT-2), and a paraxylene-enriched stream is withdrawn through the line (14). . The raffinate is sent via line (16) to the distillation column (RAF-2). The desorbent (17) which is reintroduced via the line (18) into the separation unit (SMB-2) and a mixture of xylenes and ethylbenzene are withdrawn from the distillation column (RAF-2) by line (19). The effluents from the line (19) are sent to the isomerization unit (ISOM-2) operating at high temperature in the vapor phase. The isomerization unit (ISOM-2) is operated preferably under the following conditions: - temperature above 300 ° C, preferably from 360 ° C to 480 ° C, - pressure below 2.5 MPa and from preferably between 0.5 and 0.8 MPa, - space velocity of less than 10 h -1, preferably of between 0.5 h -1 and 6 h -1, - molar ratio of hydrogen to hydrocarbon of less than 10, and preferably ranging from 3 to 6. All catalysts capable of isomerizing hydrocarbons with 8 carbon atoms, whether zeolitic or not, are suitable for the isomerization unit (ISOM-2) of the present invention. Preferably, a catalyst containing an acidic zeolite, for example of structural type MFI, MOR, MAZ, FAU and / or EUO, is used. Even more preferably, a catalyst containing a zeolite of structure type EUO and at least one metal of group VIII of the periodic table of elements is used.
    [0024] Preferably, the catalyst of the isomerization unit (ISOM-2) contains from 1 to 70% by weight of a zeolite of structural type EUO (EU-1 for example) comprising silicon and at least one selected element T preferably, aluminum and boron, the Si / T ratio of which is between 5 and 100. Said zeolite is in hydrogen form, at least in part, and the sodium content is such that the atomic ratio Na / T is less than at 0.1. Optionally, the catalyst of the isomerization unit may contain between 0.01 and 2% by weight of tin or indium, and sulfur with 0.5 to 2 atoms per atom of Group VIII metal. The isomerization unit effluent (ISOM-2) is sent to a separator train that allows the recovery of part of the hydrogen that is recycled to the isomerization unit (ISOM-2). The part of non-recycled hydrogen is compensated by a supplement of fresh hydrogen. At the end of the separation train, an isomer is recovered consisting of the heavier fractions which is returned to the distillation column (S-1) via the line (20).
    [0025] The process according to the invention is particularly well suited to modifying an existing unit in order to increase the quantity of paraxylene produced, an operation called debottlenecking. In the particular case of debottlenecking of an existing aromatic loop, the invention consists in significantly increasing the fresh feed rate and the flow of paraxylene produced while continuing to use the main equipment of the loop, namely: ) the xylenes distillation column (S-1) 2) the simulated moving bed xylenes separation unit operating in 24 beds 3) the isomerization unit (ISOM-2) fed by the raffinate withdrawn from the column separation unit for converting ethylbenzene, said unit using for example an EUO structural type zeolite catalyst comprising a reactor, a recycle compressor, a stabilization column, and a column for recovering the C8 and C9 naphthenes from 4) the raffinate column (RAF-1) 5) the extract column (EXT-1) To carry out this debottlenecking according to the invention, converting a process into a bed mob 24-bed simulated island containing two 12-bed adsorbers in series, in a two-adsorber twelve-bed process, each connected in parallel. To do this: - the twelfth bed of the first adsorber is connected to the first bed of said first adsorber via a line containing at least one recirculation pump, - the twelfth bed of the second adsorber is connected to the first bed of said second adsorber via a line containing at least less a recirculation pump. The system for controlling and regulating the feed and desorbent feed rates and the extraction rates of the extract and the raffinate of the 24-bed adsorption stage is adapted so as to be able to independently manage the flow rates. injection and withdrawal in each of the two adsorbers of the remodeled method according to the invention. For the injection devices, this operation can be carried out either by doubling the system 20 pump + measuring member to regulate the flow injected into each of the adsorbers, or, in order to minimize costs, using the pump and the pump. pre-existing measuring unit that will manage all of the two flows to be injected, and adding a flow measurement and regulation system feeding one of the two adsorbers. When the supply or draw-off of the fluids on all the trays of the existing 24-bed process is ensured by a plurality of on-off valves, there are no additional modifications to be made to the supply networks. and racking. When the supply or withdrawal of fluids on all the trays of the existing process in 24 beds is ensured by the use of a multi-way rotary valve, these functions will preferably be ensured by the use of two multi-way rotary valves 15 (possibly recycling the pre-existing valve to one of the two tracks after adaptation).
    [0026] In the case of an existing 24-bed unit consisting of twice twelve beds in series, the main stream flows from the bottom of the first adsorber to the head of the second adsorber, and from the bottom of the second adsorber to the head of the first adsorber.
    [0027] The flows from the bottoms of the two adsorbers are then redirected to flow to the head of the adsorber from which they are derived by performing the valve and pipe modifications. The bottom flow of the first adsorber is recycled to the head of said adsorber and the bottom flow of the second adsorber is recycled to the head of said second adsorber.
    [0028] The configuration (average number of beds per zone) of the two adsorbers can be carried out according to one of the 3 variants explained above, ie: with a fixed number of beds in each of the chromatographic zones for the two adsorbers, - Variable number of beds for one adsorber and fixed for the other - Variable number of beds for both adsorbers. In order to separate the second raffinate from the desorbent, a new distillation column (RAF-2) will also have to be put in place. The flow of xylenes and ethylbenzene withdrawn from the distillation column (RAF-2) will be isomerized in the vapor isomerization unit (ISOM-1) as described above. A second liquid phase isomerization unit (ISOM-2) is added, the effluent of which will feed the separation unit (SMB-2) preferentially without passing through the distillation column (S-1) to avoid the addition a second xylenes separation column. On the other hand, it is necessary to add an extract distillation column (EXT-2) supplied with the extract (13) of the separation unit (SMB-2). FIG. 2 shows a variant of the process scheme according to the invention which differs from that of FIG. 1 in that the separation unit (SMB-1) uses PDEB as desorbent and toluene as desorbent of the separation unit (SMB-2).
    [0029] In contrast to the separation unit (SMB-1) at the PDEB, the separation unit (SMB-2) recovers the desorbent (toluene) at the top of column EXT-2 and RAF-2, because toluene is lighter than C8-aromatics.
    [0030] The fact of using two different desorbents in the two separation units (SMB-1 and SMB-2) has the advantage of avoiding the accumulation of aromatic impurities such as benzene and C9 and C10 heavy aromatics.
    [0031] Using two different desorbents in the two separation units (SMB-1 and SMB-2) also allows thermal integration between columns (EXT-1) and (EXT-2) and (RAF-1) and (RAF-1). 2). Indeed the column head (EXT-1) can potentially reboil all or part of the column (EXT-2) and the head of the column (RAF-1) can potentially reboil all or part of the column (RAF-2) .
    [0032] EXAMPLES ACCORDING TO THE INVENTION Example 1 According to the Prior Art (FIG. 3): This example illustrates the prior art and describes an aromatic complex consisting of two C8-aromatic loops in parallel, typical of industrial complexes in which the quantity of paraxylene produced is greater than the acceptable capacity by a single C8-aromatic loop, as schematized in FIG. 3 and comprising: two xylenes column (S-10 and S-20) making it possible to extract the aromatics at C9 and C10 (stream 104 and 113) and to send to the separation units (SMB-10 and SMB-20) a stream (103) and a stream (112) consisting essentially of C8 aromatics, - a first simulated moving bed separation unit (SMB-10) to 4 zones from which an extract (105) and a single raffinate (107) are withdrawn, - a first isomerization unit (ISOM-10) fed by a portion (108) of the raffinate (107) after removing the desorbent (109) by means of the distillation column (RAF- 10), a first column of paraxylene extract (EXT-10) from which the desorbent which is recycled to the separation unit (SMB-1) via the stream (109) and at the head of a cup paraxylene-rich (106); - a second 4-zone simulated moving bed separation unit (SMB-20) from which an extract (114) and a single raffinate (116) are withdrawn; a second isomerization unit; (ISOM-20) fed with a portion (117) of the raffinate (116) after removal of the desorbent (118) by means of the distillation column (RAF-20), - a second column of paraxylene extract (EXT-20) ) from which the desorbent which is recycled to the adsorption (SMB-2) is drawn downwards through the flow (118) and at the top a paraxylene-rich cut (115). The material balance of the process is described in the table below. Only C8-aromatic and C9 + compounds are described. The other compounds and the formation of C9 + in the isomerization units are neglected. As a unit of flow, 1,000 tonnes per year (kt / year) are used. 15 PX EB MOX C9 + Total Fresh Charge 101 23.6 15.6 67.7 13.8 120.6 Charge S-10 102 50.0 22.9 148.5 6.9 228.3 Charge SMB-10 103 50 , 0 22.9 148.5 0 221.4 Bottom S-10 104 0 0 0 6.9 6.9 Head EXT-10 106 50, 0 0 0 0 50.0 Input ISOM-10 108 0 22.9 148 171.4 Output ISOM-10 110 38, 2 15.1 114.7 0 168.0 Charge S-20 111 50.0 22.9 148.5 6.9 228.3 Charge SMB-20 112 50 , 0 22.9 148.5 0 221.4 Fund 5-20 113 0 0 0 6.9 6.9 Head EXT-20 115 50.0 0 0 0 50.0 Input ISOM-20 117 0 22.9 148 , 171.4 Output ISOM-20 119 38.2 15.1 114.7 0 168.0 TABLE 1 The feed (101) which feeds the aromatic loop (mixture of heavy reformate and toluene column bottom) has a flow rate of 120.6 kt / year. This load is divided into two equal streams of 60.3 kt / year. A first part of the charge (101) is added 168 kt / year of isomerate (110) recycled from the isomerization unit (ISOM-10) in order to isomerize the ethylbenzene. The resulting stream (102) is distilled in the xylenes column (S-10). 6.9 kt / year of a mixture of aromatic C9 and C10 (104) and 221.4 kt / year of an aromatic C8 cut (103) were withdrawn from the bottom of the column (S-10). paraxylene content is 22.6%, the ethylbenzene content is 10.3%, the content of orthoxylene and metaxylene is 67.1%. This section is sent to a four-zone simulated moving bed separation unit (SMB-10) and four main streams: the feed (103), the desorbent (109), the extract (105) and the raffinate (107). ). This unit is composed of 12 beds containing a zeolite X exchanged with barium. The temperature is 175 ° C. The configuration is: 2 beds in zone 1, 5 beds in zone 2, 20 3 beds in zone 3 and 2 beds in zone 4. The solvent used is paradiethylbenzene. The extract (105) at the outlet of the separation unit (SMB-10) is sent to a distillation column (EXT-10) from which the recycled desorbent is drawn down to the separation unit (SMB-10). ) and at the top 50 kt / year of a mixture (106) consisting essentially of toluene and paraxylene. The raffinate is sent to a distillation column (RAF-10) from which the recycled desorbent is drawn down to the separation unit (SMB-10) and at the top 171.4 kt / year of a mixture (108). ). This stream is sent to an isomerization unit (ISOM-10). The isomerization unit (ISOM-10) works in the gas phase under the following conditions: Temperature: 385 ° C. Catalyst: contains 0.2% wt platinum and zeolite EU-1 Spatial velocity: 3.5 hr 1 H 2 / hydrocarbons ratio: 4.4: 1 Pressure: 0.9 MPa The ethylbenzene content of the mixture introduced into the isomerization unit (ISOM-10) is 13.4%.
    [0033] 2% loss by cracking is observed in this isomerization, ie a flow rate of 3.4 kt / year. Ethylbenzene is partially isomerized, with 9% remaining in the exit stream (110). This isomerate (110) has a flow rate of 168 kt / year. It is recycled to the inlet of the S-10 column where it is mixed with a portion of the fresh feed (101) which has a flow rate of 60.3 kt / year. A first part of the charge (101) is added 168 kt / year of isomerate (119) recycled from the isomerization unit (ISOM-20) in order to isomerize the ethylbenzene. The resulting stream (111) is distilled in the xylene column (S-20). 6.9 kt / year of a mixture of aromatic C9 and C10 (stream 113) and 221.4 kt / year of aromatic C8 cut (stream 112) are withdrawn at the bottom of the distillation column (S-20). whose paraxylene content is 22.6%, and the ethylbenzene content of 10.4%. This section is sent to a four-zone simulated moving bed adsorption unit (SMB-20) and four main streams: the feed (stream 112), the desorbent (stream 118), the extract (stream 114) and the raffinate (stream 116). This unit is composed of 12 beds containing a zeolite X exchanged with barium. The temperature is 175 ° C. The configuration is: 2 beds in zone 1, 5 beds in zone 2, 3 beds in zone 3 and 2 beds in zone 4. The solvent used is paradiethylbenzene.
    [0034] The extract (114) at the outlet of the separation unit (SMB-20) is sent to a distillation column (EXT-20) from which the recycled desorbent is drawn down to the adsorption unit (SMB-20). 20), and at the top 50 kt / year of a mixture (115) consisting essentially of toluene and paraxylene. The raffinate is sent to a distillation column (RAF-20) from which the recycled desorbent is drawn down to the separation unit (SMB-20) and at the top 171.4 kt / year of a mixture (117). ). This stream is sent to an isomerization unit (ISOM-20). The obtained isomerate (119) is recycled to the inlet of the distillation column (S-20) where it is mixed with a portion of the fresh feed (101). The isomerization unit (ISOM-20) works in the gas phase under the following conditions: Temperature: 385 ° C Catalyst: contains 0.2% wt platinum and zeolite EU-1 Spatial velocity: 3.5 hr 1 H 2 / hydrocarbons ratio: 4.4 / 1. Pressure: 0.9 MPa. The ethylbenzene content of the mixture introduced into the isomerization unit (ISOM-20) is 13.4%. 2% loss by cracking is observed in this isomerization, ie a flow rate of 3.4 kt / year. Ethylbenzene is partially isomerized, with 9% remaining in the exit stream (119). This isomerate (119) has a flow rate of 168 kt / yr, it is recycled to the inlet of the S-20 column where it is mixed with a part of the fresh feed (101) which has a flow rate of 60.3 kt / yr . EXAMPLE 2 According to the Invention This example illustrates the invention and describes an aromatic loop schematized in FIG. 1 and comprising: a column of xylenes (S-1) making it possible to extract the aromatics at C9 and C10 (4) and sending to the adsorption unit (SMB-1) a stream (3) consisting essentially of C8 aromatics. a first 4-zone simulated mobile bed separation unit (SMB-1) from which an extract (5) and a raffinate (8) are withdrawn. a first column of paraxylene extract (EXT-1) from which the desorbent (7) is withdrawn at the bottom and is recycled to the separation unit (SMB-1) via the stream (10) and at the top a cup rich in paraxylene (6). a second 4-zone simulated mobile bed separation unit (SMB-2) from which an extract (13) and a raffinate (16) are withdrawn. a second column of paraxylene extract (EXT-2) from which the desorbent (15) is withdrawn at the bottom and is recycled to the separation unit (SMB-2) via the stream (18) and at the top a cup rich in paraxylene (14). a first isomerization unit (ISOM-1) fed by the first raffinate (11) after removal of the desorbent (9) by means of the distillation column (RAF-1). a second isomerization unit (ISOM-2) fed by the second raffinate (19) after removal of the desorbent (17) by means of the distillation column (RAF-2). The material balance of the process is described in Table 2 below. Only the compounds C8- and C9 + are described, the other compounds and the formation of C9 + are neglected in the isomerization units. As a unit of flow, 1,000 tonnes per year (kt / year) are used. 30 PX EB MOX C9 Total Fresh load 1 22.7 15.3 65.1 13.3 116.4 Load S-1 2 57.6 29.1 169.7 13.3 269.7 Load SMB-1 3 57 , 6 29.1 169.7 0 256.4 Bottom S-1 4 0 0 0 13.3 13.3 Head EXT-1 6 57.6 0 0 0 57.6 Load ISOM-11 0 29.1 169, 7 0 198.8 1 ISOM-1 output 12 42.4 29.1 127.3 0 198.8 Head EXT-2 14 42.4 0 0 0 42.4 ISOM-2 input 19 0 29.1 127.3 0 156.4 ISOM-2 output 20 34.9 13.8 104.6 0 153.3 TABLE 2 The fresh feed (1) which feeds the aromatic loop has a flow rate of 116.4 kt / year. To this feedstock is added 153.3 kt / year of isomerate (20) recycled from the isomerization unit (ISOM2) isomerizing ethylbenzene. The resulting stream (2) is distilled in the xylenes column (S1). The bottom of the distillation column (S-1) is withdrawn 13.3 kt / year of a mixture of aromatic C9 and C10 (4), and at the top 256.4 kt / year of aromatic C8 cut (3). whose content of paraxylene is 22.5%, the ethylbenzene content of 11.3%, the content of orthoxylene and metaxylene of 66.2%. This aromatic C8 cut is fed into a four-zone simulated moving bed separation unit (SMB-1) and four main streams: the feed (3), the desorbent (10), the extract (5) and the feedstock (5). raffinate (8). This unit is composed of 12 beds containing a zeolite X exchanged with barium. The temperature is 175 ° C. The configuration is: 2 beds in zone 1, 5 beds in zone 2, 3 beds in zone 3 and 2 beds in zone 4. The solvent used is paradiethylbenzene. The extract (5) at the outlet of the separation unit (SMB-1) is sent to a distillation column (EXT-1) from which the desorbent (7) recycled to the separating unit ( SMB-1), and at the top 57.6 kt / year of a mixture (6) consisting essentially of toluene and paraxylene. The raffinate (8) is sent to a distillation column (RAF-1) from which the recycled desorbent (9) is drawn down to the adsorption unit (SMB-1) and at the top 198.8 kt / year of a mixture (11). This stream (11) is sent to an isomerization unit (ISOM-1). The isomerization unit (ISOM-1) works in the liquid phase under the following conditions: Temperature: 240 ° C Catalyst: contains ZSM-5 zeolite Spatial velocity: 3 h-1 Pressure: 1.9 MPa Ethylbenzene content the mixture introduced into the isomerization unit (ISOM-1) is about 14.6%. Ethylbenzene is not converted, so its quantity is the same in the output stream (12). The isomerate (12) has a flow rate of 198.8 kt / year. It is recycled to the inlet of the adsorption unit (SMB-2) without passing through the column (S-1). The isomerate (12) from the isomerization unit (ISOM-1) feeds a second four-zone simulated moving bed separation unit (SMB-2) and four main streams: the feed (12), the desorbent (18), the extract (13) and the raffinate (16). This unit is composed of 12 beds containing a zeolite X exchanged with barium. The temperature is 175 ° C. The configuration is: 2 beds in zone 1, 5 beds in zone 2, 3 beds in zone 3 and 2 beds in zone 4. The solvent used is paradiethylbenzene. The extract (13) at the outlet of the separation unit (SMB-2) is sent to a distillation column (EXT-2) from which the recycled desorbent (15) is drawn down to the distillation unit. separation (SMB-2), and at the top 42.4 kt / year of a mixture (14) consisting essentially of toluene and paraxylene. The raffinate (16) is sent to a distillation column (RAF-2) from which the recycled desorbent (17) is drawn down to the separation unit (SMB-2), and at the top 156.4 kt / year of a mixture (19). This stream (19) is sent to an isomerization unit (ISOM-2). The isomerization unit (ISOM-2) works in the gas phase under the following conditions: Temperature: 385 ° C Catalyst: contains 0.2% wt platinum and zeolite EU-1 Spatial velocity: 3.5 hr 1 Pressure: 0.9 MPa The ethylbenzene content of the mixture introduced into the isomerization unit (ISOM-2) is about 18.6%. 2% loss by cracking is observed in this isomerization unit, ie a flow rate of 3.1 kt / year. Ethylbenzene is partially isomerized, with 9% remaining in the exit stream (20). The isomerate (20) has a flow rate of 153.3 kt / year, it is recycled to the inlet of the S-1 column where it is mixed with the fresh feed (1) which has a flow rate of 116.4 kt / year. . The invention has several advantages over the prior art. First, the isomerization unit in the liquid phase is less energy consuming than isomerization in the gas phase. Indeed, it works at a lower temperature. It also works without recycle hydrogen and therefore without recycle compressor.
    [0035] Finally, the isomerization unit in the liquid phase produces much less by-products, especially C9 aromatics, which makes it possible to pass the aromatic elimination column at C9 (S-1), inducing a very strong lower energy needed for this separation. Coupling isomerization in the liquid phase to isomerization in the gas phase isomerizing ethylbenzene makes it possible to reduce the losses by cracking. In order to output 100 kt / year of paraxylene, it is necessary to introduce 103.1 kt / year of C8 aromatic compounds (calculated as the difference 116.4 - 13.3 kt / year) in the fresh feedstock in the process according to the invention, against 106.8 kt / year of C8 aromatic compounds (calculated as the difference 120.6 -13.8 kt / year) for the process according to the prior art.
    权利要求:
    Claims (12)
    [0001]
    1) Process for producing high purity paraxylene, from a xylenes cut containing ethylbenzene and C9 + compounds, method using two simulated moving bed separation units (SMB-1 and SMB-2), and two isomerization units (ISOM-1 and ISOM-2) consisting of the following series of steps: - the charge (2) is sent to a distillation column (S-1), from which at the top a mixture (3) comprising most of the metaxylene, paraxylene, ethylbenzene, and at least a portion of the orthoxylene, and bottom a C9-C10 hydrocarbon stream (4), and the remaining portion a first separation of the head mixture (3) from the orthoxylene is carried out in the separation unit (SMB1) comprising at least one adsorber containing a plurality of interconnected and closed-loop beds, said unit comprising at least four zones delimited by the injections of the flow (3) and the die sorbent (10) resulting from the mixing of the streams (9) and (7), and the withdrawals of a first extract (5) enriched in paraxylene, and a first raffinate (8) depleted in paraxylene, it carries out a second separation in the separation unit (SMB-2) of the isomerate (12) from the isomerization unit (ISOM-1), said separation unit (SMB-2) consisting of at least one adsorber containing a plurality of interconnected beds and preferably working in a closed loop, and said unit comprising at least four zones defined by the injections of the charge (12) and the desorbent (18) resulting from the flows (17) and 25 (15), and the withdrawals of a second extract (13) enriched in paraxylene, and a second raffinate (16) depleted in paraxylene, - the first extract (5) from the separation unit (SMB-1) is distilled in a distillation column (EXT-1), for recovering a flux (6) enriched in paraxylene, and a stream (7) which is used as a d separator unit (SMB-1), the second extract (13) from the separation unit (SMB-2) is distilled in a distillation column (EXT-2) to recover a flow ( 14) enriched in paraxylene, and a stream (15) which is used as desorbent of the separation unit (SMB-2), the raffinate (16) from the separation unit (SMB-2) is distilled off. in a distillation column (RAF-2), so as to produce a stream (19) which feeds the isomerization unit (ISOM-2), and a stream (17) which is used as a desorbent of the unit of separation (SMB-2), the raffinate (8) from the separation unit (SMB-1) is distilled in a distillation column (RAF-1) which produces the flow (11) which feeds the unit d isomerization (ISOM-1), and a stream (9) which is used as desorbent of the separation unit (SMB-1), - the isomerization unit (ISOM-1) is fed with the stream (11). ) to obtain the first isomerate (12), the flow (19) is fed through the the second isomerization unit (ISOM-2) to obtain a second isomerate (20) which is recycled at the inlet of the distillation column (S-1), said isomerization unit (ISOM-2) operating in the gas phase and at the following conditions: - temperature above 300 ° C, preferably from 350 ° C to 480 ° C, - pressure below 4.0 MPa, and preferably from 0.5 to 2.0 MPa, - space velocity less than 10 h -1, preferably between 0.5 h -1 and 6 h -1, molar ratio of hydrogen to hydrocarbon of less than 10, and preferably of between 3 and 6, and the catalyst used in said unit. isomerization (ISOM-2) comprising at least one zeolite having channels whose opening is defined by a ring with 10 or 12 oxygen atoms (denoted 10 MR or 12 MR), and at least one metal of the group VIII of content between 0.1 and 0.3% by weight, inclusive. 25
    [0002]
    2) A process for producing high purity paraxylene from a xylenes containing ethylbenzene and C9 + compounds according to claim 1, wherein the isomerization unit (ISOM1) operates in liquid phase at the following conditions : - Temperature below 300 ° C, preferably between 200 and 260 ° C, 30 - Pressure less than 4 MPa, preferably between 2 and 3 MPa, - Space velocity of less than 10 h -1, preferably between 2 h -1 and 4 h -1, Catalyst comprising at least one zeolite having channels whose opening is defined by a ring with 10 or 12 oxygen atoms (denoted 10 MR or 12 MR), preferentially a zeolite having channels whose opening is defined by a ring with 10 oxygen atoms (denoted 10 MR), and even more preferably a zeolite of ZSM-5 type.
    [0003]
    3) A process for producing high purity paraxylene from a xylenes containing ethylbenzene and C9 + compounds according to claim 1, wherein the catalyst used for the gas phase isomerization unit (ISOM- 2) contains an EUO or MOR structural zeolite, and preferably an EU-1 zeolite and platinum.
    [0004]
    4) A method for producing high purity paraxylene from a xylenes containing ethylbenzene and C9 + compounds according to claim 1, wherein the separation unit (SMB-1) uses as desorbent PDEB. 15
    [0005]
    5) A method for producing high purity paraxylene from a xylenes containing ethylbenzene and C9 + compounds according to claim 1, wherein the separation unit (SMB-2) uses toluene as desorbent. 20
    [0006]
    A process for producing high purity paraxylene from a xylenes cut containing ethylbenzene and C9 + compounds according to claim 1, wherein the separation units (SMB-1) and (SMB-2) contain each of 6 to 24 beds, and preferably 8 to 15 beds distributed over one or more adsorbers, the number of beds being adjusted so that each bed preferably has a height of between 0.70 m and 1, 40 m. 25
    [0007]
    7) A process for producing high purity paraxylene from a xylenes containing ethylbenzene and C9 + compounds according to claim 1, wherein the distribution of the amount of adsorbent solid in the separation units (SMB- 1) and (SMB-2) is as follows: the amount of adsorbent solid in zone 1 is 17% ± 5%, the amount of adsorbent solid in zone 2 is 42% ± 5%, the amount of adsorbent solid in zone 3 is 25% ± 5%, the amount of adsorbent solid in zone 4 is 17% ± 5%, the zones being defined as follows: zone 1 being between the injection of the desorbent and withdrawal of the extract, zone 2 being between withdrawal of the extract and injection of the charge, zone 3 being between the injection of the feedstock and the withdrawal of the raffinate; zone 4 being between the withdrawal of the raffinate and the injection of the desorbent.
    [0008]
    8) A process for producing high purity paraxylene from a xylenes cut containing ethylbenzene and C9 + compounds according to claim 1, wherein for the separation unit (SMB-1), the volumetric ratio desorbent on charge is at most 1.7 / 1, and preferably between 1.5 / 1 and 0.4 / 1, inclusive.
    [0009]
    9) A process for producing high purity paraxylene from a xylenes containing ethylbenzene and C9 + compounds according to claim 1, wherein for the separation unit (SMB-2), the volumetric ratio desorbent on charge is at most 1.7 / 1, and preferably between 1.5 / 1 and 0.4 / 1 inclusive.
    [0010]
    10) A process for the production of high purity paraxylene from a xylenes containing ethylbenzene and C9 + compounds according to claim 1, obtained from the debottlenecking of an existing unit consisting of two adsorbers used in series, as follows: - the last bed of the first adsorber is connected to the first bed of the first adsorber via a line containing at least one recirculation pump, this first adsorber acting as separation unit (SMB-1) - the last bed of the second adsorber is connected to the first bed of the second adsorber via a line containing at least one recirculation pump, this second adsorber serving as separation unit (SMB-2). 30
    [0011]
    11) A process for producing high purity paraxylene from a xylenes containing ethylbenzene and C9 + compounds according to claim 1, wherein the configuration of the two separation units (SMB-1) and (SMB- 2) has a fixed number of beds in each of the chromatographic zones of each of the two separation units (SMB1) and (SMB-2).
    [0012]
    12) A process for producing high purity paraxylene from a xylenes cut containing ethylbenzene and C9 + compounds according to claim 1, wherein a fraction of the isomerate (12) is fed to the column of distillation (S-1).
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    同族专利:
    公开号 | 公开日
    EP3169654A1|2017-05-24|
    KR20170036717A|2017-04-03|
    PT3169654T|2018-11-16|
    CN106715372A|2017-05-24|
    CN106715372B|2020-03-03|
    EP3169654B1|2018-08-29|
    US20170210683A1|2017-07-27|
    US10029958B2|2018-07-24|
    KR102343701B1|2021-12-24|
    WO2016008653A1|2016-01-21|
    FR3023841B1|2016-07-15|
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    优先权:
    申请号 | 申请日 | 专利标题
    FR1456941A|FR3023841B1|2014-07-18|2014-07-18|PROCESS FOR PRODUCING PARAXYLENE COMPRISING TWO SIMUL MOBILE BED SEPARATION UNITS AND TWO ISOMERIZING UNITS, ONE OF WHICH IS GAS PHASE|FR1456941A| FR3023841B1|2014-07-18|2014-07-18|PROCESS FOR PRODUCING PARAXYLENE COMPRISING TWO SIMUL MOBILE BED SEPARATION UNITS AND TWO ISOMERIZING UNITS, ONE OF WHICH IS GAS PHASE|
    PT15727016T| PT3169654T|2014-07-18|2015-06-10|Method for the production of paraxylene, comprising two simulated moving bed separation units and two isomerisation units, one being in the gas phase|
    US15/326,887| US10029958B2|2014-07-18|2015-06-10|Method for the production of paraxylene, comprising two simulated moving bed separation and two isomerization units, one being in the gas phase|
    EP15727016.6A| EP3169654B1|2014-07-18|2015-06-10|Method for the production of paraxylene, comprising two simulated moving bed separation units and two isomerisation units, one being in the gas phase|
    CN201580050222.7A| CN106715372B|2014-07-18|2015-06-10|Process for the production of para-xylene comprising two simulated moving bed separation units and two isomerization units, one of which is a gas phase unit|
    PCT/EP2015/062984| WO2016008653A1|2014-07-18|2015-06-10|Method for the production of paraxylene, comprising two simulated moving bed separation units and two isomerisation units, one being in the gas phase|
    KR1020177004406A| KR102343701B1|2014-07-18|2015-06-10|Method for the production of paraxylene, comprising two simulated moving bed separation units and two isomerisation units, one being in the gas phase|
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