Method for the production of paraxylene, comprising two simulated moving bed separation and two isomerization units, one being in the gas phase

Patent metadata

Field	Value
Publication number	US-10029958-B2
Application number	US-201515326887-A
Country	US
Kind code	B2
Filing date	Jun 10, 2015
Priority date	Jul 18, 2014
Publication date	Jul 24, 2018
Grant date	Jul 24, 2018

Abstract

The present invention describes a process for the production of high-purity paraxylene from a xylenes cut containing xylenes and ethylbenzene, a process using two simulated moving bed separation units and two isomerization units.

First claim

The invention claimed is:

1. A process for producing high-purity paraxylene based on a xylenes cut containing ethylbenzene and C9+ compounds, a which process is performed in an apparatus that contains two simulated moving bed separation units (SMB-1 and SMB-2), and two isomerization units (ISOM-1 and ISOM-2), wherein ISOM-1 operates in liquid phase and ISOM-2 operates in gas phase, said process consisting of the following series of stages:
sending a feedstock (2) comprising metaxylene, paraxylene, orthoxylene, ethylbenzene, and C9+ compounds to a distillation column (S-1) from where a mixture (3) is drawn off at a top comprising a major part of the metaxylene, paraxylene, and ethylbenzene, and at least a part of the orthoxylene, and a flow (4) of C9-C10 hydrocarbons and the remaining part of the orthoxylene is drawn off at a bottom,
carrying out a first separation of the mixture from the top (3) in the separation unit (SMB-1) comprising at least one adsorber containing a plurality of interconnected beds and operating in a closed loop, said unit comprising at least four zones delimited by injections of the mixture (3) and a first desorbent (10), resulting from a mixture of flows (9) and (7), and draw-offs of a first extract (5) enriched with paraxylene and a first raffinate (8) depleted of paraxylene,
carrying out a second separation of a first isomerate (12) originating from the isomerization unit (ISOM-1) in the separation unit (SMB-2), said separation unit (SMB-2) being constituted by at least one adsorber containing a plurality of interconnected beds and operating optionally in a closed loop, and said unit comprising at least four zones delimited by injections of the first isomerate (12) and of a second desorbent (18), resulting from a mixture of flows (17) and (15), and draw-offs of a second extract (13) enriched with paraxylene and a second raffinate (16) depleted of paraxylene,
distilling the first extract (5) originating from the separation unit (SMB-1) in a distillation column (EXT-1) to recover a flow (6) enriched with paraxylene, and a flow (7) which is sent as desorbent (10) to the separation unit (SMB-1),
distilling the second extract (13) originating from the separation unit (SMB-2) in a distillation column (EXT-2) to recover a flow (14) enriched with paraxylene, and a flow (15) which is sent as desorbent (18) to the separation unit (SMB-2),
distilling the raffinate (16) originating from the separation unit (SMB-2) in a distillation column (RAF-2) to produce a flow (19) which is supplied to the isomerization unit (ISOM-2), and a flow (17) which is sent as desorbent (18) to the separation unit (SMB-2)
distilling the raffinate (8) originating from the separation unit (SMB-1) in a distillation column (RAF-1) to produce a flow (11) which is supplied to the isomerization unit (ISOM-1), and a flow (9) which is sent as desorbent (10) to the separation unit (SMB-1)
supplying the isomerization unit (ISOM-1) with flow (11) to obtain the first isomerate (12),
supplying the second isomerization unit (ISOM-2) with flow (19) 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 gas phase and under the following conditions:
a temperature greater than 300° C.,
a pressure less than 4.0 MPa,
an hourly space velocity less than 10 h −1 ,
a hydrogen to hydrocarbon molar ratio less than 10, and
in the presence of a catalyst in said isomerization unit (ISOM-2) comprising at least one zeolite having channels the opening of which is defined by a ring with 10 to 12 oxygen atoms (denoted 10 MR or 12 MR), and at least one group VIII metal at a content between 0.1 and 0.3% by weight, inclusive.

2. The process for the production of high-purity paraxylene based on a xylenes cut containing ethylbenzene and C9+ compounds according to claim 1 , in which the isomerization unit (ISOM-1) operates in liquid phase under the following conditions:
a temperature less than 300° C.,
a pressure less than 4 MPa,
an hourly space velocity less than 10 h −1 ,
in the presence of a catalyst comprising at least one zeolite having channels the opening of which is defined by a ring with 10 or 12 oxygen atoms (denoted 10 MR or 12 MR).

3. The process for the production of high-purity paraxylene based on a xylenes cut containing ethylbenzene and C9+ compounds according to claim 1 , in which the catalyst for the gas-phase isomerization unit (ISOM-2) contains a zeolite of EUO or MOR structure type and platinum.

4. The process for the production of high-purity paraxylene based on a xylenes cut containing ethylbenzene and C9+ compounds according to claim 1 , in which the separation unit (SMB-1) contains PDEB as desorbent.

5. The process for the production of high-purity paraxylene based on a xylenes cut containing ethylbenzene and C9+ compounds according to claim 1 , in which the separation unit (SMB-2) contains toluene as desorbent.

6. The process for the production of high-purity paraxylene based on a xylenes cut containing ethylbenzene and C9+ compounds according to claim 1 , in which the separation units (SMB-1) and (SMB-2) each contain from 6 to 24 beds, distributed over one or more adsorbers, the number of beds being adjusted so that each bed optionally has a height between 0.70 m and 1.40 m.

7. The process for the production of high-purity paraxylene based on a xylenes cut containing ethylbenzene and C9+ compounds according to claim 1 , in which the distribution of the quantity of solid adsorbent in the separation units (SMB-1) and (SMB-2) is as follows:
the quantity of solid adsorbent in a zone 1 is 17%±5%,
the quantity of solid adsorbent in a zone 2 is 42%±5%,
the quantity of solid adsorbent in a zone 3 is 25%±5%,
the quantity of solid adsorbent in a zone 4 is 17%±5%,

wherein the zones are as follows:
zone 1 is between the injection of the desorbent and the draw-off of the extract,
zone 2 is between the draw-off of the extract and the injection of the feedstock,
zone 3 is between the injection of the feedstock and the draw-off of the raffinate,
zone 4 is between the draw-off of the raffinate and the injection of the desorbent.

8. The process for the production of high-purity paraxylene based on a xylenes cut containing ethylbenzene and C9+ compounds according to claim 1 , in which, for the separation unit (SMB-1), a ratio by volume of desorbent to feedstock is at least 1.7/1.

9. The process for the production of high-purity paraxylene based on a xylenes cut containing ethylbenzene and C9+ compounds according to claim 1 , in which, for the separation unit (SMB-2), a ratio by volume of desorbent to feedstock is at least 1.7/1.

10. The process for the production of high-purity paraxylene from a xylenes cut containing ethylbenzene and C9+ compounds according to claim 1 , which is a process based on debottlenecking of an existing separation unit, constituted by 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 a separation unit (SMB-1), and
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 acting as a separation unit (SMB-2).

11. The process for the production of high-purity paraxylene based on a xylenes cut containing ethylbenzene and C9+ compounds according to claim 1 , in which 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 un

Assignees

• Ifp Energies Now

Inventors

• Dreux Heloise
• Leflaive Philibert
• Leinekugel Le Cocq Damien

Classifications

• C07C5/2775

  with crystalline alumino-silicates, e.g. molecular sieves · CPC title

• B01D15/1821

  Simulated moving beds · CPC title

• C07C5/2737 Primary

  with crystalline alumino-silicates, e.g. molecular sieves · CPC title

• C07C7/005 Primary

  Processes comprising at least two steps in series · CPC title

• C07C7/13

  by molecular-sieve technique · CPC title