KR101572702B1

KR101572702B1 - Novel system for optimising the production of high octane gasoline and the coproduction of aromatic bases

Info

Publication number: KR101572702B1
Application number: KR1020107015580A
Authority: KR
Inventors: 수히르 마띠유; 쟈끄 로
Original assignee: 아이에프피 에너지스 누벨
Priority date: 2007-12-17
Filing date: 2008-12-01
Publication date: 2015-11-27
Also published as: BRPI0822083A2; BRPI0822083B1; FR2925065A1; WO2009101281A3; FR2925065B1; CN102037102A; CN102037102B; KR20100093601A; WO2009101281A2

Abstract

The present invention relates to a process for the production of at least three units: an aromatic separation unit (SEP), a catalytic reforming unit (RC) and so-called < RTI ID = 0.0 & Relates to a continuum of aromatic units (CA), and the distribution between the production of high octane gasoline and the production of aromatic groups may change in some way.

Description

TECHNICAL FIELD [0001] The present invention relates to a novel system for optimizing the production of high octane gasoline and the co-

The present invention relates to the field of high-octane gasoline production for petrochemicals and the production of aromatic groups (xylene, toluene, benzene).

The configuration described in the present invention is characterized in that it comprises an aromatic separator unit (SEP), a catalyst reforming unit (RC) for the production of high-octane gasoline (octane number greater than 95) and hydrogen rich gas, and xylene, benzene, A unit known as an aromatic compound synthesis unit (CA) is used which essentially allows the production of the same aromatic group.

The present invention also allows the catalyst reforming operating conditions to be optimized, resulting in more high-octane gasoline than using the prior art configuration for a given capacity.

Another advantage of the arrangement according to the invention is that it permits an increase in the production of para-xylene for a given amount of filler in the aromatics composite according to one variant of the configuration.

Finally, this configuration is essential to the overall economics of the refinery configuration where the hydrogen requirements are constantly increasing to achieve various hydrotreatment and hydrogenation, and the overall hydrogen yield of the process is clearly improved compared to prior art configurations.

Traditionally, the purpose of the catalytic reforming unit is to convert naphthenic and paraffinic compounds (n-paraffin and iso-paraffin) into aromatics. The main reactions used are dehydrogenation of naphthenes to aromatics and dehydrocyclisation of paraffins to aromatics and isomerisation of paraffins and naphthenes. Hydrocracking and hydrogenolysis of paraffins and naphthenes, hydrogen-dealkylation of alkylaromatics that produce hard compounds and harder aromatics, and formation of coke on the surface of catalysts Other so-called "parasite" reactions may occur.

The performance that must be optimized for gasoline applications is the yield of liquid reformate and the octane number of the reformate, while the performance sought in petrochemical applications is the yield of aromatic materials and the distribution of the resulting aromatics. The aromatics are generally treated in the aromatics synthesis section to maximize the production of one or more products, usually xylene and benzene. Toluene and heavier aromatics can be engineered to constitute gasoline feedstocks or to produce a xylene mixture.

The conventional packing of the catalytic reforming unit is rich in paraffinic compounds and naphthenic compounds and relatively low aromatic compounds. This packing is typically naphtha coming from a crude distillation or natural gas condensate.

In addition to conventional fillers, variable soluble aromatics, such as catalytic cracking (FCC), coking, heavy naphtha from hydrocracking, or other available fillers including gasoline from steam cracking, are found in refineries. Such fillers varying in their content in aromatic compounds can be used to fill the catalyst reforming unit for the production of gasoline or aromatic groups.

There are certain drawbacks to directing a charge containing a significant amount of aromatics directly to the catalyst reforming unit. First, since the aromatics need not undergo a reforming reaction, an increase in the capacity of the unit is useless. Second, such aromatic species may undergo a "para-site" reaction of hydrogen-dealkylation or a polycondensation reaction which causes coke deposition on the catalyst, which results in loss of yield of the aromatic material.

The presence of such paper fillers with high coking capacity generally results in an increase in the strength of the reforming, which leads to an increase in investment costs and operating costs.

There has been a proposal for a modification in the conventional configuration for recovering aromatic compounds contained in the reformer packing.

Thus, according to one approach for the production of benzene, US 2007/0129590 discloses a method applied to naphtha filling a conventional reformer using a platinum based and / or rhenium based catalyst which may or may not be doped .

The proposed arrangement consists of three fractions from a C6-C11 naphtha cut in a unit for the extraction of aromatics; Aromatic fractions, fractions of aromatic precursors, and raffinate fractions.

While the raffinate fraction is the final product, the aromatic precursor fraction is sent to a reforming unit operating at low intensities to convert the aromatic precursor into an aromatic material. The effluent from the reforming unit is sent to the extraction unit together with the naphtha in order to recover the aromatics and the unconverted aromatic precursor. These aromatics and unconverted aromatic precursors are recycled to the low-strength reforming unit until they are exhausted.

The arrangement described in the cited document comprises two separate cuts; That is, a fraction of the aromatic precursor and an extraction unit capable of recovering the non-aromatic compound in the raffinate fraction. This type of separation requires additional distillation and / or adsorption steps to obtain the naphthene-rich flow of the aromatic precursor fraction and the paraffin-rich flow of the second raffinate fraction.

In addition, the construction described in the cited document does not use paraffin available in the filler to produce the aromatics, which is not very suitable when the purpose is to maximize aromatic production or gasoline production. In fact, the paraffin recovered from the raffinate fraction is mainly n-paraffin or mono-branched paraffine, which is not the most interested species for gasoline applications.

The object of the arrangement according to the invention is to provide a highly flexible process arrangement in which the effluent can be sent for the production of a gasoline unit or for the production of an aromatic group. The arrangement according to the invention also makes it possible to avoid defects caused by the conversion of the aromatics-rich filler in the catalytic reforming unit and to improve the yield for the pursuing product.

The arrangement according to the invention also makes it possible to increase the flexibility of the catalytic reforming unit by improving the applicability of the catalytic reforming unit to changes in the composition of the packing or to the expansion of the source, with a limited impact on operating conditions and strength .

In order to facilitate understanding of the text, it should be understood that the "naphtha" is hereinafter referred to as a gasoline cut of any random chemical composition and having a distillation range between 50 ° C. and 250 ° C. The chemical groupings represented by the letters PONA (Paraffines for P, Olefins for O, N for Naphthenes for Naphthenes and A for Aromatics) may be arbitrary.

A wide range of aromatic groups includes xylene (para-xylene, meta-xylene, ortho-xylene), ethylbenzene, toluene and benzene, and possibly monomeric styrene, lt; / RTI > is a heavier aromatic material such as cumene or linear alkylbenzene.

The reformate is a high-octane gasoline cut having an octane number greater than 95 produced by the catalytic reforming unit.

High-octane gasoline is a high-octane gasoline having an octane number greater than 95, preferably greater than 98.

The present invention relates to a process for the separation of natural gas condensates from at least one of the following units: atmospheric distillation unit, FCC unit, caulking unit, steam cracking unit, hydrogen cracking unit, A process for producing high-octane gasoline having a octane number of more than 95, preferably more than 98, from the naphtha cut, and a process for co-producing an aromatic group.

In the process according to the invention, the naphtha packing 1 is sent to an aromatic separation unit (SEP), generally called the so-called "extract" cut 3 containing the majority of the aromatic material, Called "raffinate" cut (2).

In some cases, when the aromatics content of the naphtha packing is low, i.e. less than 30 wt%, preferably less than 20 wt%, and even more preferably less than 10 wt%, the aromatics separation step may be omitted, Quot ;, the naphtha may be sent directly to the catalytic reforming unit (RC).

Most commonly, when the filling consists of a naphtha with a high aromatic content (as determined to be greater than 30 wt%) and a naphtha with a low aromatic content, the consequent configuration is such that a portion of the naphtha packing with a low aromatic content Corresponds to the configuration of Figure 2, which is divided into direct sending to the catalytic reforming unit (RC) and sending a portion of the naphtha packing having a high aromatic content to the aromatic separation unit (SEP).

The aromatic separation unit (SEP) produces raffinate (14), which is almost free of aromatics and an aromatic-rich extract (3).

At least a part of the raffinate 14 mixed with a part of the packing 11 consisting of naphtha, possibly with a low aromatic content, is sent to the catalytic reforming unit RC, Hydrogen flows 5 and high-octane gasoline cuts 4 are formed to form part of the gasoline pool, which is possibly partially or completely recycled (stream 9 ') into the aromatics separation unit, 6 to the aromatics synthesis unit (CA), and

- all or part of the extract (3) is sent to the so-called aromatic compound synthesis unit (CA) to allow the production of aromatics (flows 7 and 8), and if there is another part of the extract (3) Is sent to gasoline "pool"

When the raffinate 14 is not entirely sent to the catalytic reforming unit RC, the portion 2 'not sent to the catalytic reforming unit RC forms part of the gasoline pool or is sent to a conversion unit such as a steam reforming unit .

The process according to the invention, in its most general form, involves the production of high-octane gasoline (4) and the production of aromatics (4), including the production of only two extreme cases: high-octane gasoline only, Flow 7 and 8). &Lt; / RTI >

These two extreme cases are preferably within the scope of the present invention.

According to one variant of the process for producing co-octane gasoline and co-production of aromatic groups having an octane number greater than 95 according to the invention, shown in Figure 2, the packing to be treated comprises at least one And a naphta cut 12 from a naphta cut 10 and a catalytic cracking unit (not shown in Fig. 2).

The naphta cuts 12 from the FCC are sent to the hydrotreating unit HDT1 and the resulting hydrotreated cuts 13 are sent to an aromatic separation unit SEP to produce a flow of the extract 3, The flow of the extract (3) is sent to the aromatics synthesis unit (CA).

The naphta cut 10 from the direct distillation is sent to the hydrotreating unit HDT2 and the hydrotreated cut 11 is then mixed with the raffinate 14 from the aromatic separation unit SEP, Thereby constituting the packing 2 of the reforming unit RC.

Catalyst reforming unit RC produces reformate 4 which at least a portion is sent to the aromatics synthesis unit CA to allow for the production of aromatics 7 and 8.

The catalytic reforming unit RC also produces a flow of hydrogen 5.

A portion of the extract 3 can be mixed with the reformate 4 and the resulting flux 6 'can be sent to the gasoline pool.

According to another variant of the process according to the invention, the packing 1 to be treated can be used for the following operations: direct distillation of crude oil, catalytic cracking, caulking, hydrocracking, steam cracking or random mixtures of various cuts from natural gas condensates And the packing to be treated may be sent as a mixture to a hydrotreating unit (HDT) located upstream of the aromatic separation unit (SEP).

In other cases, depending on the impurity content, especially the sulfur and nitrogen compounds, or the unsaturated compound content of the various cuts constituting the filler to be treated, some cuts constituting the filler may be sent to a separate hydrotreatment unit.

According to another variant of the process of the invention, all of the extract 3 coming from the aromatic separation unit (SEP) can be sent to the aromatics synthesis unit (CA).

According to another variant of the process according to the invention, all of the high-octane gasoline produced as a result of the catalytic reforming (RC) can be sent to the aromatics synthesis part (CA).

In some configurations that form part of the configuration of the present invention, the catalytic reforming unit RC operates at high velocities as follows:

- the average reactor inlet temperature between 450 ° C and 560 ° C,

- H2 / HC ratio between 1 mole / mole and 5 mole / mole,

An average reactor pressure between 3 bar and 16 bar (1 bar = 10 ⁵ Pa)

- the mass space velocity between 1 kg filler / (kg catalyst .h) and 5 kg filler / (kg catalyst .h).

1 shows a process configuration according to the invention in a very general manner, comprising an aromatic separation unit (SEP), a catalytic reforming unit (RC) and a so-called aromatics synthesis unit (CA). In Fig. 1, the unit or line shown by the dashed line represents an optional component.
Figure 2 shows one particular configuration according to the present invention for the purpose of maximizing para-xylene production.
Figure 3 shows a prior art configuration that does not include an aromatics separation unit.

The following detailed description will provide a better understanding of the operation of the unit used in the arrangement according to the invention. Will be described with reference to Fig.

The present invention relates to a process for the production of a) high-octane gasoline, i. E. Obtaining gasoline having an octane number greater than 95, and b) obtaining at least an aromatic group, Namely, an aromatic material separation unit (SEP), a catalyst reforming unit (RC), and a so-called aromatic material synthesis unit (CA).

The naphtha packing 1 after hydrotreating, possibly shown as units denoted by (HDT) in Figure 1, comprises a so-called "extract" cut 3 containing the bulk of the aromatics and a non- Is sent to an aromatic material separation unit (SEP) producing so-called "raffinate" cuts 2, at least a portion of raffinate 2 is sent to a catalytic reforming unit RC, A so-called " reformate "gasoline cut 4 and a hydrogen flow 5 of high-octane constituting a part of the gasoline pool are produced, which can be completely or partially recycled to the aromatics separation unit ') Stream 6 to the aromatics synthesis unit (CA) and the extract (3) is wholly or partly sent to the so-called aromatics synthesis unit (CA) From an aromatic group (flow 7 and 8) is generated, and the other part if the other portion of the extract (3) is sent to the petrol "pool" flow through 9.

When part 9 'of the reformate 4 is recycled to the aromatic separation unit SEP, this part 9' is preferably a fraction of C6, C7 and C8 contained in the reformate 4, .

When the raffinate 2 is not entirely sent to the catalytic reforming unit RC, the part 2 'not sent to the catalytic reforming unit RC constitutes part of the gasoline pool or is converted into a conversion unit such as a steam reforming unit Can be sent.

In one particular case a) of the process according to the invention, all of the extract (3) is sent to the aromatics synthesis part (CA) and most of the reformate (4) is fed via flow 6 to the aromatics synthesis part By recycling it is possible to maximize the production of aromatic groups (flows 7 and 8).

In another particular case b) of the process according to the invention the production of the high-octane gasoline (stream 4) is carried out by sending most of the extract 3 to the gasoline pool via the flow 9 and sending all of the reformate 4 to the gasoline pool Can be maximized.

All intermediate variants between the above examples a) and b) are clearly possible and are based on the recycle level of the extract 3 to the gasoline pool via the flow 9 and the reformate 4 to the aromatics composition CA via the flow 6, Lt; / RTI >

In another specific case of the process according to the invention, it is possible to obtain only the reformate (4) and the extract (3). This occurs in practice when the extract 3 produced in an aromatic separation unit (SEP) is sent to an aromatics synthesis unit which can not be present at the location where the aromatics separation unit and the catalyst reforming unit are located and which can be provided at different locations.

When the aromatic compound synthesis part is located in a separate place from the aromatic separation unit and the catalytic reforming unit, it is considered to be equivalent to the case where all the units are located in the same place, and are thus completely within the scope of the present invention.

In another variation of the process of the present invention, it is possible to send all of the reformate (4) to the gasoline pool and send all of the extract (3) to the aromatics synthesis section.

The flexibility of the arrangement according to the invention is an important aspect distinguishing the arrangement of the invention from the arrangement of the prior art.

In the following description, it provides information on 1) an aromatic separation unit, 2) a catalyst reforming unit, and 3) an aromatic compound synthesis unit.

1) Separation units (SEPs) for aromatic compounds, generally having from 6 to 11 carbon atoms, can be prepared by known methods known to those skilled in the art, such as liquid-liquid extraction or extractive distillation using one or more solvents, Process. The process according to the present invention is not associated with any particular technology, so long as the aromatic separation unit is concerned.

The aromatics separation unit may be configured to extract only a portion of the aromatics contained in the charge, for example, compounds having 6 to 10, 6 to 9, or 6 to 8 carbon atoms. Thus, the remainder of the aromatics, C11, C10 to C11, or C9 to C11 aromatics, will be found in raffinates.

In the following examples, the aromatics are separated according to liquid-liquid extraction techniques. The extraction is carried out by the use of a sulfolane-type solvent of the formula C4H8O2S, which has a strong affinity for an aromatic compound. The product from the aromatics separation unit is an "extract" (3) in which the non-aromatics compound is enriched "raffinate" (2) and the aromatics contained in packing (1) are enriched.

(2) in which the packing (1) after hydrotreatment, possibly after the hydrotreatment, is in contact with the solvent in a first extraction column and a solvent and a nonaromatic compound rich in aromatics from the extraction column Is recovered. Raffinate (2) is then purified in a washing column to remove residual amounts of solvent.

First, in a "stripping" column, the non-aromatics are stripped from the solvent rich in aromatics, and then the solvent rich in aromatics is sent to the column for the recovery of the aromatics. After regeneration, the solvent is recycled and the aromatics are recovered in the extract (3).

2) The catalytic reforming unit (RC) operates under operating conditions that depend on the product sought and the packing to be converted in order to optimize the yield of the product pursued.

If necessary, the filler that arrives for catalyst modification may be hydrotreated to obtain the requirements relating to the content of sulfur, nitrogen and olefinic and diolefinic compounds.

Generally, there are three, four or five reactors constituting the catalyst reforming unit. Also, the catalyst used is a catalyst system selected according to operating conditions. The catalyst is typically an activated platinum group and the activator may be any combination of Re, Sn, In, P, Ge, Bi, boron, iridium, rare earth elements, Preferably, the catalyst activator of the catalytic reforming unit will be selected from Sn, In, P.

The catalytic reforming unit may require a fixed bed or moving bed technique.

The catalytic reforming unit in the fixed bed or mobile bed or the catalytic reforming unit as a combination of the two techniques typically operates within the following operating ranges:

An average reactor inlet temperature between 400 ° C and 560 ° C,

- H2 / HC ratio between 1 mole / mole and 10 mole / mole,

An average reactor pressure between 3 bar and 37 bar (1 bar = 10 ⁵ Pa)

It is desirable that the catalytic reforming unit operate within the scope of a so-called continuous regeneration process in which the operating range is more stringent, namely:

- the average reactor inlet temperature between 450 ° C and 560 ° C,

- H2 / HC ratio between 1 mole / mole and 5 mole / mole,

An average reactor pressure between 3 bar and 16 bar,

3) The aromatics synthesis section represents a combination of different sorting units, such as adsorption units, distillation units, extractive distillation units, liquid-liquid extraction units, or crystallization units, and / or conversion units, An aromatic dealkylation or alkylation unit, either selective or not, for the rearrangement of aromatics such as transaclylation or disproportionation treatments, or an isomer of xylene with or without dealkylation of ethylbenzene It is a unit for isomerisation.

The product from the aromatics synthesis part is mainly intermediate petrochemicals, and here, benzene, para-xylene, auto-xylene, meta-xylene, xylene cut, ethylbenzene, styrene monomer, cumene Quot;), or "aromatic group " such as linear alkylbenzene, or a component for constituting a gasoline group such as toluene, or a cut of heavy aromatic material.

If necessary, the filler arriving at the aromatics synthesis section can be hydrotreated.

Example

The following examples compare the configurations of two processes: one configuration is according to the present invention (as shown in FIG. 2), one configuration is according to the prior art, and there is no aromatic separation unit (as in FIG. 3).

In both of the constitution of the prior art and the constitution according to the present invention, the catalyst modifying unit RC and the aromatic material synthesizing unit CA are the same.

In both cases, the packing considered is:

- A heavy naphtha cut (10) resulting from the direct distillation of crude oil in the distillation range between 60 ° C and 165 ° C along the actual distillation curve (so-called "TBP" curve).

- A naphtha curve (12) originating from a catalytic cracking unit (FCC) in which the aromatics are enriched.

This type of packing is dedicated to the production of gasoline or light olefins for the petrochemical industry and operates at high strengths (reactor outlet temperature above 550 占 폚 and ratio of catalyst flow rate to filler flow rate above 10) (Denoted as FCC), using a particular combination of catalysts, either doped or undoped.

When attempting to maximize the propylene yield of the FCC, as in the case of this example, the content of aromatic compounds of the naphtha cut produced in the FCC is actually significantly increased.

The chemical grouping of the two charges (PONA) is given in Table 1 below:

Description of the Prior Art Configuration

The prior art configuration is as shown in Fig.

In the prior art configuration, a filling 21 consisting of a mixture of two cuts shown in Table 1 (naphtha cut 10 resulting from direct distillation of crude oil and naphta cut 12 from FCC unit) (HDT), where the hydrotreated effluent 22 is produced. This hydrotreating is a requirement for impurities (less than 100 Bromine of olefins and diolefins, 1 ppm wt. Or less of sulfur, and 1 ppm wt. Or less of nitrogen) for the catalyst reforming unit (RC) So that the catalyst reforming unit (RC) can be filled.

The reformed product 24 in which the hydrotreated stream 22 constitutes the packing of the catalytic reforming unit RC and the catalytic reforming unit RC is fed to the aromatic compound synthesis unit CA and the hydrogen rich gas 23 ).

The catalyst reforming unit (RC) operates under the following conditions:

Reactor inlet temperature: 510 ° C

Pressure: 4.5 bar

H2 / HC ratio: 3.0

The same aromatic compound synthesis portion as used in the construction of the process according to the present invention will be described below.

This aromatic compound synthesis unit (CA) produces para-xylene (27) and benzene (28).

Description of the configuration according to the present invention

The configuration of the process according to this embodiment is shown in Fig.

The filling is the same as the filling of the prior art configuration as follows;

- Cutting naphtha from direct distillation of crude oil (10)

- A naphtha cut (11) from an FCC unit, where the aromatic compound is enriched.

1) The initial hydrotreatment of the naphtha filler from the FCC requires the requirements for impurities that the catalyst reforming unit (RC) may include (less than 100 bromine index of olefins and diolefins, 1 ppm wt or less of sulfur, and 1 lt; RTI ID = 0.0 > ppm) < / RTI >

Since gasoline from the FCC after hydrotreating contains about 67% aromatic compounds compared to the gasoline from the direct distillation containing only 7% aromatics, only gasoline from the FCC after the hydrotreatment contains only aromatics extraction unit Lt; / RTI >

The effluent from the aromatics extraction unit (SEP) is as follows:

- an extract (3) which is all sent to the aromatics synthesis part (CA), and

- raffinate (14) mixed with heavy naphtha (11) from the hydrotreated direct distillation to constitute the packing (2) of the catalytic reforming unit (RC).

The chemical grouping (PONA) of the charge of the catalyst reforming unit is given in the following Table 2 for the prior art and the present invention.

2) The catalytic reforming unit (RC) operates under the following conditions:

Reactor inlet temperature: 520 ° C

Pressure: 4.5 bar

H2 / HC ratio: 1.5

The reformate 4 produced by the catalytic reforming unit is all sent to the aromatics synthesis unit CA (flow 6) to produce para-xylene 7 and benzene 8.

Table 3 below shows the relationship between the capacity of the catalyst reforming unit RC and the operating conditions thereof, the average pressure P of the reactor, the average reactor inlet temperature T, and the recirculation rate ({H2 / HC} ratio.

In the case of the present invention,

- two prior art cases referring to a) and b) having the following meaning:

- Case A corresponds to a prior art configuration with a catalytic reforming unit having the same packing of catalyst as used according to the invention.

The capacity of the catalytic reforming unit is 77 (arbitrary unit) for the configuration according to the present invention and 100 (arbitrary unit) for the prior art configuration due to the aromatic material missing upstream of the catalytic reforming unit.

Therefore, the space velocity is in the same ratio as for the filling, i.e. 77 according to the invention and 100 according to the prior art.

- Case B corresponds to a prior art configuration having a reforming unit operating with more catalyst filler, to allow comparison between prior art configurations and configurations according to the present invention, given the same catalyst reforming space velocities.

The configuration according to the invention allows operation under optimal catalyst reforming conditions since this optimum catalyst reforming condition is more advantageous for the improved selectivity of the aromatics: specifically, the H2 / HC ratio is divided by 2 And the temperature is increased by 10 ° C.

3) In the prior art construction and the construction according to the present invention, the same aromatic material synthesis portion is composed of the following units:

Two conversion units

- One unit for transalkylation of toluene and C9 + aromatics to produce C8 aromatics and benzene.

- One unit for isomerization of xylene and dealkylation of ethylbenzene.

Various classification units:

A fractionation column for all of the hard (C7 < - >) reformate and the C8 + reformate,

- fractionation column for C8 + aromatic cuts with C8 cuts and C9 + aromatic cuts,

- fractionation columns for C9 + aromatic cuts and C9-C10 rich cuts and cuts of heavier aromatics,

An extractive distillation unit for separating the aromatic cuts of benzene and toluene from the non-aromatics,

- a BT fractionation zone consisting of a column of benzene and a column of toluene,

- a unit for the separation of para-xylenes from C8 aromatic cuts by adsorption.

More specifically, the aromatics synthesis section operates in the following manner with reference to Figure 2:

The reformate (6) is sent to the fractionation column which separates the hard reformate (C7 < - >) from the C8 + reformate. The hard reformate is sent to an extractive distillation unit for separating enriched aromatic cuts of benzene and toluene from non-aromatics. Benzene and toluene enriched aromatic cuts are sent to the fractionation column to separate the benzene from the toluene used as the reagent in the transalkylation unit as the end product of the synthesis part. The heavier aromatics (C8 +) are mixed with the C8 + reformate.

The C8 + reformate is sent to a fractionation column (column of xylene) that separates the C8 aromatics from the heavier aromatics. The C8 aromatics are subsequently classified to send the aromatic cuts rich in C9-C10 type carbon atoms as reactants to the transalkylation unit.

In this unit, toluene reacts with heavier aromatics to produce C8 aromatics and benzene. Recirculation of the effluent to the BT fractionation zone allows classification of unconverted products and reactants, so that the unconverted products and reactants recombine with the C8 aromatics at the top of the column of xylene. This C8 cut is then converted to para-xylene, which is separated from the other isomers by an adsorption process. The effluent is then sent to a unit for isomerization of xylene where the balance between the various xylene isomers is restored and the ethylbenzene is converted to benzene by dealkylation. The isomerization effluent is recycled to the column of xylene until the fresh charge is depleted of all the xylene. As a result, para-xylene (7) is the main product of the synthesis and benzene (8) is the main product.

Considering an assembly comprising an " aromatic separation unit + catalytic reforming unit ", Table 4 below compares the production of the products described as hydrogen (H2), liquid reformate (C5 +) and aromatic compound.

The following Table 4 compares the performance of the catalyst reforming catalyst in terms of aromatic selectivity (STA) and the conversion of the prior art and the non-aromatics (C6 + NA) according to the present invention.

Compared with prior art A, the configuration according to the present invention allows greater production of liquid reformate, hydrogen, and aromatics, and also allows for better retention of the heavy aromatics (C8 +).

The B configuration of the prior art makes it possible to produce more hydrogen and aromatic compounds (reducing the yield of liquid reformate) than the prior art A case, but the yield is lower than that obtained by the configuration according to the invention maintain.

Also, the distribution of the resulting aromatics is different from that of the present invention: the more benzene and toluene are produced, the less C9 + aromatics are produced, which affects the performance of the downstream aromatics synthesis part.

From the study of the performance of the catalytic reforming unit, it can be seen that the conversion of the non-aromatic C6 + compound is definitely increased in the B case compared to the case A, and the selectivity for the aromatic compound is clearly less than that achieved by the arrangement according to the invention .

None of the prior art A and B cases can achieve the yield of the present invention.

caution

The selectivity for aromatic compounds (mol / mol) is defined as the ratio of moles of aromatic compounds produced to moles of converted non-aromatic C6 + compounds.

The conversion of the C6 + non-aromatics in the charge is defined as the ratio of moles of converted non-aromatic C6 + compounds to moles of non-aromatic C6 + compounds at the inlet.

Table 5 below compares the production of para-xylene and benzene at the exit from the aromatics synthesis unit (CA).

The production of para-xylene according to the invention increases by 2.5 w / h compared to case A and 2.2 w / h compared to case B, which is of great significance.

Compared to case A, prior art B configuration certainly produces slightly more para-xylene. However, the ratio of para-xylene / benzene produced is overall reduced.

Therefore, the configuration according to the present invention makes it possible to maximize para-xylene production.

Claims

A process for the production of gasoline having an octane number greater than 95 and for the co-production of aromatic groups, wherein the packing (1) to be treated in this process comprises several sources (direct distillation, catalytic cracking unit, coker, steam reforming unit , &Lt; / RTI > or a classification of natural gas condensate)
A portion of the charge with a high aromatic content (greater than 30 wt%) as indicated by flow 12 is sent to the hydrotreating unit HDT 1 and the resulting hydrotreated cut 13 is sent to an aromatic separation unit (SEP) (14)
A portion of the filler having a low aromatic content (less than 30 wt%) as represented by the flow 10 is sent to the hydrotreating unit HDT2 and the resulting hydrotreated cut 11 is transferred to the reclaimed fraction from the aromatics reforming unit (SEP) Nate 14 to constitute the packing 2 of the catalyst reforming unit RC,
At least a portion of the extract (3) coming from the aromatic separation unit (SEP) is sent to an aromatic compound synthesis unit (AC) to produce aromatic groups (7 and 8), and another part of the extract (3) To the gasoline pool,
- the catalyst reforming unit (RC) produces a reformate (4) and a hydrogen flow (5), at least a part of the reformate (4) being sent to the aromatic compound synthesis unit (CA) A process for the production of gasoline having an octane number of more than 95, and another process for producing an aromatic group, wherein another portion of the reformate (4) is sent to the gasoline pool through the flow 6 '.

The process according to claim 1, wherein all of the extract (3) from the aromatic material separation unit (SEP) is fed to an aromatic compound synthesis unit (CA), producing gasoline having an octane number greater than 95, For the process.

The process according to claim 1, wherein all of the reformates (4) produced by the catalytic reforming unit (RC) are fed to an aromatic compound synthesis unit (CA), the production of gasoline having an octane number greater than 95, Process for generation.

2. The process according to claim 1, wherein the catalyst reforming unit (RC)
- the average reactor inlet temperature between 450 ° C and 560 ° C,
- H2 / HC ratio between 1 mole / mole and 5 mole / mole,
An average reactor pressure between 3 bar and 16 bar,
Production of gasoline having an octane number greater than 95, operating at a mass space velocity between 1 kg of filler / (kg of catalyst .h) and 5 kg of filler / (kg of catalyst .h) .

The catalyst according to claim 1, wherein the catalyst reforming unit (RC) comprises a Pt-based catalyst activated by an element selected from the following elements: Re, Ge, Bi, boron, iridium, &Lt; / RTI > and a process for the co-generation of an aromatic group.

The process according to claim 1, wherein the production of gasoline having an octane number greater than 95, in which a portion (9 ') of the reformate (4) coming from the catalytic reforming unit (RC) is recycled to the aromatics separation unit, Process for generation.

The process according to claim 1, wherein the production of gasoline having a low aromatic content of less than 20 wt% as represented by stream 10, and the co-production of aromatic groups.

2. The process of claim 1, wherein the catalyst reforming unit (RC) is a gas reforming unit for producing gasoline having an octane number greater than 95, using a Pt-based catalyst activated by an element selected from the following elements: Sn, Process for the co-production of aromatic groups.