Title of Invention	A PROCESS FOR THE PRODUCTION OF PARAXYLENE OF HIGH PURITY
Abstract	The present invention relates to a process for the production of paraxylene high purity from a change containing a mixture of aromati hydrocarbons having 7 to 9 carbon atoms, conprising circulating at least a portion of the charge in an enrichment zone to produce a first fraction with paraxylene, purifying at least a portion of said first fraction in a purification zone by at least one crystallization in at least one crysallization zone, said crystallization zone comprising at least two crystallization stages at a temperature between +50and -22F and recovering pararxylene crystals from each crystallization stages. PRICE: THIRTY RUPEES

Title of Invention

A PROCESS FOR THE PRODUCTION OF PARAXYLENE OF HIGH PURITY

Abstract

The present invention relates to a process for the production of paraxylene high purity from a change containing a mixture of aromati hydrocarbons having 7 to 9 carbon atoms, conprising circulating at least a portion of the charge in an enrichment zone to produce a first fraction with paraxylene, purifying at least a portion of said first fraction in a purification zone by at least one crystallization in at least one crysallization zone, said crystallization zone comprising at least two crystallization stages at a temperature between +50and -22F and recovering pararxylene crystals from each crystallization stages. PRICE: THIRTY RUPEES

Full Text	The invention relates to a process for separating and preparing paraxylene from a mixture of aromatic hydrocarbons comprising xylene isomers. The xylene isomers are orthoxylene, metaxylene, paraxylene and ethylbenzene. The main application of the invention is in obtaining paraxylene to a degree of purity that is sufficient for the synthesis, for example, of terephthalic acid, used in the preparation of synthetic fibers and particularly polyester. The applicant has described in a patent FR 2,681,066 (US 5,284,992), which is incorporated as a reference, a process for separating and recovering paraxylene contained in a charge of hydrocarbons comprising essentially aromatic hydrocarbons having 8 carbon atoms. This process comprises the combination of an enrichment step, which is a selective adsorption on an adsorbent in a simulated moving bed, of a charge containing essentially the xylene isomers, which makes it possible to substantially enrich a first adsorption effluent with paraxylene, and of a purification, which is a crystallization, in at least one crystallization unit operating at high temperature, of the paraxylene-enriched effluent so as to obtain paraxylene having a very high purity, the mother liquor being recycled to the adsorption step. This high-temperature crystallization corresponds to the second crystallization step of the conventional crystallization processes (Chevron ; Arco) which generally comprise a first crystallization at low temperature (-40 to -70°C) and a second crystallization to purify, at high temperature (0 to -20°C, for example), crystals obtained that were previously remelted. Furthermore, a second fraction depleted of paraxylene and therefore enriched with ortho- and meta-xylene as well as ethylbenzene, delivered by the selective adsorption unit, is sent into an isomerization unit to increase its concentration of paraxylene to a value close to equilibrium and approximately close to or greater than the composition of the initial charge of hydrocarbons, and the isomerate obtained can then be recycled to the adsorption. In the adsorption, crystallization and isomerization sequence described, various types of impurities can appear in the various effluents and cause disturbances in the operation of the units/ which are detrimental to the yield obtained and to the purity of the paraxylene recovered. First of all, during isomerization of the paraxylene-depleted fraction, olefinic hydrocarbons can be produced in a variable amount depending on the values of the partial pressures of hydrogen introduced. The subsequent formation of polymers and their passage into the adsorption unit can cause serious problems of circulation through the adsorbent, even deactivate it. In addition, paraffinic and naphthenic hydrocarbons having 8 and 9 carbon atoms, whose volatility is between that of toluene, a desorption solvent for example, and that of the xylenes, are intermediate products of the conversion of ethylbenzene into xylenes during the isomerization and their accumulation can prove to be harmful. Furthermore, aromatic hydrocarbons having 9 carbon atoms, present in low proportion and poorly separated in distillation columns, can be detrimental to the process, such as aldehydes and ketones that are heavier than the initial charge, which are formed when oxygen is accidentally dissolved. Finally, another problem is linked to the presence of methanol. This alcohol is sometimes added in low proportion in mixtures of xylenes to be crystallized to prevent the cocrystallization of water and paraxylene. Actually, the dry Cg-aromatic mixtures are relatively hygroscopic and when the suspension of paraxylene crystals in the mother liquor passes into the centrifuges, water contained in the ambient air can be absorbed into the mother liquor and this water can possibly crystallize in conjunction with the temperature of this mother liquor. In addition, some exchangers can have leaks and some water can accidentally pass into the mixture to be crystallized. An object of the invention is to improve the recovery of the paraxylene produced and to minimize the energy cost, particularly of the purification step. Another object of the invention is to eliminate these drawbacks and to limit in particular how much of these various impurities the adsorption section contains to seek to optimize it, to the extent that the adsorbent is very sensitive to the impurities of the charge of the adsorption zone. This invention relates to a process for producing paraxylene of very high quality from a charge containing a mixture of aromatic hydrocarbons having 7 to 9 carbon atoms in which at least a portion of the charge is made to drculate in a so-called enrichment zone suited to enrich a first fraction of paraxylene and at least a portion of said first fraction is purified in a so-called purification zone by at least one high-temperature crystallization in at least one crystallization zone, the process being characterized in that said first paraxylene-enriched fraction is crystallized in a purification zone comprising at least two crystallization stages at high temperature, and advantageously between +10 and -ZS^C. By high-temperature crystallization of the paraxylene is meant a crystallization of a solution or suspension of paraxylene that is already enriched with paraxylene, which corresponds to what the literature calls a purification step. For example, the patent US 2,866,833, incorporated as a reference, mentions a step for purifying paraxylene at -34°C. Earch crystallization stage can comprise one or more crystallizes. According to a first variant, the enrichment zone of the first fraction having at least 30% weight of paraxylene can be at least one very low-temperature crystallization zone, for example lower than -40°C, known as a recovery section, in which a charge containing a mixture of aromatic hydrocarbons having 8 carbon atoms is introduced, such as the one described according to the patent US 2,866,833 or such as the ones described according to patent US 5,329,061, incorporated as references. This enrichment zone delivers a suspension of crystals which is separated in a separation zone and the recovered crystals are melted and constitute at least a portion of said first fraction to be purified later on. In addition, a mother liquor resulting from the separation can be isomerized in an isomerization zone and the isomerate recycled at least in part to the enrichment zone (recovery section). According to a second variant, the paraxylene enrichment zone can be a selective adsorption zone of the charge containing a mixture of aromatic hydrocarbons having 8 carbon atoms delivering theparaxyleneenriched fraction. According to a third variant the paraxylene enrichment zone can be a disproportionation zone of a charge consisting essentially in toluene and using a coke-selectivated catalyst or a silicon-selectivated catalyst according to the patents US-4.117.026,4.097.543,4.851.604,5.173.461, 5.243.117 and U&-5.321.183 incorporated by reference. The unreacted toluene and the benzene are avantageously removed by distillation from the disproportionation effluent comprising the xylenes. It is advantageous to have at the output of the enrichment zone, i.e., for example of the selective adsorption zone as described in the patent US 5,284,992 of the applicant, an effluent containing more than 50% by weight of paraxylene and preferably 75 to 98%. Another alternative for producing paraxylene may result from the combination of an adsorption, an isomerization, and a :rystallization step in a single stage at high temperature. According to a variant of the invention, the process comprises, in combination, an adsorption operation and a crystallization operation. According to this variant, at least a portion of the charge and/or of the products resulting from the crystallization, for example the mother liquor, undergoes a clay treatment operation. At least a portion of the effluent resulting from the clay treatment operation is recycled to undergo an adsorption operation. This invention also applies to a process comprising, in combination, besides the operations of adsorption and crystallization, an isomerization step. In this case, at least a portion of the isomerate can be clay treated. This invention relates furthermore to a process for separating and recovering paraxylene from a charge that can contain metaxylene, this process comprising, in combination, an adsorption operation and a crystallization operation. According to this process, at least a portion of the mother liquor coming from the crystallization operation is purified by distillation before being recycled to the adsorption operation. This invention also relates to a process for separating and recovering paraxylene contained in a charge of hydrocarbons comprising Cg-aromatic hydrocarbons, a process in which in particular: • in at least one adsorption zone, said charge containing at least metaxylene, paraxylene is put in contact with at least one adsorbent in the presence of at least one suitable desorption solvent under adsorption conditions such that there is obtained a first fraction containing solvent, metaxylene and optionally ethylbenzene and/or orthoxylene and a second fraction containing solvent of the substantially enriched paraxylene; • the first fraction is distilled to recover a mixture of metaxylene and optionally ethylbenzene, and/or orthoxylene; • said mixture is isomerized at least in part under suitable conditions in at least one isomerization zone and an isomerate is recovered that is recycled at least partially to the adsorption zone; • said second fraction is distilled to obtain substantially enriched paraxylene and a crystallization of the substantially enriched paraxylene is performed obtaining, on the one hand, a mother liquor that is at least partially recycled to the adsorption step and, on the other hand, paraxylene crystals. According to another variant embodiment of the process according to the invention, it is possible to have at least a portion selected from the charge at least in part, the isomerate at least in part and the mother liquor at least in part circulate in at least one clay, or equivalent material, treatment zone and a first effluent is recovered that is introduced at least in part into the adsorption zone to produce said first and second fractions that are drawn off from the adsorption zone. More specifically, the invention relates to a process for separating and recovering paraxylene contained in a charge of hydrocarbons comprising Cg-aromatic hydrocarbons, the process comprising the following steps: a) in an adsorption zone, said charge containing metaxylene, paraxylene and optionally ethylbenzene and/or orthoxylene is put in contact with an adsorbent in the presence of a suitable desorption solvent under adsorption conditions such that a first fraction containing solvent, metaxylene and optionally ethylbenzene and/or orthoxylene and a second fraction containing solvent and substantially enriched paraxylene are obtained; b) the first fraction is distilled to separate the solvent on the one hand, and the mixture of metaxylene and optionally ethylbenzene, and/or orthoxylene, on the other hand; c) said mixture is isomerized under suitable conditions in an isomerization zone and an isomerate is recovered that is recycled at least in part to step a); d) the second fraction is distilled and the solvent on the one hand, and substantially enriched paraxylene, are recovered; e) a crystallization of the paraxylene of step d) is performed in at least one crystallization zone at high temperature, advantageously between +10°C and -25°C and there is obtained, by separation, on the one hand, a mother liquor that is recycled at least in part to step a) and, on the other hand, paraxylene crystals saturated with mother liquor; f) the paraxylene crystals are washed with a suitable washing solvent in a washing zone and paraxylene crystals having a very high degree of purity are recovered; According to another variant of the invention, it is possible to have at least a portion selected from the charge, the isomerate and the mother liquor circulate in at least one clay treatment zone and a first effluent is recovered that is introduced into the adsorption zone to produce said first and second fractions of step (a). At least a portion of the charge of hydrocarbons can be pretreated in a clay-treatment reactor. It can be advantageous to put the isomerate in a clay-treatment reactor before being sent into the adsorption. These reactors can be independent or form only a single reactor, optionally common with the one that treats the mother liquor. These clay treatments make it possible to eliminate at least in part the olefins created in particular in the isomerization step and at least a portion of the heavy impurities, which circulate in the adsorption, crystallization and isomerization loop. Various variants can be envisioned: The mother liquor can be advantageously introduced at least in part into a distillation column downstream from the isomerization zone. This column also treats the effluent of the isomerization zone and delivers a top fraction containing light compounds (air, water, methanol, C^-) and another fraction containing a distilled mixture of mother liquor and isomerate that is then introduced into the clay treatment zone. A distillation bottom fraction containing heavy compounds can also be drawn off from this distillation column, which makes it possible to reduce the size of the downstream equipment. A portion of the mother liquor can also be mixed with the effluent, whatever it is, leaving the clay treatment zone, whether this is the effluent resulting from the circulation of the isomerate, the mother liquor and the charge in the clay treatment zone, or the effluent resulting from the circulation, in the clay treatment zone, of the latter and of the distillation fraction containing said distilled mixture of mother liquor and isomerate, before being introduced into the selective adsorption zone. The resulting effluent of the latter variants can be distilled in at least one distilling column (a so-called rerun column) that delivers a bottom fraction containing heavy compounds and a top fraction that is introduced into the adsorption zone optionally with a portion of the mother liquor. The conditions for adsorbing or eliminating the undesirable compounds on the clay are, as a general rule, the following: • Temperature: 100 to 300°C, preferably 160 to 230'C • Hourly space velocity: 1 to 8, preferably l to 4 (Hourly volume of charge per volume of clay) • Type of clay: activated natural aluminosilicates, for example the clay referenced F54 with ENGELHARD. • Pressure: 3 to 100 bar, preferably 4 to 20 bar. The distillation column, depending on the isomerization, generally has the following characteristics: • Pressure: 1 to 20 bar, preferably 3 to 8 bar • Base temperature: 150 to 280C, preferably 200 to 240°C • Number of plates: 30 to 80, preferably 50 to 70. The distilling column, known as rerun, located between the clay treatment zone and the selective adsorption zone usually has the following characteristics: • Pressure: 1 to 20 bar, preferably 3 to 8 bar • Base temperature: 160 to 290°C, preferably 210 to 250C • Number of plates: 40 to 200, most often 50 to 90. According to another characteristic of the invention, it is possible to keep the amount of constituents with intermediate volatility at a tolerable level. In this case, at least a portion of the mother liquor can be purged before being introduced into the clay treatment zone. It can also be advantageous to purge at least in part the desorption solvent resulting from distillation steps (b) and (d) • of the depleted fraction or of the paraxylene-enriched fraction before it is recycled and to compensate for the purge of the solvent by an addition of fresh solvent, either into the charge or upstream from the adsorption zone. As has been indicated, it is possible to recycle the crystallization mother liquor in different places of the installation depending on the magnitude of the amount of undesirable compounds, but it can be advantageous to combine these different recyclings with one another, for example, when it involves reusing existing pieces of equipment for the distillation of the isomerate, the clay treatment or the so-called rerun distillation and when one of these pieces of equipment is already operated at its maximum flow rate. It is also possible to combine these different recyclings and these purges when it is desired to have the amount of an impurity in the loop reduced without seeking to eliminate it altogether. The crystallization step of the paraxylene-enriched fraction is generally performed, as has been mentioned above, at high temperature, for example between +10 and -30°C and preferably +10 and -25°C. The temperature is usually selected as a function of the concentration of paraxylene that it is desired to have in the mother liquor, and of the economic cost of the crystallization operation. It is possible under these conditions to perform a crystallization of the paraxylene in a single stage when the paraxylene that is collected, for example as an extract of the adsorption unit, has a purity greater, for example, than 85%. But it can be advantageous, particularly for economic reasons, to perform a crystallization in several stages, for example a first crystallization at a temperature Tl between +10 and -10C, and a second crystallization at a temperature T2, lower than Tl, between 0 and -25°C. According to a first embodiment of the invention, a crystallization of the paraxylene of step (d) is performed in a single stage, a suspension of crystals in the mother liquor is recovered, the crystals are separated from the mother liquor in a separation zone, the crystals obtained are washed with the washing solvent, a washing liquor is recovered, at least a portion of the mother liquor and at least a portion of the washing liquor are recycled and the paraxylene crystals are melted completely so as to obtain a liquid stream of melted paraxylene. According to a second embodiment that uses a first variant of a two-stage crystallization of the paraxylene-enriched fraction, a first crystallization of the paraxylene of step (d) is performed in a first crystallization zone at a temperature Tl, a suspension of first paraxylene crystals in a first mother liquor is recovered, the first crystals are separated from the zone or to the very low temperature crystallization zone, the separated first crystals are melted and they are crystallized in a second crystallization zone at a temperature T2 that is higher than Tl, a suspension of second paraxylene crystals in a second mother liquor is recovered, the second crystals are separated from the second mother liquor in a second separation zone, the second crystals are washed with the suitable washing solvent in the second separation zone, a washing liquor is recovered, the second mother liquor, at least in part, and at least a portion of the washing liquor are recycled to the first crystallization zone and optionally in part to the second crystallization zone and the second paraxylene crystals are melted completely so as to obtain a liquid stream of melted paraxylene. For example, temperature Tl of the first crystallization can be -5 to -25°C while temperature T2 of the second crystallization can be +10 to -5°C. According to another embodiment of the invention, using a second variant of a two-stage crystallization, a first crystallization of the paraxylene of step (d) is performed in a first crystallization zone at a temperature Tl, a suspension of first paraxylene crystals in a first mother liquor is recovered, the first crystals are separated from the first mother liquor in a first separation zone, optionally the first crystals are washed with the washing solvent in the first separation zone, at least a portion of the first mother liquor is crystallized in a second crystallization zone at a temperature T2 that is lower than temperature Tl, a suspension of second paraxylene crystals in a second mother liquor is recovered, the second crystals are separated from the second mother liquor in a second separation zone, the second crystals are washed with the washing solvent in the second separation zone, a second mother liquor is recovered that is recycled at least in part to the adsorption zone or to the very low temperature crystallization zone, the first and second paraxylene crystals are mixed, they are melted completely and a stream of melted paraxylene is recovered. For example, the first crystallization can be performed at a temperature Tl between +10 and -10°C while the second T2, which is lower than Tl, can be performed between 0 and -250. According to another embodiment of the invention comprising a crystallization having several stages, a first crystallization of the paraxylene of stage (d) and of recycled partially melted or possibly melted crystals coming from a second crystallization afterward is performed in a first crystallization zone at a temperature Tl, a suspension of paraxylene crystals in a first mother liquor is recovered, the crystals are separated from the first mother liquor in a first separation zone, said crystals are washed, they are melted and a stream of melted paraxylene is recovered, at least a portion of the first mother liquor is crystallized in a second crystallization zone at a temperature T2 that is lower than temperature Tl, a suspension of second paraxylene crystals in a second mother liquor is recovered, the second crystals are separated from the second mother liquor in a second separation zone, a second mother liquor is recovered that is recycled at least in part to the adsorption zone, or to the very low crystallization zone, optionally the second crystals are melted and the optionally melted crystals are recycled to the first crystallization zone to recrystallize them with the paraxylene of step (d) at temperature Tl. Another variant can compnse a partial melting of the second crystals and a recycling of the obtained slurry to the first crystallization zone to recrystallize it with the paraxylene of step (d) at temperature Tl. According to another particularly advantageous embodiment of the invention, a first crystallization of the paraxylene of step (d) is performed in a first crystallization zone at a temperature Tl, a suspension of first paraxylene crystals in a first mother liquor is recovered, the first crystals are separated from the first mother liquor in a first separation zone, at least a portion of the first mother liquor is crystallized in a second crystallization zone at a temperature T2 that is lower than Tl, the second crystals are separated from the second mother liquor in a second separation zone, the second mother liquor is _recpvered. .that is recycled at least in part to the adsorption zone or to the very low temperature crystallization zone, the first crystals and the second crystals are recovered and they are washed in at least one separation and countercurrent washing zone with the suitable washing solvents, a washing liquor which is recycled at least in part to the first crystallization zone is recovered on the one hand, paraxylene crystals are recovered on the other hand, they are melted completely in a melting zone and a stream of melted paraxylene is collected. The invention also relates to a process for separating and recovering paraxylene contained in a charge of hydrocarbons comprising Cg-aromatic hydrocarbons, the process comprising the following steps: a) in at least one adsorption zone (8) , said charge (1) containing metaxylene, paraxylene and optionally ethylbenzene and/or orthoxylene is put in contact with an adsorbent in the presence of a suitable desorption solvent under adsorption conditions such that there is obtained a first fraction containing solvent, metaxylene and optionally ethylbenzene and/or orthoxylene and a second fraction containing solvent and essentially substantially enriched paraxylene; the first fraction is distilled (12) to separate the solvent on the one hand, and the mixture of metaxylene and optionally ethylbenzene, and/or orthoxylene, on the other hand; said mixture is isomerized under suitable conditions in an isomerization zone (21) and an isomerate (2) is recovered that is recycled at least in part to step a); the second fraction is distilled (16) and the solvent on the one hand, and substantially enriched paraxylene, are recovered; a crystallization of the paraxylene of step d) is performed in at least one crystallization zone (5a, 5b) at high temperature, advantageously between +10°C and -25'C and there is obtained, by separation, on the one hand, a mother liquor that is recycled (3) at least in part to step a) and, on the other hand, paraxylene crystals saturated with mother liquor; the paraxylene crystals are washed with a suitable washing solvent in at least one washing zone and paraxylene crystals having a very high degree of purity are recovered ; the process being characterized in that at least a portion of the mother hquor (3) (33) is introduced into a distillation column, a fraction containing purified mother liquor is obtained, a fraction which is then sent into adsorption zone (8). Of course, one will not go outside the scope of this invention by using a desorption solvent other than toluene such as in particular paradiethylbenzene (PDEB), this solvent, being heavier than the xylenes, will be recovered at the bottom of certain columns while the toluene was recovered at the top. Accordingly, the present invention provides a process for the production of paraxylene of high purity from a charge containing a mixture of aromatic hydrocarbons having 7 to 9 carbon atoms, comprising circulating at least a portion of the charge in an enrichment zone to produce a first fraction with paraxylene, purifying at least a portion of said first fraction in a purification zone by at least one crystallization in at least one crystallization zone, said crystallization zone comprising at least two crystallization stages at a temperature between +50 and -22°F, and recovering paraxylene crystals from each crystallization stage. Our co-pending application no.l741/MAS/95 provides a process for separating and recovering paraxylene from a charge optionally containing metaxylene. Our other co-pending application no.l726/MAS/95 provides a process for the production of paraxylene. The invention will be better understood in view of the following figures that illustrate in a nonlimiting way, several with reference to the accompanying drawing, m embodiments of the invention, / which: • figure 1 diagrammatically represents the process and the various possibilities for recycling the isomerate and the crystallization mother liquor to the adsorption via a clay treatment. • figures 2 and 3 illustrate a purification of paraxylene by crystallization in a single stage. • figures 4 and 5 show a purification of paraxylene by crystallization in a double stage, the first being colder than the second. • figures 6 to 10 represent a purification of paraxylene by crystallization in a double stage, the first being hotter than the second. The operating conditions and the adsorption in simulated moving bed (countercurrent, for example) are selected so that the first fraction containing metaxylene, orthoxylene and . . ethylbenzene is a raffinate and the second fraction containing essentially paraxylene is an extract. These conditions are described in the patent US 5,284,992. By a line l, a charge is conveyed that comprises about 20% ethylbenzene, 18% paraxylene, 45% metaxylene and 17% orthoxylene. Joined to it by a line 2 is a recycled effluent whose ethylbenzene content is appreciably lower, typically 8 to 13%, and which contains impurities. By lines 3 and 30, another recycled effluent is introduced whose paraxylene content is greater, typically 25 to 45%. A line 4 recovers the charge and these two effluents, it conveys a mixture of approximate composition, paraxylene 20 to 22.5, ethylbenzene 9 to 14%, orthoxylene 20 to 22.5%, metaxylene 45 to 50%, which is introduced into a simulated countercurrent adsorption zone 8 comprising one or more columns 6 and/or 7 filled with a zeolitic adsorbent, each of the columns being divided into a limited number of beds, the number of the beds of each column being able to be between 4 and 20, the productivity, expressed in relation to the paraxylene produced, being about 0.07 m3 per m3 of sieve and per hour expressed at ambient conditions. Desorbing is by toluene, at a rate of about 1.45 m3 of toluene per m3 of charge, the operating temperature being approximately 160°C. Drawn off from this unit by a line 10 is a paraxylene-depleted raffinate containing essentially toluene, metaxylene, ethylbenzene and orthoxylene and, by a line 9, an extract of paraxylene-enriched composition containing essentially toluene and paraxylene, the major impurity being ethylbenzene. The raffinate is introduced into a distilling column 12 (top temperature 125°C, bottom temperature 160'C, for example) . Drawn off at the top by a line into the adsorptinr). 14 is toluene (about 30% of the amount introduced/ for example) containing for example less than 2% of C8-aromatic compounds and, drawn off at the bottom of this column by a line 15, is a liquid (raffinate freed of solvent) rich in ethylbenzene, metaxylene and orthoxylene and depleted of paraxylene (less than 3%, for example) that is sent into an isomerization unit 21. This raffinate is put in contact with hydrogen introduced by a line 20 and with a catalyst having a base of mordenite and platinum on aluminum at about 380C. A line 22 conducts the isomerate from the outlet of the reactor to a flask for separating the gaseous constituents (not shown in the figure) , then to a distilling column 23 (top temperature 90°C, bottom temperature 160°C, for example). Drawn off at the top by a line 24 are C1 to C5 hydrocarbons, hexane, cyclohexane, benzene and toluene and at the bottom of this column by a line 2, an effluent containing 8 to 13% ethylbenzene, 21 to 24% paraxylene, 21 to 24% orthoxylene, 45 to 50% metaxylene and impurities, which is recycled to adsorption zone 8. Line 9 introduces the extract into a distilling column 16 from which toluene having less than 2% Cg-aromatic compounds into the adsorption, (about 70% of the amount introduced, for example) is drawn off at the top and is recycled by lines 17 and 11 to the feed of desorption solvent of the adsorption unit. At the bottom of column 16 at about 160°C, a stream enriched with paraxylene (at about 90% paraxylene) is drawn off by means of a line 19 which conducts it into a one-stage crystallization unit 5a for example operating at about -10'C. In this unit 5a, 5b paraxylene crystals are produced which are in suspension in a mother liquor. The crystals are separated in at least one centrifuge 5b for example and washed in the centrifuge. On the one hand, a paraxylene-depleted (about 54%) mother liquor is collected which is recycled by line 3 to adsorption zone 8 via clay-treatment and distillation zones discussed below and, on the other hand, paraxylene crystals, that are melted, are collected. The washing solvent, toluene for example, is brought by a line 18 and can, as shown in the figure, come from the distillation unit of raffinate 12 and/or from the unit for distillation of extract 16. There is recovered from unit 5b, after a distillation of the melted crystals not shown, liquid paraxylene with a purity for example equal to 99.75% by a line 25 and toluene that is recycled (line not shown) . Figure 2 illustrates more precisely the steps of crystallization and of downstream treatment of the paraxylene crystals with a washing with toluene. According to this figure, crystallization unit 50 in a single stage receives the crystallization charge (the distilled extract) by line 19. Crystals in suspension in a mother liquor are recovered by a line 51 and are separated at least in part in at least one centrifuge 52. A mother liquor containing for example 54% paraxylene is drawn off and recycled at least in part to adsorption zone 8 by lines 53 and 3, another part being able to be recycled to crystallization zone 50 by a line 53a. A portion of the crystals in suspension in the mother liquor can also be recycled in the crystallization zone by a line 51a. Then, recycled toluene coming from a distillation column 60 brought by a line 56, and toluene brought by a line 57 of fresh solvent coming from line 18 are introduced into centrifuge 52 as washing solvent. A washing liquor is collected separately by a line 54 that is connected to centrifuge 52, and it is recycled at least in part in the unit for distilling raffinate 12. The washed crystals of paraxylene are drawn off by a line 55, completely melted in a melting zone 58 and introduced into distillation column 60 by a line 59. At the bottom of the column, liquid paraxylene of very high purity is recovered, and at the top of the column, toluene is recovered which is recycled at least in part into centrifuge 52. At least one centrifuge was used to separate the crystals and the mother liquor. Also, at least one rotary filter could have been used instead of the centrifuge. According to a variant that is not shown, the centrifuge can be replaced by at least one column for separating and countercurrent washing, cited in the patents US 4 475 355, US 4 481 169, the NIRO column for example, incorporated as references. In this case, the mother liquor and the washing liquor are one and the same liquor which is optionally distilled before being recycled, at least in part, to the adsorption zone, via the clay treatment and distillation zones, and optionally in part in the crystallization zone. According to another variant illustrated by figure 3, it is possible to use another washing solvent such as the melted paraxyiene coming from melting zone 58. In this case of a figure having the same references for the same elements as those of figure 1, at least a portion of the melted paraxyiene is introduced countercurrent of suspension 51, by a line 59b, into a countercurrent column 80, a NIRO-type column for example, and is used to wash the paraxyiene crystals in the column. At least a portion of the melted paraxyiene that is introduced into the column crystallizes there. The crystals recovered from the column by line 55 are then melted in melting zone 58 and the liquid paraxyiene of very high purity is recovered by line 59. The washing liquor and the mother liquor are recovered at the same time by line 53 and are recycled to adsorption zone 8, a portion being able to be recycled to crystallization zone 50. If a washing solvent, for example pentane, other than the desorption solvent (toluene) and melted paraxyiene, were used, the process described according to figure 2 would be reproduced, except that the washing liquor coming from centrifuge 52 would have to be freed of solvent by a subsequent distillation (not shown in the figure) before being recycled to the adsorption or to the crystallization. The distilled solvent is then recycled into the centrifuge. The process according to figure 3 could also be reproduced with a countercurrent washing column and a washing solvent other than the melted paraxyiene and the desorption solvent. In this case, after complete melting of the crystals, a stream of melted paraxyiene containing washing solvent is distilled, solvent is recovered, at the top, that is recycled at least in part in the washing column and, at the bottom, paraxylene of very high purity-is recovered. The mother liquor comprising the washing liquor is drawn off from the washing column, distilled and recycled at least in part to the selective adsorption zone and optionally in part to the crystallization zone. Figures 4 and 5 illustrate a two-stage crystallization, the temperature of the second crystallization stage being higher than that of the first stage. According to figure 4, the first crystallization unit 50, at -20°C for example, receives the crystallization charge (the extract distilled from the adsorption) by line 19. Its purity is about 80%. Crystals in suspension in a mother liquor are recovered by a line 51 and are separated in a first centrifuge 52. A first mother liquor containing, for example, 40% paraxylene is drawn off and recycled at least in part to adsorption zone 8 by lines 53 and 3 via the clay treatment and distillation zones, the other part being able to be recycled to the first crystallization. The crystals recovered by a line 55 are melted in a melting zone 58 and are introduced by a line 59 into a second crystallization unit 70 operating for example at 0°C. A suspension of second crystals is recovered by a line 71, and is introduced into at least a second centrifuge 72 or a rotary filter. A second mother liquor is recovered, by a line 73, and is recycled at least in part to the first crystallization unit 50 and optionally in part to the second crystallization zone. The separated crystals are washed with the desorption solvent (toluene, for example) used as a washing solvent is introduced into the centrifuge by a line 56, and an added portion 57 coming from line 17 in particular, and a washing liquor 74 is drawn off that is recycled at least in part to the first crystallization unit 50 and/or to the second crystallization unit 70 after optionally having been distilled. It could also be recycled to the unit for distilling the raffinate (step b). Furthermore, from a line 75 that is connected to centrifuge 72, the second crystals that are melted completely in a melting zone 76 are recovered, and melted paraxylene that is distilled in distilling column 60 is collected by line 77. The toluene recovered at the top is recycled by line 56 while the paraxylene of very high purity is drawn off at the bottom of the column by line 61. Centrifuge 72 could be replaced with a countercurrent washing column. In this case, the second mother liquor containing washing toluene can be distilled, as is the case with a single stage before being recycled, and the washing toluene sent back to the washing column. Figure 5 illustrates the use of a countercurrent column, of the NIRO column type, as a second zone for separation and washing of the second crystals, instead of centrifuge 72 of figure 4 or instead of a rotary filter, and which uses as washing solvent not toluene, but a portion of the melted paraxylene stream. According to this figure 5, comprising the same elements as those of figure 4, the second crystals in suspension in the second mother liquor are recovered by a line 71 coining from the second crystallization unit, and it is introduced into NIRO column 80 which is fed with washing solvent by a portion of the melted paraxylene that is collected by a line 77a. Paraxylene crystals, of very high purity that are melted in melting zone 76 are collected by a line 75 and a stream of melted paraxylene is recovered by line 77. The second mother liquor having 70%, for example, paraxylene and the washing liquor are recovered at the same time and are recycled at least in part to the first crystallization unit 50 by a line 73 and optionally in part to the second crystallization unit. According to another variant that is not illustrated by the figures, the washing solvent can be a solvent other than the stream of melted paraxylene and the desorption solvent, for example pentane. In this case, the stream of melted paraxylene is distilled so as to recover, at the top, washing solvent that is recycled at least in part in the second separation zone and, at the bottom, paraxylene of very high purity, the mother liquor comprising the washing liquor is distilled before being recycled to the first crystallization zone and optionally in part to the second crystallization zone if the second separation zone is a countercurrent washing column (a NIRO column, for example). However, if the second separation zone is a centrifuge or a rotary filter, the mother liquor is recycled to the first crystallization zone and optionally in part to the second crystallization zone, and the washing liquor is distilled before being recycled to the first crystallization zone and optionally in part to the second crystallization zone. A recycling of the first crystals in suspension 51a and of the second crystals in suspension 71a can be envisioned, respectively in the first and in the second crystallization zone. Figures 6 and 7 illustrate a two-stage crystallization of the paraxylene, the temperature of the second stage of crystallization of the mother liquor being lower than that of the first stage. According to figure 6, the crystallization charge (the extract distilled from the adsorption) is introduced by line 19 into the first crystallization unit 70 which operates at about 0°C. First crystals in suspension in a first mother liquor are recovered by a line 81, and are separated in at least one first centrifuge 82, washed by toluene brought by a line 97 and recovered by a line 84. The first mother liquor containing, for example, 70% paraxylene is introduced at least in part by a line 83 into the second crystallization unit 50 operating at -10°C. Another part can be recycled in the first crystallization unit by a line 83a. Second crystals in suspension in a second mother liquor are recovered by a line 85, and they are separated in at least one second centrifuge 86. They are collected by a line 88 after having been washed with toluene that has been introduced by a line 98 into the second centrifuge. The second mother liquor collected by line 87 contains a fraction of the washing toluene; it is recycled at least in part to adsorption zone 8 via the clay treatment and distillation zones and optionally in part by a line 87a to the second crystallization unit. The first and second paraxylene crystals are mixed and introduced into a melting zone 89. A line 90 collects the melted paraxylene stream that is introduced into a distilling column 91 which delivers, at the bottom, paraxylene of very high purity and, at the top, toluene that is recycled by a line 92 and that is mixed with an added portion of toluene brought by a line 95 or line 18. The mixture of toluene obtained is introduced, at least in part, into each of centrifuges 82 and 86, as washing solvent. Figure 7 uses the same elements and the same references as figure 6, except that for the step of washing the crystals, very pure melted paraxylene recovered from line 90 is used as washing solvent. Actually, at least a portion of the very pure melted paraxylene is drawn off by a line 91 and introduced into first centrifuge 82 and into second centrifuge 86 to wash the first and second crystals, respectively. The first mother liquor and a first washing liquor are sent by line 83 into the second crystallization unit 50 while the second mother liquor and the second washing liquor are collected by line 87 to be recycled, at least in part, to adsorption zone 8. In this figure, the use of centrifuges 82 and 86 to separate the crystals of the mother liquors and to wash them has been described, but they could also be replaced with countercurrent columns, of the NIRO column type. In this case, the respective solutions collected would gather together the mother liquor and the washing liquor coming from each column. Figure 8 illustrates another variant of the process having several crystallization stages, in which the melted paraxylene of; very high purity is collected at the output of the high-temperature crystallization zone. The crystallization charge (the extract distilled from the adsorption) is introduced by line 19 into the first crystallization unit 70 which operates at about 0°C. Crystals in suspension in a first mother liquor are recovered by a line 81, and are separated for example on a NIRO column 80, the crystals recovered by a line 84 being melted in a melting zone 100. A stream of melted paraxylene of very high purity is collected by a line 101, that is drawn off in part thanks to line 102 to wash the crystals in the NIRO column. The first mother liquor which is drawn off from the NIRO column by line 83 is introduced, at least in part, into a second crystallization unit 50 operating at a temperature of -15°C, for example. Another part of this first mother liquor can be recycled by a line 83a and mixed with the charge of the first crystallization unit. From the second crystallization unit 50, a suspension of second crystals in a second mother liquor is collected by a line 85, that is separated in at least one centrifuge 86 or a rotary filter. A second mother liquor is recovered, by a line 87, that is recycled at least in part to adsorption unit 8 via the clay treatment and distillation zones, a part being able to be recycled also to the second crystallization unit 50 by a line 105 connected to line 87. The second crystals, once separated, are collected by a line 88 and melted optionally in a melting zone 103. The melted paraxylene is recycled by a line 104 and mixed with the charge of the first crystallization unit 70 to be recrystallized at the temperature of the first crystallization. Figure 9 represents a preferred variant of the two-stage crystallization process operating advantageously between +5 and -7°C for the first and between -7 and -25C for the second. The crystallization charge (the extract distilled from the adsorption) is introduced by line 19 into a first crystallization unit 70. First crystals in suspension in a first mother liquor are recovered by a line 81 and are separated in at least one centrifuge 82 or at least one rotary filter. The first mother liquor, collected by line 83, is introduced at least in part into a second crystallization unit 50, another part being able to be recycled to the first crystallization unit 70. A second suspension of crystals is collected by a line 85, that is separated in at least one centrifuge or rotary filter 86. A second mother liquor is drawn off by a line 87 and recycled at least in part to adsorption zone 8 via the clay-treatment and distillation zones, another part being able to be drawn off and recycled to the second crystallization unit by a line 87a connected to line 87. The first and second crystals respectively collected by lines 84 and 88 are gathered together and introduced into at least one washing column 110, of the NIRO column type, where they are washed by a washing solvent. Paraxylene crystals are collected by a line 111, which are completely melted in a melting zone 112 and a stream of paraxylene of very high purity is drawn off. A portion of the paraxylene stream is drawn off by a line 114 and introduced as washing solvent into column 110. The washing liquor collected in the column is recycled at least in part to the first crystallization unit. According to figure 10, when the washing solvent in the washing column is the desorption solvent (toluene) or another suitable solvent such as pentane, the stream of melted paraxylene containing a minor portion of solvent can be distilled in a distillation unit 117. The paraxylene of very high purity is collected by a line 118 while the light fraction comprising the washing solvent is recycled into the NIRO column. Finally, the washing liquor drawn off by line 15 and containing solvent is distilled in a distillation unit 120, the solvent is recycled at least in part in the column and the washing liquor, freed of the major portion of the solvent, is recycled at least in part to the first crystallization unit by line 121. The recycling of the mother liquor coming from a crystallization stage A in said stage A or from a stage B in said stage B has been mentioned for a given figure. Of course, these recyclings can apply for all the figures. Also, it is known that a suspension of crystals coming from a crystallization stage can be recycled to this stage and this recycling can also apply to all the figures (81a and 85a) . The term of a separation zone has often been used in the description. Of course, it involves at least one centrifuge or at least one rotary filter or at least one column for countercurrent washing by a solvent. The separation zone where the washing of the crystals is performed can comprise at least one centrifuge or at least one rotary filter. It has been observed, however, that by using, as separation zone where the washing of the crystals is performed, at least one countercurrent washing column, of the NIRO type for example and in particular, with a portion of the very pure melted paraxylene collected, as washing solvent, excellent results were obtained and the cost of the utilities was reduced. As has been diagrammed in figure 1, the mother liquor coming from crystallization unit 5b is recycled to adsorption unit 8. In the case of a two-stage or multi-stage crystallization, the mother liquor comes from the coldest crystallization stage after the separation of the paraxylene crystals (line 53, figure 5, line 87, figure 7 to 9). The impurities which circulate in the loop of the adsorption, crystallization, isomerization device can be olefinic hydrocarbons, as well as paraffinic and naphthenic hydrocarbons or other oxygenated compounds. They can come in particular, both from the charge to be treated which comes from a catalytic reforming and from the isomerization. These impurities therefore circulate and can be found in all the fractions and particularly in the extract and therefore in the mother liquor resulting from the crystallization step. This mother liquor can be introduced by a line 32 that is connected to line 3 and to line 53 or 87 in at least one clay-treatment reactor 26, advantageously two, placed upstream and connected by a line 27 to adsorption unit 8. Line 1 containing the charge to be treated and line 2 containing the isomerate can be connected to this line-32, the three flows being thus treated in a mixture in a single reactor 26. According to another variant, charge 1 can have been pretreated in another clay-treatment reactor (not indicated in the figure). It is the same for isomerate 2 which can also have been initially pretreated after having passed into distillation unit 23. According to a preferred variant, mother liquor 3 can be introduced directly into line 22 leading to distillation unit 23 of the isomerate, before being treated, in mixture with the distilled isomerate, in clay-treatment reactor 26. This variant makes it possible to eliminate approximately all the most volatile compounds, not only from the isomerate but from the mother liquor. When the distillation unit is adjusted to deliver also, at the bottom, an additional fraction containing most of the heavy compounds (C9+ hydrocarbons, aldehydes, ketones), the clay treatment of the distilled mixture comprising the isomerate and the mother liquor is thereby substantially improved. A portion of the mother liquor can also be recycled by a line 31 to effluent 27 of reactor 26. The effluent of the clay-treatment reactor and optionally the crystallization mother liquor 31 that can further contain heavy hydrocarbons, such as hydrocarbons having nine carbon atoms, are introduced by a line 27 into a distilling column 28 which delivers, at the bottom of the column (line 29), the undesirable impurities and, at the top, a distillate corresponding to the purified C8 fraction, that is introduced by line 4 to adsorption unit 8. A portion of the mother liquor can also be introduced into line 4 by a line 30. These various recyclings can be combined with one another, when it involves, for example, reusing existing pieces of equipment for distillation 23, clay treatment 26 or distillation 28 and when one of these pieces of equipment is already operated at its maximum flow rate or else when it is desired to have the amount of an impurity in the loop lowered without seeking to eliminate it completely. In other words, the mother liquor of the crystallization unit (the coldest stage), conveyed by line 3, can be partially recycled to adsorption unit 8 either directly by means of line 30, or indirectly by means of lines 31, 32 or 33. So as to keep the amount of constituents with intermediate volatility of the toluene (desorption solvent) at a tolerable level, for example less than 5%, at least one purge of toluene polluted by said constituents is performed by means of a line 35 connected either to line 17, or to line 14 or to line 11 collecting all the solvent recycled to adsorption unit 8. In addition, it is possible to perform a purge of the mother liquor coming from the crystallization if the amount of constituents with intermediate volatility is too great there. This purge is performed by means of line 34 connected to line 3. The purge of toluene can be compensated for by an added portion of toluene. Since the greatest sources of Cg-aromatic fraction (line la) come from the catalytic reforming, from dismutation (disproportionation) of the toluene into benzene and • xylene and from the toluene - C8-aromatic transalkylation and since the effluents of these units from which they come are in part generally purified in a series of distillation units of which column 28 can be part, it is possible to use, at least in part, as a source of added portion of toluene, either the one produced at the top (line 42) of a distilling column 40 of toluene, before reactor 26 containing the clay, or the one which results from the bypass by a line lb of at least a portion of the charge (line 1) that is mixed with the effluent from the bottom of column 40, or the one which is introduced into the purified charge (line 1) by putting column 40 out of adjustment, which makes it possible to allow the desired proportion of toluene pass into the C8 fraction. WE CLAIM: 1. A process for the production of paraxylene of high purity from a charge containing a mixture of aromatic hydrocarbons having 7 to 9 carbon atoms, comprising circulating at least a portion of the charge in an enrichment zone to produce a first fraction with paraxylene, purifying at least a portion of said first fraction in a purification zone by at least one crystallization in at least one crystallization zone, said crystallization zone comprising at least two crystallization stages at a temperature between +50 and -22°F, and recovering paraxylene crystals from each crystallization stage. 2. The process according to claim 1, wherein the enrichment zone is at least one crystallization zone at a temperature lower than that of said crystallization stages, said process comprising introducing the charge, to said enrichment zone, producing a liquid and crystals, isomerizing said liquid in an isomerization zone and melting said crystals to form at least a portion of said first fraction. 3. The process according to claim 1, wherein the enrichment zone is a selective adsorption zone containing a zeolitic adsorbent, said process comprising introducing the charge, performing selective adsorption of the charge in the presence of a desorption solvent, recovering a paraxylene enriched first fraction and a paraxylene depleted second fraction, isomerizing said second fraction in an isomerization zone containing an isomerization catalyst under suitable conditions, to produce an isomerate containing paraxylene, and recycling the isomerate, at least in part, to the adsorption zone. 4. The process according to claim 1, wherein the enrichment zone is at least one zone of disproportionation of a charge consisting essentially of toluene, said process comprising producing in said disproportionation zone an effluent containing benzene and xylenes, and distilling said effluent to remove beazene and unreacted toluene to produce the first fraction with parax. 5. The process according to claim 1, comprising performing in the purification zone a first crystallization at a temperature Tl and a second csystallization at a temperature T2, higher than T1. 6. The process according to claim 5, comprising recycling at least a portion of mother liquor resulting from the coldest crystallization stage of the purification zone to the enrichment zone. 7. The process according to claim 1, comprising performing a first crystallization of the paraxylene-enriched fraction in a first crystallization zone at a temperature Tl, recovering a suspension of first paraxylene crystals in a first mother liquor, separating the first crystals from the first mother liquor in a first separation zone, recovering a first mother liquor, recycling separated liquior to the enrichment zone, melting separated first crystals completely and crystallizing in a second crystallization zone at a temperature T2 that is higher than Tl, recovering a suspension of second paraxylene crystals in a second mother liquor, separating the second crystals from the second mother liquor in a second separation zone, washing the second crystals with a washing solvent in the second separation zone, recovering a washing liquor, recycling at least part of the second mother liquor, and at least a porticxi of the washing liquor to the first crystallization stage and optionally in part to the second crystallization zone and melting the second paraxylene crystals completely so as to obtain a liquid stream of melted paraxylene. 8. The process according to claim 7, comprising recycling the washing liquor, in part, to the second crystallization zone. 9. The process according to claim 7, wherein the content of paraxylene resulting from the enrichment zone is at least 50% by weight 10. The process according to claim 1, comprising performing a first crystallization of the paraxylene-enriched fraction in a first crystallization zone at a temperature Tl, recovering a suspension of first paraxylene crystals in a first mother liquor, separating the first crystals from the first mother liquor in a first separation zone, ooptionally washing the first crystals with a washing solvent in the first separation zone, crystallizing at least a portion of the first mother liquor in a second crystallization zone at a temperature T2 that is lower than temperature Tl, recovering a suspension of second paraxylene crystals in a second mother liquor, separating the second crystals from the second mother liquor in a second separation zone, washing the second crystals with the washing solvent in the second separation zone, recovering a second mother liquor, mixing the first and second paraxylene crystals, completely melting said crystals and recovering a stream of melted paraxylene. 11. The process according to claim 10, comprising washing the first crystals with a washing solvent in the first separation zone. 12. The process according to claim 10, wherein the content of paraxylene resulting from the enrichment zone is at least 50% by weight. 13. The process as claimed in claim 1, wherein performing a first crystallization of a paraxylene-enriched fraction, having a paraxylene content of at least 50% by weight, and of optionally melted recycled crystals coming from a second crystallization in a first high temperature crystallization zone at a temperature Tl, recovering a suspension of paraxylene crystals in a first mother liquor, separating the crystals from the first mother liquor in a first separation zone, washing said crystals, melting said crystals and recovering a stream of melted paraxylene, crystallizing at least a portion of the first mother liquor in a second high temperature crystallization zone at a temperature T2 that is lower than temperature Tl, recovering a suspension of second paraxylene crystals in a second mother liquor, separating the second crystals from the second mother liquor in a second separation zone, recovering a second mother hquor, and second crystals, optionally melting a portion of the second crystals and recycling the optionally melted second melted crystals to the first crystallization zone and recrystallizing the melted crystals with the paraxylene-enriched fraction at a temperature Tl. 14. The process according to claim 13, wherein melting the second crystals, recycling and recrystallizing said crystals with the paraxylene-enriched fraction at temperature T1. 15. The process according to claim 1, wherein performing a first crystallization of the paraxylene-enriched fraction and of partially melted recycled crystals coming from a second crystallization in a first crystallization zone at a temperature Tl, recovering a suspension, of paraxylene crystals in a first mother liquor, separating the crystals from the first mother liquor in a first separation zone, washing said crystals in a centrifuge or a countercurrent column, melting said crystals and recovering a stream of melted paraxylene. crystallizing at least a portion of the first mother liquor in a second crystallization zone at a temperature T2 that is lower than temperature Tl, recovering a suspension of second paraxylene crystals in a second mother liquor, separating the second crystals from the second mother liquor in a second separation zone, recovering a second mother liquor, partially melting the second crystals and recycling the crystals in a slurry to the first crystallization zone, and recrystallizing said slurry with the paraxylene-enriched fraction at temperature Tl. 16. The process according to claim 1, wherein performing a first crystallization of the paraxylene-enriched fraction in a first crystallization zone at a temperature Tl, recovering a suspension of first paraxylene crystals in a first mother liquor, • separating the first crystals from the first mother liquor in a first separation zone, crystallizing at least a portion of the fu-st mother liquor in a second crystallization zone at a temperature T2 that is lower than Tl, separating the second crystals from the second mother liquor is a second separation zone, recovering the second mother liquor, recovering the first crystals and the second crystals and washing in at least one separation and washing zone with a washing solvent, recycling a washing liquor at least in part to the first crystallization zone; recovering paraxylene crystals and completely melting said crystals in a melting zone and collecting a stream of melted paraxylene. 17. The process according to claim 16, wherein the first and second crystals are washed in a separation and countercurrent washing zone subsequent to recovery. 18. The process according to claim 1, wherein the content of paraxylene resulting from the enrichment zone is at least 50% by weight, and the temperature Tl of one of the crystallization stages is different than the temperature T2 of another crystallization stage. 19. The process according to claim 18, wherein the crystallization temperature is between -10 °C and -25"C. 20. The process according to claim I, wherein the crystallization zone comprising a first and second crystallization stage, said process comprising recovaing first crystals from said first crystallization stage, and washing said crystals in at least one countercurrent washing zone. 21. The process according to claim 20, comprising washing said crystals with a washing solvent which is melted paraxylene from said crystallization zone. 22. The process according to claim 20, con:q)rising washing said crystals with a washing solvent which is toluene. 23. The process according to claim 22, wherein the toluene is used as a desorption solvent in a selective adsorption process in the enrichment zone. 24. The process according to claim 20, comprising washing said crystals with a washing solvent which is pentane. 25. The process according to claim 1, said crystallization zone comprising a first and second crystallization stage, said process comprising recovering second crystals from said second crystallization stage, and washing said crystals in at least one countercurrent washing zone. 26. The process according to claim 1, said crystallization zone comprising a first and second crystallization stage, said process comprising recovering first and second crystals from said first and second crystallization stages, respectively, and washing said crystals in at least one countercurrent washing zone. 27. The process according to claim 26, wherein said first and second crystals are combined and sent to said countercurrent washing zone. 28. The process according to claim 13, wherein T2 is +10 to -30C. 29. The process according to claim 13, wherein Tl and T2 are +10 to -30°C. 30. A process for the production of high purity paraxylene substantially as herein described with reference to the accompanying drawings.

Full Text

The invention relates to a process for separating and preparing paraxylene from a mixture of aromatic hydrocarbons comprising xylene isomers.
The xylene isomers are orthoxylene, metaxylene, paraxylene and ethylbenzene. The main application of the invention is in obtaining paraxylene to a degree of purity that is sufficient for the synthesis, for example, of terephthalic acid, used in the preparation of synthetic fibers and particularly polyester.
The applicant has described in a patent FR 2,681,066 (US 5,284,992), which is incorporated as a reference, a process for separating and recovering paraxylene contained in a charge of hydrocarbons comprising essentially aromatic hydrocarbons having 8 carbon atoms.
This process comprises the combination of an enrichment step, which is a selective adsorption on an adsorbent in a simulated moving bed, of a charge containing essentially the xylene isomers, which makes it possible to substantially enrich a first adsorption effluent with paraxylene, and of a purification, which is a crystallization, in at least one crystallization unit operating at high temperature, of the paraxylene-enriched effluent so as to obtain paraxylene having a very high purity, the mother liquor being recycled to the adsorption step.
This high-temperature crystallization corresponds to the
second crystallization step of the conventional crystallization
processes (Chevron ; Arco) which generally comprise a first crystallization at low temperature (-40 to -70°C) and a second

crystallization to purify, at high temperature (0 to -20°C, for example), crystals obtained that were previously remelted.
Furthermore, a second fraction depleted of paraxylene and therefore enriched with ortho- and meta-xylene as well as ethylbenzene, delivered by the selective adsorption unit, is sent into an isomerization unit to increase its concentration of paraxylene to a value close to equilibrium and approximately close to or greater than the composition of the initial charge of hydrocarbons, and the isomerate obtained can then be recycled to the adsorption.
In the adsorption, crystallization and isomerization sequence described, various types of impurities can appear in the various effluents and cause disturbances in the operation of the units/ which are detrimental to the yield obtained and to the purity of the paraxylene recovered.
First of all, during isomerization of the paraxylene-depleted fraction, olefinic hydrocarbons can be produced in a variable amount depending on the values of the partial pressures of hydrogen introduced. The subsequent formation of polymers and their passage into the adsorption unit can cause serious problems of circulation through the adsorbent, even deactivate it.
In addition, paraffinic and naphthenic hydrocarbons having 8 and 9 carbon atoms, whose volatility is between that of toluene, a desorption solvent for example, and that of the xylenes, are intermediate products of the conversion of ethylbenzene into xylenes during the isomerization and their accumulation can prove to be harmful.

Furthermore, aromatic hydrocarbons having 9 carbon atoms, present in low proportion and poorly separated in distillation columns, can be detrimental to the process, such as aldehydes and ketones that are heavier than the initial charge, which are formed when oxygen is accidentally dissolved.
Finally, another problem is linked to the presence of methanol. This alcohol is sometimes added in low proportion in mixtures of xylenes to be crystallized to prevent the cocrystallization of water and paraxylene.
Actually, the dry Cg-aromatic mixtures are relatively hygroscopic and when the suspension of paraxylene crystals in the mother liquor passes into the centrifuges, water contained in the ambient air can be absorbed into the mother liquor and this water can possibly crystallize in conjunction with the temperature of this mother liquor.
In addition, some exchangers can have leaks and some water can accidentally pass into the mixture to be crystallized.
An object of the invention is to improve the recovery of the paraxylene produced and to minimize the energy cost, particularly of the purification step.
Another object of the invention is to eliminate these drawbacks and to limit in particular how much of these various impurities the adsorption section contains to seek to optimize it, to the extent that the adsorbent is very sensitive to the impurities of the charge of the adsorption zone.
This invention relates to a process for producing paraxylene of very high quality from a charge containing a mixture of

aromatic hydrocarbons having 7 to 9 carbon atoms in which at least a portion of the charge is made to drculate in a so-called enrichment zone suited to enrich a first fraction of paraxylene and at least a portion of said first
fraction is purified in a so-called purification zone by at least
one high-temperature crystallization in at least one
crystallization zone, the process being characterized in that
said first paraxylene-enriched fraction is crystallized in a
purification zone comprising at least two crystallization stages
at high temperature, and advantageously between +10 and -ZS^C.
By high-temperature crystallization of the paraxylene is
meant a crystallization of a solution or suspension of paraxylene
that is already enriched with paraxylene, which corresponds to
what the literature calls a purification step. For example, the
patent US 2,866,833, incorporated as a reference, mentions a step
for purifying paraxylene at -34°C.
Earch crystallization stage can comprise one or more crystallizes. According to a first variant, the enrichment zone of the
first fraction having at least 30% weight of paraxylene can be at least one very low-temperature crystallization zone, for example lower than -40°C, known as a recovery section, in which a charge containing a mixture of aromatic hydrocarbons having 8 carbon atoms is introduced, such as the one described according to the patent US 2,866,833 or such as the ones described according to
patent US 5,329,061, incorporated as references. This enrichment
zone delivers a suspension of crystals which is separated in a
separation zone and the recovered crystals are melted and
constitute at least a portion of said first fraction to be
purified later on. In addition, a mother liquor resulting from
the separation can be isomerized in an isomerization zone and the

isomerate recycled at least in part to the enrichment zone (recovery section).
According to a second variant, the paraxylene enrichment zone can be a selective adsorption zone of the charge containing a mixture of aromatic hydrocarbons having 8 carbon atoms delivering theparaxyleneenriched fraction.
According to a third variant the paraxylene enrichment zone can be a disproportionation zone of a charge consisting essentially in toluene and using a coke-selectivated catalyst or a silicon-selectivated catalyst according to the patents US-4.117.026,4.097.543,4.851.604,5.173.461, 5.243.117 and U&-5.321.183 incorporated by reference.
The unreacted toluene and the benzene are avantageously removed by distillation from the disproportionation effluent comprising the xylenes.
It is advantageous to have at the output of the enrichment zone, i.e., for example of the selective adsorption zone as described in the patent US
5,284,992 of the applicant, an effluent containing more than 50%
by weight of paraxylene and preferably 75 to 98%.
Another alternative for producing paraxylene may result from the combination of an adsorption, an isomerization, and a :rystallization step in a single stage at high temperature.
According to a variant of the invention, the process comprises, in combination, an adsorption operation and a crystallization operation. According to this variant, at least a portion of the charge and/or of the products resulting from the crystallization, for example the mother liquor, undergoes a clay treatment operation. At least a portion of the effluent resulting from the clay treatment operation is recycled to undergo an adsorption operation.
This invention also applies to a process comprising, in combination, besides the operations of adsorption and crystallization, an isomerization step. In this case, at least a portion of the isomerate can be clay treated.

This invention relates furthermore to a process for separating and recovering paraxylene from a charge that can contain metaxylene, this process comprising, in combination, an adsorption operation and a crystallization operation. According to this process, at least a portion of the mother liquor coming from the crystallization operation is purified by distillation before being recycled to the adsorption operation.
This invention also relates to a process for separating and recovering paraxylene contained in a charge of hydrocarbons comprising Cg-aromatic hydrocarbons, a process in which in particular:
• in at least one adsorption zone, said charge containing at least metaxylene, paraxylene is put in contact with at least one adsorbent in the presence of at least one suitable desorption solvent under adsorption conditions such that there is obtained a first fraction containing solvent, metaxylene and optionally ethylbenzene and/or orthoxylene and a second fraction containing solvent of the substantially enriched paraxylene;
• the first fraction is distilled to recover a mixture of metaxylene and optionally ethylbenzene, and/or orthoxylene;
• said mixture is isomerized at least in part under suitable conditions in at least one isomerization zone and an isomerate is recovered that is recycled at least partially to the adsorption zone;
• said second fraction is distilled to obtain substantially enriched paraxylene and a crystallization of the

substantially enriched paraxylene is performed obtaining, on the one hand, a mother liquor that is at least partially recycled to the adsorption step and, on the other hand, paraxylene crystals.
According to another variant embodiment of the process according to the invention, it is possible to have at least a portion selected from the charge at least in part, the isomerate at least in part and the mother liquor at least in part circulate in at least one clay, or equivalent material, treatment zone and a first effluent is recovered that is introduced at least in part into the adsorption zone to produce said first and second fractions that are drawn off from the adsorption zone.
More specifically, the invention relates to a process for separating and recovering paraxylene contained in a charge of hydrocarbons comprising Cg-aromatic hydrocarbons, the process comprising the following steps:
a) in an adsorption zone, said charge containing metaxylene, paraxylene and optionally ethylbenzene and/or orthoxylene is put in contact with an adsorbent in the presence of a suitable desorption solvent under adsorption conditions such that a first fraction containing solvent, metaxylene and optionally ethylbenzene and/or orthoxylene and a second fraction containing solvent and substantially enriched paraxylene are obtained;
b) the first fraction is distilled to separate the solvent on the one hand, and the mixture of metaxylene and optionally ethylbenzene, and/or orthoxylene, on the other hand;

c) said mixture is isomerized under suitable conditions in an isomerization zone and an isomerate is recovered that is recycled at least in part to step a);
d) the second fraction is distilled and the solvent on the one hand, and substantially enriched paraxylene, are recovered;
e) a crystallization of the paraxylene of step d) is performed in at least one crystallization zone at high temperature, advantageously between +10°C and -25°C and there is obtained, by separation, on the one hand, a mother liquor that is recycled at least in part to step a) and, on the other hand, paraxylene crystals saturated with mother liquor;
f) the paraxylene crystals are washed with a suitable washing solvent in a washing zone and paraxylene crystals having a very high degree of purity are recovered;
According to another variant of the invention, it is possible to have at least a portion selected from the charge, the isomerate and the mother liquor circulate in at least one clay treatment zone and a first effluent is recovered that is introduced into the adsorption zone to produce said first and second fractions of step (a).
At least a portion of the charge of hydrocarbons can be pretreated in a clay-treatment reactor. It can be advantageous to put the isomerate in a clay-treatment reactor before being sent into the adsorption. These reactors can be independent or form only a single reactor, optionally common with the one that treats the mother liquor.

These clay treatments make it possible to eliminate at least in part the olefins created in particular in the isomerization step and at least a portion of the heavy impurities, which circulate in the adsorption, crystallization and isomerization loop.
Various variants can be envisioned:
The mother liquor can be advantageously introduced at least in part into a distillation column downstream from the isomerization zone. This column also treats the effluent of the isomerization zone and delivers a top fraction containing light compounds (air, water, methanol, C^-) and another fraction containing a distilled mixture of mother liquor and isomerate that is then introduced into the clay treatment zone.
A distillation bottom fraction containing heavy compounds can also be drawn off from this distillation column, which makes it possible to reduce the size of the downstream equipment.
A portion of the mother liquor can also be mixed with the effluent, whatever it is, leaving the clay treatment zone, whether this is the effluent resulting from the circulation of the isomerate, the mother liquor and the charge in the clay treatment zone, or the effluent resulting from the circulation, in the clay treatment zone, of the latter and of the distillation fraction containing said distilled mixture of mother liquor and isomerate, before being introduced into the selective adsorption zone.
The resulting effluent of the latter variants can be distilled in at least one distilling column (a so-called rerun

column) that delivers a bottom fraction containing heavy compounds and a top fraction that is introduced into the adsorption zone optionally with a portion of the mother liquor.
The conditions for adsorbing or eliminating the undesirable compounds on the clay are, as a general rule, the following:
• Temperature: 100 to 300°C, preferably 160 to 230'C
• Hourly space velocity: 1 to 8, preferably l to 4 (Hourly volume of charge per volume of clay)
• Type of clay: activated natural aluminosilicates, for example the clay referenced F54 with ENGELHARD.
• Pressure: 3 to 100 bar, preferably 4 to 20 bar.
The distillation column, depending on the isomerization,
generally has the following characteristics:
• Pressure: 1 to 20 bar, preferably 3 to 8 bar
• Base temperature: 150 to 280C, preferably 200 to 240°C
• Number of plates: 30 to 80, preferably 50 to 70.
The distilling column, known as rerun, located between the clay treatment zone and the selective adsorption zone usually has the following characteristics:
• Pressure: 1 to 20 bar, preferably 3 to 8 bar
• Base temperature: 160 to 290°C, preferably 210 to 250C
• Number of plates: 40 to 200, most often 50 to 90. According to another characteristic of the invention, it is
possible to keep the amount of constituents with intermediate volatility at a tolerable level. In this case, at least a portion of the mother liquor can be purged before being introduced into the clay treatment zone.

It can also be advantageous to purge at least in part the desorption solvent resulting from distillation steps (b) and (d) • of the depleted fraction or of the paraxylene-enriched fraction before it is recycled and to compensate for the purge of the solvent by an addition of fresh solvent, either into the charge or upstream from the adsorption zone.
As has been indicated, it is possible to recycle the crystallization mother liquor in different places of the installation depending on the magnitude of the amount of undesirable compounds, but it can be advantageous to combine these different recyclings with one another, for example, when it involves reusing existing pieces of equipment for the distillation of the isomerate, the clay treatment or the so-called rerun distillation and when one of these pieces of equipment is already operated at its maximum flow rate.
It is also possible to combine these different recyclings and these purges when it is desired to have the amount of an impurity in the loop reduced without seeking to eliminate it altogether.
The crystallization step of the paraxylene-enriched fraction is generally performed, as has been mentioned above, at high temperature, for example between +10 and -30°C and preferably +10 and -25°C. The temperature is usually selected as a function of the concentration of paraxylene that it is desired to have in the mother liquor, and of the economic cost of the crystallization operation.

It is possible under these conditions to perform a crystallization of the paraxylene in a single stage when the paraxylene that is collected, for example as an extract of the adsorption unit, has a purity greater, for example, than 85%.
But it can be advantageous, particularly for economic reasons, to perform a crystallization in several stages, for example a first crystallization at a temperature Tl between +10 and -10C, and a second crystallization at a temperature T2, lower than Tl, between 0 and -25°C.
According to a first embodiment of the invention, a crystallization of the paraxylene of step (d) is performed in a single stage, a suspension of crystals in the mother liquor is recovered, the crystals are separated from the mother liquor in a separation zone, the crystals obtained are washed with the washing solvent, a washing liquor is recovered, at least a portion of the mother liquor and at least a portion of the washing liquor are recycled and the paraxylene crystals are melted completely so as to obtain a liquid stream of melted paraxylene.
According to a second embodiment that uses a first variant of a two-stage crystallization of the paraxylene-enriched fraction, a first crystallization of the paraxylene of step (d) is performed in a first crystallization zone at a temperature Tl, a suspension of first paraxylene crystals in a first mother liquor is recovered, the first crystals are separated from the

zone or to the very low temperature crystallization zone, the separated first crystals are melted and they are crystallized in a second crystallization zone at a
temperature T2 that is higher than Tl, a suspension of second paraxylene crystals in a second mother liquor is recovered, the second crystals are separated from the second mother liquor in a second separation zone, the second crystals are washed with the suitable washing solvent in the second separation zone, a washing liquor is recovered, the second mother liquor, at least in part, and at least a portion of the washing liquor are recycled to the first crystallization zone and optionally in part to the second crystallization zone and the second paraxylene crystals are melted completely so as to obtain a liquid stream of melted paraxylene.
For example, temperature Tl of the first crystallization can be -5 to -25°C while temperature T2 of the second crystallization can be +10 to -5°C.
According to another embodiment of the invention, using a second variant of a two-stage crystallization, a first crystallization of the paraxylene of step (d) is performed in a first crystallization zone at a temperature Tl, a suspension of first paraxylene crystals in a first mother liquor is recovered, the first crystals are separated from the first mother liquor in a first separation zone, optionally the first crystals are washed with the washing solvent in the first separation zone, at least a portion of the first mother liquor is crystallized in a second crystallization zone at a temperature T2 that is lower than temperature Tl, a suspension of second paraxylene crystals in a

second mother liquor is recovered, the second crystals are separated from the second mother liquor in a second separation zone, the second crystals are washed with the washing solvent in the second separation zone, a second mother liquor is recovered
that is recycled at least in part to the adsorption zone or to the very low temperature crystallization zone, the first and second paraxylene crystals are mixed, they are melted completely and a stream of melted paraxylene is recovered.
For example, the first crystallization can be performed at a temperature Tl between +10 and -10°C while the second T2, which is lower than Tl, can be performed between 0 and -25*0.
According to another embodiment of the invention comprising a crystallization having several stages, a first crystallization of the paraxylene of stage (d) and of recycled partially melted or possibly melted crystals
coming from a second crystallization afterward is performed in a first crystallization zone at a temperature Tl, a suspension of paraxylene crystals in a first mother liquor is recovered, the crystals are separated from the first mother liquor in a first separation zone, said crystals are washed, they are melted and a stream of melted paraxylene is recovered, at least a portion of the first mother liquor is crystallized in a second crystallization zone at a temperature T2 that is lower than temperature Tl, a suspension of second paraxylene crystals in a second mother liquor is recovered, the second crystals are separated from the second mother liquor in a second separation zone, a second mother liquor is recovered that is recycled at
least in part to the adsorption zone, or to the very low crystallization zone, optionally the second crystals are melted and the optionally melted crystals are

recycled to the first crystallization zone to recrystallize them
with the paraxylene of step (d) at temperature Tl. Another variant can compnse a partial melting of the second crystals and a recycling of the obtained slurry to the first crystallization zone to recrystallize it with the paraxylene of step (d) at temperature Tl.
According to another particularly advantageous embodiment of
the invention, a first crystallization of the paraxylene of step
(d) is performed in a first crystallization zone at a temperature
Tl, a suspension of first paraxylene crystals in a first mother
liquor is recovered, the first crystals are separated from the
first mother liquor in a first separation zone, at least a
portion of the first mother liquor is crystallized in a second
crystallization zone at a temperature T2 that is lower than Tl,
the second crystals are separated from the second mother liquor
in a second separation zone, the second mother liquor is
_recpvered. .that is recycled at least in part to the adsorption
zone or to the very low temperature crystallization zone, the first crystals and the second crystals are recovered and they are washed in at least one separation and countercurrent washing zone with the suitable washing solvents, a washing liquor
which is recycled at least in part to the first crystallization zone is recovered on the one hand, paraxylene crystals are recovered on the other hand, they are melted completely in a melting zone and a stream of melted paraxylene is collected.
The invention also relates to a process for separating and recovering paraxylene contained in a charge of hydrocarbons comprising Cg-aromatic hydrocarbons, the process comprising the following steps:
a) in at least one adsorption zone (8) , said charge (1) containing metaxylene, paraxylene and optionally ethylbenzene and/or orthoxylene is put in contact with an

adsorbent in the presence of a suitable desorption solvent
under adsorption conditions such that there is obtained a
first fraction containing solvent, metaxylene and optionally
ethylbenzene and/or orthoxylene and a second fraction
containing solvent and essentially substantially enriched
paraxylene;
the first fraction is distilled (12) to separate the solvent
on the one hand, and the mixture of metaxylene and
optionally ethylbenzene, and/or orthoxylene, on the other
hand;
said mixture is isomerized under suitable conditions in an
isomerization zone (21) and an isomerate (2) is recovered
that is recycled at least in part to step a);
the second fraction is distilled (16) and the solvent on the
one hand, and substantially enriched paraxylene, are
recovered;
a crystallization of the paraxylene of step d) is performed
in at least one crystallization zone (5a, 5b) at high
temperature, advantageously between +10°C and -25'C and
there is obtained, by separation, on the one hand, a mother
liquor that is recycled (3) at least in part to step a) and,
on the other hand, paraxylene crystals saturated with mother
liquor;
the paraxylene crystals are washed with a suitable washing
solvent in at least one washing zone and paraxylene crystals having a very high degree of purity are recovered ;

the process being characterized in that at least a portion of the mother hquor (3) (33) is introduced into a distillation column, a fraction containing purified mother liquor is obtained, a fraction which is then sent into adsorption zone (8).
Of course, one will not go outside the scope of this invention by using a desorption solvent other than toluene such as in particular paradiethylbenzene (PDEB), this solvent, being heavier than the xylenes, will be recovered at the bottom of certain columns while the toluene was recovered at the top.
Accordingly, the present invention provides a process for the production of paraxylene of high purity from a charge containing a mixture of aromatic hydrocarbons having 7 to 9 carbon atoms, comprising circulating at least a portion of the charge in an enrichment zone to produce a first fraction with paraxylene, purifying at least a portion of said first fraction in a purification zone by at least one crystallization in at least one crystallization zone, said crystallization zone comprising at least two crystallization stages at a temperature between +50 and -22°F, and recovering paraxylene crystals from each crystallization stage.
Our co-pending application no.l741/MAS/95 provides a process for separating and recovering paraxylene from a charge optionally containing metaxylene.
Our other co-pending application no.l726/MAS/95 provides a process for the production of paraxylene.

The invention will be better understood in view of the
following figures that illustrate in a nonlimiting way, several
with reference to the accompanying drawing, m
embodiments of the invention, / which:
• figure 1 diagrammatically represents the process and the various possibilities for recycling the isomerate and the crystallization mother liquor to the adsorption via a clay treatment.
• figures 2 and 3 illustrate a purification of paraxylene by crystallization in a single stage.
• figures 4 and 5 show a purification of paraxylene by crystallization in a double stage, the first being colder than the second.
• figures 6 to 10 represent a purification of paraxylene by crystallization in a double stage, the first being hotter than the second.
The operating conditions and the adsorption in simulated
moving bed (countercurrent, for example) are selected so that the
first fraction containing metaxylene, orthoxylene and . .

ethylbenzene is a raffinate and the second fraction containing essentially paraxylene is an extract. These conditions are described in the patent US 5,284,992.
By a line l, a charge is conveyed that comprises about 20% ethylbenzene, 18% paraxylene, 45% metaxylene and 17% orthoxylene. Joined to it by a line 2 is a recycled effluent whose ethylbenzene content is appreciably lower, typically 8 to 13%, and which contains impurities. By lines 3 and 30, another recycled effluent is introduced whose paraxylene content is greater, typically 25 to 45%. A line 4 recovers the charge and these two effluents, it conveys a mixture of approximate composition, paraxylene 20 to 22.5, ethylbenzene 9 to 14%, orthoxylene 20 to 22.5%, metaxylene 45 to 50%, which is introduced into a simulated countercurrent adsorption zone 8 comprising one or more columns 6 and/or 7 filled with a zeolitic adsorbent, each of the columns being divided into a limited number of beds, the number of the beds of each column being able to be between 4 and 20, the productivity, expressed in relation to the paraxylene produced, being about 0.07 m3 per m3 of sieve and per hour expressed at ambient conditions. Desorbing is by toluene, at a rate of about 1.45 m3 of toluene per m3 of charge, the operating temperature being approximately 160°C. Drawn off from this unit by a line 10 is a paraxylene-depleted raffinate containing essentially toluene, metaxylene, ethylbenzene and orthoxylene and, by a line 9, an extract of paraxylene-enriched composition containing essentially toluene and paraxylene, the major impurity being ethylbenzene. The raffinate is introduced

into a distilling column 12 (top temperature 125°C, bottom
temperature 160'C, for example) . Drawn off at the top by a line
into the adsorptinr). 14 is toluene (about 30% of the amount introduced/ for example)
containing for example less than 2% of C8-aromatic compounds and,
drawn off at the bottom of this column by a line 15, is a liquid
(raffinate freed of solvent) rich in ethylbenzene, metaxylene and
orthoxylene and depleted of paraxylene (less than 3%, for
example) that is sent into an isomerization unit 21. This
raffinate is put in contact with hydrogen introduced by a line 20
and with a catalyst having a base of mordenite and platinum on
aluminum at about 380C. A line 22 conducts the isomerate from
the outlet of the reactor to a flask for separating the gaseous
constituents (not shown in the figure) , then to a distilling
column 23 (top temperature 90°C, bottom temperature 160°C, for
example). Drawn off at the top by a line 24 are C1 to C5 hydrocarbons,
hexane, cyclohexane, benzene and toluene and at the bottom of
this column by a line 2, an effluent containing 8 to 13%
ethylbenzene, 21 to 24% paraxylene, 21 to 24% orthoxylene, 45 to
50% metaxylene and impurities, which is recycled to adsorption
zone 8.
Line 9 introduces the extract into a distilling column 16
from which toluene having less than 2% Cg-aromatic compounds
into the adsorption, (about 70% of the amount introduced, for example) is drawn off at
the top and is recycled by lines 17 and 11 to the feed of desorption
solvent of the adsorption unit. At the bottom of column 16 at
about 160°C, a stream enriched with paraxylene (at about 90%
paraxylene) is drawn off by means of a line 19 which conducts it

into a one-stage crystallization unit 5a for example operating at about -10'C. In this unit 5a, 5b paraxylene crystals are produced which are in suspension in a mother liquor. The crystals are separated in at least one centrifuge 5b for example and washed in the centrifuge. On the one hand, a paraxylene-depleted (about 54%) mother liquor is collected which is recycled by line 3 to adsorption zone 8 via clay-treatment and distillation zones discussed below and, on the other hand, paraxylene crystals, that are melted, are collected. The washing solvent, toluene for example, is brought by a line 18 and can, as shown in the figure, come from the distillation unit of raffinate 12 and/or from the unit for distillation of extract 16. There is recovered from unit 5b, after a distillation of the melted crystals not shown, liquid paraxylene with a purity for example equal to 99.75% by a line 25 and toluene that is recycled (line not shown) . Figure 2 illustrates more precisely the steps of crystallization and of downstream treatment of the paraxylene crystals with a washing with toluene. According to this figure, crystallization unit 50 in a single stage receives the crystallization charge (the distilled extract) by line 19. Crystals in suspension in a mother liquor are recovered by a line 51 and are separated at least in part in at least one centrifuge 52. A mother liquor containing for example 54% paraxylene is drawn off and recycled at least in part to adsorption zone 8 by lines 53 and 3, another part being able to be recycled to crystallization zone 50 by a line 53a. A portion of the crystals

in suspension in the mother liquor can also be recycled in the crystallization zone by a line 51a.
Then, recycled toluene coming from a distillation column 60 brought by a line 56, and toluene brought by a line 57 of fresh solvent coming from line 18 are introduced into centrifuge 52 as washing solvent. A washing liquor is collected separately by a line 54 that is connected to centrifuge 52, and it is recycled at least in part in the unit for distilling raffinate 12.
The washed crystals of paraxylene are drawn off by a line 55, completely melted in a melting zone 58 and introduced into distillation column 60 by a line 59. At the bottom of the column, liquid paraxylene of very high purity is recovered, and at the top of the column, toluene is recovered which is recycled at least in part into centrifuge 52. At least one centrifuge was used to separate the crystals and the mother liquor. Also, at least one rotary filter could have been used instead of the centrifuge.
According to a variant that is not shown, the centrifuge can be replaced by at least one column for separating and
countercurrent washing, cited in the patents US 4 475 355, US 4 481 169, the NIRO column for example, incorporated as references. In this case, the mother liquor and the washing liquor are one and the same liquor which is optionally distilled before being recycled, at least in part, to the adsorption zone, via the clay treatment and distillation zones, and optionally in part in the crystallization zone.
According to another variant illustrated by figure 3, it is possible to use another washing solvent such as the melted

paraxyiene coming from melting zone 58. In this case of a figure having the same references for the same elements as those of figure 1, at least a portion of the melted paraxyiene is introduced countercurrent of suspension 51, by a line 59b, into a countercurrent column 80, a NIRO-type column for example, and is used to wash the paraxyiene crystals in the column. At least a portion of the melted paraxyiene that is introduced into the column crystallizes there.
The crystals recovered from the column by line 55 are then melted in melting zone 58 and the liquid paraxyiene of very high purity is recovered by line 59.
The washing liquor and the mother liquor are recovered at the same time by line 53 and are recycled to adsorption zone 8, a portion being able to be recycled to crystallization zone 50.
If a washing solvent, for example pentane, other than the desorption solvent (toluene) and melted paraxyiene, were used, the process described according to figure 2 would be reproduced, except that the washing liquor coming from centrifuge 52 would have to be freed of solvent by a subsequent distillation (not shown in the figure) before being recycled to the adsorption or to the crystallization. The distilled solvent is then recycled into the centrifuge.
The process according to figure 3 could also be reproduced with a countercurrent washing column and a washing solvent other than the melted paraxyiene and the desorption solvent. In this case, after complete melting of the crystals, a stream of melted paraxyiene containing washing solvent is distilled, solvent is

recovered, at the top, that is recycled at least in part in the washing column and, at the bottom, paraxylene of very high purity-is recovered. The mother liquor comprising the washing liquor is drawn off from the washing column, distilled and recycled at least in part to the selective adsorption zone and optionally in part to the crystallization zone.
Figures 4 and 5 illustrate a two-stage crystallization, the temperature of the second crystallization stage being higher than that of the first stage. According to figure 4, the first crystallization unit 50, at -20°C for example, receives the crystallization charge (the extract distilled from the adsorption) by line 19. Its purity is about 80%. Crystals in suspension in a mother liquor are recovered by a line 51 and are separated in a first centrifuge 52. A first mother liquor containing, for example, 40% paraxylene is drawn off and recycled at least in part to adsorption zone 8 by lines 53 and 3 via the clay treatment and distillation zones, the other part being able to be recycled to the first crystallization.
The crystals recovered by a line 55 are melted in a melting zone 58 and are introduced by a line 59 into a second crystallization unit 70 operating for example at 0°C. A suspension of second crystals is recovered by a line 71, and is introduced into at least a second centrifuge 72 or a rotary filter.
A second mother liquor is recovered, by a line 73, and is recycled at least in part to the first crystallization unit 50 and optionally in part to the second crystallization zone. The

separated crystals are washed with the desorption solvent (toluene, for example) used as a washing solvent is introduced into the centrifuge by a line 56, and an added portion 57 coming from line 17 in particular, and a washing liquor 74 is drawn off that is recycled at least in part to the first crystallization unit 50 and/or to the second crystallization unit 70 after optionally having been distilled. It could also be recycled to the unit for distilling the raffinate (step b).
Furthermore, from a line 75 that is connected to centrifuge 72, the second crystals that are melted completely in a melting zone 76 are recovered, and melted paraxylene that is distilled in distilling column 60 is collected by line 77. The toluene recovered at the top is recycled by line 56 while the paraxylene of very high purity is drawn off at the bottom of the column by line 61.
Centrifuge 72 could be replaced with a countercurrent washing column. In this case, the second mother liquor containing washing toluene can be distilled, as is the case with a single stage before being recycled, and the washing toluene sent back to the washing column.
Figure 5 illustrates the use of a countercurrent column, of the NIRO column type, as a second zone for separation and washing of the second crystals, instead of centrifuge 72 of figure 4 or instead of a rotary filter, and which uses as washing solvent not toluene, but a portion of the melted paraxylene stream. According to this figure 5, comprising the same elements as those of figure 4, the second crystals in suspension in the second

mother liquor are recovered by a line 71 coining from the second crystallization unit, and it is introduced into NIRO column 80 which is fed with washing solvent by a portion of the melted paraxylene that is collected by a line 77a. Paraxylene crystals, of very high purity that are melted in melting zone 76 are collected by a line 75 and a stream of melted paraxylene is recovered by line 77. The second mother liquor having 70%, for example, paraxylene and the washing liquor are recovered at the same time and are recycled at least in part to the first crystallization unit 50 by a line 73 and optionally in part to the second crystallization unit.
According to another variant that is not illustrated by the figures, the washing solvent can be a solvent other than the stream of melted paraxylene and the desorption solvent, for example pentane. In this case, the stream of melted paraxylene is distilled so as to recover, at the top, washing solvent that is recycled at least in part in the second separation zone and, at the bottom, paraxylene of very high purity, the mother liquor comprising the washing liquor is distilled before being recycled to the first crystallization zone and optionally in part to the second crystallization zone if the second separation zone is a countercurrent washing column (a NIRO column, for example).
However, if the second separation zone is a centrifuge or a rotary filter, the mother liquor is recycled to the first crystallization zone and optionally in part to the second crystallization zone, and the washing liquor is distilled before

being recycled to the first crystallization zone and optionally in part to the second crystallization zone.
A recycling of the first crystals in suspension 51a and of the second crystals in suspension 71a can be envisioned, respectively in the first and in the second crystallization zone.
Figures 6 and 7 illustrate a two-stage crystallization of the paraxylene, the temperature of the second stage of crystallization of the mother liquor being lower than that of the first stage.
According to figure 6, the crystallization charge (the extract distilled from the adsorption) is introduced by line 19 into the first crystallization unit 70 which operates at about 0°C. First crystals in suspension in a first mother liquor are recovered by a line 81, and are separated in at least one first centrifuge 82, washed by toluene brought by a line 97 and recovered by a line 84. The first mother liquor containing, for example, 70% paraxylene is introduced at least in part by a line 83 into the second crystallization unit 50 operating at -10°C. Another part can be recycled in the first crystallization unit by a line 83a. Second crystals in suspension in a second mother liquor are recovered by a line 85, and they are separated in at least one second centrifuge 86. They are collected by a line 88 after having been washed with toluene that has been introduced by a line 98 into the second centrifuge. The second mother liquor collected by line 87 contains a fraction of the washing toluene; it is recycled at least in part to adsorption zone 8 via the clay

treatment and distillation zones and optionally in part by a line 87a to the second crystallization unit.
The first and second paraxylene crystals are mixed and introduced into a melting zone 89. A line 90 collects the melted paraxylene stream that is introduced into a distilling column 91 which delivers, at the bottom, paraxylene of very high purity and, at the top, toluene that is recycled by a line 92 and that is mixed with an added portion of toluene brought by a line 95 or line 18. The mixture of toluene obtained is introduced, at least in part, into each of centrifuges 82 and 86, as washing solvent.
Figure 7 uses the same elements and the same references as figure 6, except that for the step of washing the crystals, very pure melted paraxylene recovered from line 90 is used as washing solvent. Actually, at least a portion of the very pure melted paraxylene is drawn off by a line 91 and introduced into first centrifuge 82 and into second centrifuge 86 to wash the first and second crystals, respectively. The first mother liquor and a first washing liquor are sent by line 83 into the second crystallization unit 50 while the second mother liquor and the second washing liquor are collected by line 87 to be recycled, at least in part, to adsorption zone 8.
In this figure, the use of centrifuges 82 and 86 to separate the crystals of the mother liquors and to wash them has been described, but they could also be replaced with countercurrent columns, of the NIRO column type. In this case, the respective solutions collected would gather together the mother liquor and the washing liquor coming from each column.

Figure 8 illustrates another variant of the process having several crystallization stages, in which the melted paraxylene of; very high purity is collected at the output of the high-temperature crystallization zone.
The crystallization charge (the extract distilled from the adsorption) is introduced by line 19 into the first crystallization unit 70 which operates at about 0°C. Crystals in suspension in a first mother liquor are recovered by a line 81, and are separated for example on a NIRO column 80, the crystals recovered by a line 84 being melted in a melting zone 100. A stream of melted paraxylene of very high purity is collected by a line 101, that is drawn off in part thanks to line 102 to wash the crystals in the NIRO column. The first mother liquor which is drawn off from the NIRO column by line 83 is introduced, at least in part, into a second crystallization unit 50 operating at a temperature of -15°C, for example. Another part of this first mother liquor can be recycled by a line 83a and mixed with the charge of the first crystallization unit.
From the second crystallization unit 50, a suspension of second crystals in a second mother liquor is collected by a line 85, that is separated in at least one centrifuge 86 or a rotary filter. A second mother liquor is recovered, by a line 87, that is recycled at least in part to adsorption unit 8 via the clay treatment and distillation zones, a part being able to be recycled also to the second crystallization unit 50 by a line 105 connected to line 87.

The second crystals, once separated, are collected by a line 88 and melted optionally in a melting zone 103. The melted paraxylene is recycled by a line 104 and mixed with the charge of the first crystallization unit 70 to be recrystallized at the temperature of the first crystallization.
Figure 9 represents a preferred variant of the two-stage crystallization process operating advantageously between +5 and -7°C for the first and between -7 and -25C for the second.
The crystallization charge (the extract distilled from the adsorption) is introduced by line 19 into a first crystallization unit 70. First crystals in suspension in a first mother liquor are recovered by a line 81 and are separated in at least one centrifuge 82 or at least one rotary filter. The first mother liquor, collected by line 83, is introduced at least in part into a second crystallization unit 50, another part being able to be recycled to the first crystallization unit 70. A second suspension of crystals is collected by a line 85, that is separated in at least one centrifuge or rotary filter 86. A second mother liquor is drawn off by a line 87 and recycled at least in part to adsorption zone 8 via the clay-treatment and distillation zones, another part being able to be drawn off and recycled to the second crystallization unit by a line 87a connected to line 87. The first and second crystals respectively collected by lines 84 and 88 are gathered together and introduced into at least one washing column 110, of the NIRO column type, where they are washed by a washing solvent. Paraxylene crystals are collected by a line 111, which are completely melted in a

melting zone 112 and a stream of paraxylene of very high purity is drawn off. A portion of the paraxylene stream is drawn off by a line 114 and introduced as washing solvent into column 110. The washing liquor collected in the column is recycled at least in part to the first crystallization unit.
According to figure 10, when the washing solvent in the washing column is the desorption solvent (toluene) or another suitable solvent such as pentane, the stream of melted paraxylene containing a minor portion of solvent can be distilled in a distillation unit 117. The paraxylene of very high purity is collected by a line 118 while the light fraction comprising the washing solvent is recycled into the NIRO column. Finally, the washing liquor drawn off by line 15 and containing solvent is distilled in a distillation unit 120, the solvent is recycled at least in part in the column and the washing liquor, freed of the major portion of the solvent, is recycled at least in part to the first crystallization unit by line 121.
The recycling of the mother liquor coming from a crystallization stage A in said stage A or from a stage B in said stage B has been mentioned for a given figure. Of course, these recyclings can apply for all the figures.
Also, it is known that a suspension of crystals coming from a crystallization stage can be recycled to this stage and this recycling can also apply to all the figures (81a and 85a) .
The term of a separation zone has often been used in the description. Of course, it involves at least one centrifuge or

at least one rotary filter or at least one column for countercurrent washing by a solvent.
The separation zone where the washing of the crystals is performed can comprise at least one centrifuge or at least one rotary filter. It has been observed, however, that by using, as separation zone where the washing of the crystals is performed, at least one countercurrent washing column, of the NIRO type for example and in particular, with a portion of the very pure melted paraxylene collected, as washing solvent, excellent results were obtained and the cost of the utilities was reduced.
As has been diagrammed in figure 1, the mother liquor coming from crystallization unit 5b is recycled to adsorption unit 8. In the case of a two-stage or multi-stage crystallization, the mother liquor comes from the coldest crystallization stage after the separation of the paraxylene crystals (line 53, figure 5, line 87, figure 7 to 9). The impurities which circulate in the loop of the adsorption, crystallization, isomerization device can be olefinic hydrocarbons, as well as paraffinic and naphthenic hydrocarbons or other oxygenated compounds. They can come in particular, both from the charge to be treated which comes from a catalytic reforming and from the isomerization. These impurities therefore circulate and can be found in all the fractions and particularly in the extract and therefore in the mother liquor resulting from the crystallization step. This mother liquor can be introduced by a line 32 that is connected to line 3 and to line 53 or 87 in at least one clay-treatment reactor 26, advantageously two, placed upstream and connected by a line 27 to

adsorption unit 8. Line 1 containing the charge to be treated and line 2 containing the isomerate can be connected to this line-32, the three flows being thus treated in a mixture in a single reactor 26.
According to another variant, charge 1 can have been pretreated in another clay-treatment reactor (not indicated in the figure). It is the same for isomerate 2 which can also have been initially pretreated after having passed into distillation unit 23.
According to a preferred variant, mother liquor 3 can be introduced directly into line 22 leading to distillation unit 23 of the isomerate, before being treated, in mixture with the distilled isomerate, in clay-treatment reactor 26. This variant makes it possible to eliminate approximately all the most volatile compounds, not only from the isomerate but from the mother liquor.
When the distillation unit is adjusted to deliver also, at the bottom, an additional fraction containing most of the heavy compounds (C9+ hydrocarbons, aldehydes, ketones), the clay treatment of the distilled mixture comprising the isomerate and the mother liquor is thereby substantially improved.
A portion of the mother liquor can also be recycled by a line 31 to effluent 27 of reactor 26.
The effluent of the clay-treatment reactor and optionally the crystallization mother liquor 31 that can further contain heavy hydrocarbons, such as hydrocarbons having nine carbon atoms, are introduced by a line 27 into a distilling column 28

which delivers, at the bottom of the column (line 29), the undesirable impurities and, at the top, a distillate corresponding to the purified C8 fraction, that is introduced by line 4 to adsorption unit 8. A portion of the mother liquor can also be introduced into line 4 by a line 30.
These various recyclings can be combined with one another, when it involves, for example, reusing existing pieces of equipment for distillation 23, clay treatment 26 or distillation 28 and when one of these pieces of equipment is already operated at its maximum flow rate or else when it is desired to have the amount of an impurity in the loop lowered without seeking to eliminate it completely. In other words, the mother liquor of the crystallization unit (the coldest stage), conveyed by line 3, can be partially recycled to adsorption unit 8 either directly by means of line 30, or indirectly by means of lines 31, 32 or 33.
So as to keep the amount of constituents with intermediate volatility of the toluene (desorption solvent) at a tolerable level, for example less than 5%, at least one purge of toluene polluted by said constituents is performed by means of a line 35 connected either to line 17, or to line 14 or to line 11 collecting all the solvent recycled to adsorption unit 8.
In addition, it is possible to perform a purge of the mother liquor coming from the crystallization if the amount of constituents with intermediate volatility is too great there. This purge is performed by means of line 34 connected to line 3.
The purge of toluene can be compensated for by an added portion of toluene. Since the greatest sources of Cg-aromatic

fraction (line la) come from the catalytic reforming, from dismutation (disproportionation) of the toluene into benzene and • xylene and from the toluene - C8-aromatic transalkylation and since the effluents of these units from which they come are in part generally purified in a series of distillation units of which column 28 can be part, it is possible to use, at least in part, as a source of added portion of toluene, either the one
produced at the top (line 42) of a distilling column 40 of toluene, before reactor 26 containing the clay, or the one which results from the bypass by a line lb of at least a portion of the charge (line 1) that is mixed with the effluent from the bottom of column 40, or the one which is introduced into the purified charge (line 1) by putting column 40 out of adjustment, which makes it possible to allow the desired proportion of toluene pass into the C8 fraction.

WE CLAIM:
1. A process for the production of paraxylene of high purity from a charge containing a mixture of aromatic hydrocarbons having 7 to 9 carbon atoms, comprising circulating at least a portion of the charge in an enrichment zone to produce a first fraction with paraxylene, purifying at least a portion of said first fraction in a purification zone by at least one crystallization in at least one crystallization zone, said crystallization zone comprising at least two crystallization stages at a temperature between +50 and -22°F, and recovering paraxylene crystals from each crystallization stage.
2. The process according to claim 1, wherein the enrichment zone is at least one crystallization zone at a temperature lower than that of said crystallization stages, said process comprising introducing the charge, to said enrichment zone, producing a liquid and crystals, isomerizing said liquid in an isomerization zone and melting said crystals to form at least a portion of said first fraction.
3. The process according to claim 1, wherein the enrichment zone is a selective adsorption zone containing a zeolitic adsorbent, said process comprising introducing the charge, performing selective adsorption of the charge in the presence of a desorption solvent, recovering a paraxylene enriched first fraction and a paraxylene depleted second fraction, isomerizing said second fraction in an isomerization zone containing an isomerization catalyst under suitable conditions, to produce an isomerate containing paraxylene, and recycling the isomerate, at least in part, to the adsorption zone.

4. The process according to claim 1, wherein the enrichment zone is at least one zone of disproportionation of a charge consisting essentially of toluene, said process comprising producing in said disproportionation zone an effluent containing benzene and xylenes, and distilling said effluent to remove beazene and unreacted toluene to produce the first fraction with parax.
5. The process according to claim 1, comprising performing in the purification zone a first crystallization at a temperature Tl and a second csystallization at a temperature T2, higher than T1.
6. The process according to claim 5, comprising recycling at least a portion of mother liquor resulting from the coldest crystallization stage of the purification zone to the enrichment zone.
7. The process according to claim 1, comprising performing a first crystallization of the paraxylene-enriched fraction in a first crystallization zone at a temperature Tl, recovering a suspension of first paraxylene crystals in a first mother liquor, separating the first crystals from the first mother liquor in a first separation zone, recovering a first mother liquor, recycling separated liquior to the enrichment zone, melting separated first crystals completely and crystallizing in a second crystallization zone at a temperature T2 that is higher than Tl, recovering a suspension of second paraxylene crystals in a second mother liquor, separating the second crystals from the second mother liquor in a second separation zone, washing the second crystals with a washing solvent in the second separation zone, recovering a washing liquor, recycling at least part of the second mother liquor, and at least a porticxi of the washing liquor to the first crystallization stage and optionally in part to the second crystallization zone and melting the second paraxylene crystals completely so as to obtain a liquid stream of melted paraxylene.

8. The process according to claim 7, comprising recycling the washing liquor, in part, to the second crystallization zone.
9. The process according to claim 7, wherein the content of paraxylene resulting from the enrichment zone is at least 50% by weight
10. The process according to claim 1, comprising performing a first crystallization of the paraxylene-enriched fraction in a first crystallization zone at a temperature Tl, recovering a suspension of first paraxylene crystals in a first mother liquor, separating the first crystals from the first mother liquor in a first separation zone, ooptionally washing the first crystals with a washing solvent in the first separation zone, crystallizing at least a portion of the first mother liquor in a second crystallization zone at a temperature T2 that is lower than temperature Tl, recovering a suspension of second paraxylene crystals in a second mother liquor, separating the second crystals from the second mother liquor in a second separation zone, washing the second crystals with the washing solvent in the second separation zone, recovering a second mother liquor, mixing the first and second paraxylene crystals, completely melting said crystals and recovering a stream of melted paraxylene.
11. The process according to claim 10, comprising washing the first crystals with a washing solvent in the first separation zone.
12. The process according to claim 10, wherein the content of paraxylene resulting
from the enrichment zone is at least 50% by weight.

13. The process as claimed in claim 1, wherein performing a first crystallization of a paraxylene-enriched fraction, having a paraxylene content of at least 50% by weight, and of optionally melted recycled crystals coming from a second crystallization in a first high temperature crystallization zone at a temperature Tl, recovering a suspension of paraxylene crystals in a first mother liquor, separating the crystals from the first mother liquor in a first separation zone, washing said crystals, melting said crystals and recovering a stream of melted paraxylene, crystallizing at least a portion of the first mother liquor in a second high temperature crystallization zone at a temperature T2 that is lower than temperature Tl, recovering a suspension of second paraxylene crystals in a second mother liquor, separating the second crystals from the second mother liquor in a second separation zone, recovering a second mother hquor, and second crystals, optionally melting a portion of the second crystals and recycling the optionally melted second melted crystals to the first crystallization zone and recrystallizing the melted crystals with the paraxylene-enriched fraction at a temperature Tl.
14. The process according to claim 13, wherein melting the second crystals, recycling and recrystallizing said crystals with the paraxylene-enriched fraction at temperature T1.
15. The process according to claim 1, wherein performing a first crystallization of the paraxylene-enriched fraction and of partially melted recycled crystals coming from a second crystallization in a first crystallization zone at a temperature Tl, recovering a suspension, of paraxylene crystals in a first mother liquor, separating the crystals from the first mother liquor in a first separation zone, washing said crystals in a centrifuge or a countercurrent column, melting said crystals and recovering a stream of melted paraxylene.

crystallizing at least a portion of the first mother liquor in a second crystallization zone at a temperature T2 that is lower than temperature Tl, recovering a suspension of second paraxylene crystals in a second mother liquor, separating the second crystals from the second mother liquor in a second separation zone, recovering a second mother liquor, partially melting the second crystals and recycling the crystals in a slurry to the first crystallization zone, and recrystallizing said slurry with the paraxylene-enriched fraction at temperature Tl.
16. The process according to claim 1, wherein performing a first crystallization of
the paraxylene-enriched fraction in a first crystallization zone at a temperature
Tl, recovering a suspension of first paraxylene crystals in a first mother liquor,
• separating the first crystals from the first mother liquor in a first separation zone, crystallizing at least a portion of the fu-st mother liquor in a second crystallization zone at a temperature T2 that is lower than Tl, separating the second crystals from the second mother liquor is a second separation zone, recovering the second mother liquor, recovering the first crystals and the second crystals and washing in at least one separation and washing zone with a washing solvent, recycling a washing liquor at least in part to the first crystallization zone; recovering paraxylene crystals and completely melting said crystals in a melting zone and collecting a stream of melted paraxylene.
17. The process according to claim 16, wherein the first and second crystals are washed in a separation and countercurrent washing zone subsequent to recovery.
18. The process according to claim 1, wherein the content of paraxylene resulting from the enrichment zone is at least 50% by weight, and the temperature Tl of one of the crystallization stages is different than the temperature T2 of another crystallization stage.

19. The process according to claim 18, wherein the crystallization temperature is between -10 °C and -25"C.
20. The process according to claim I, wherein the crystallization zone comprising a first and second crystallization stage, said process comprising recovaing first crystals from said first crystallization stage, and washing said crystals in at least one countercurrent washing zone.
21. The process according to claim 20, comprising washing said crystals with a washing solvent which is melted paraxylene from said crystallization zone.
22. The process according to claim 20, con:q)rising washing said crystals with a washing solvent which is toluene.
23. The process according to claim 22, wherein the toluene is used as a desorption solvent in a selective adsorption process in the enrichment zone.
24. The process according to claim 20, comprising washing said crystals with a washing solvent which is pentane.
25. The process according to claim 1, said crystallization zone comprising a first and second crystallization stage, said process comprising recovering second crystals from said second crystallization stage, and washing said crystals in at least one countercurrent washing zone.
26. The process according to claim 1, said crystallization zone comprising a first and second crystallization stage, said process comprising recovering first and second crystals from said first and second crystallization stages, respectively, and washing said crystals in at least one countercurrent washing zone.

27. The process according to claim 26, wherein said first and second crystals are
combined and sent to said countercurrent washing zone.
28. The process according to claim 13, wherein T2 is +10 to -30*C.
29. The process according to claim 13, wherein Tl and T2 are +10 to -30°C.
30. A process for the production of high purity paraxylene substantially as herein
described with reference to the accompanying drawings.

Documents:

1724-mas-1995 abstract.pdf

1724-mas-1995 claims.pdf

1724-mas-1995 correspondence-others.pdf

1724-mas-1995 correspondence-po.pdf

1724-mas-1995 description (complete).pdf

1724-mas-1995 drawings.pdf

1724-mas-1995 form-1.pdf

1724-mas-1995 form-26.pdf

1724-mas-1995 form-4.pdf

1724-mas-1995 others.pdf

1724-mas-1995 petition.pdf

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Patent Number

193832

Indian Patent Application Number

1724/MAS/1995

PG Journal Number

13/2007

Publication Date

30-Mar-2007

Grant Date

19-Feb-2005

Date of Filing

27-Dec-1995

Name of Patentee

M/S. INSTITUT FRANCAIS DU PETROLE

Applicant Address

4, AVENUE DE BOIS PREAU, 92502, RUEIL MALMAISON

Inventors:

#	Inventor's Name	Inventor's Address
1	MAC PHERRSON STUART R	140 HIGHLAND AVE., PIEDMONT, CA 94611
2	MIKITENKO PAUL	25 RESIDENCE OREE DE MARLY 78590 NOISY LE ROY

PCT International Classification Number

C07C7/14

PCT International Application Number

N/A

PCT International Filing date

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1			NA