CN103201240A - Process for the production of paraxylene - Google Patents
Process for the production of paraxylene Download PDFInfo
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- CN103201240A CN103201240A CN2011800523920A CN201180052392A CN103201240A CN 103201240 A CN103201240 A CN 103201240A CN 2011800523920 A CN2011800523920 A CN 2011800523920A CN 201180052392 A CN201180052392 A CN 201180052392A CN 103201240 A CN103201240 A CN 103201240A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/14—Purification; Separation; Use of additives by crystallisation; Purification or separation of the crystals
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
- C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
- C07C5/2729—Changing the branching point of an open chain or the point of substitution on a ring
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
- C07C7/13—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers by molecular-sieve technique
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Abstract
A process for the purification of aromatic feedstream to produce paraxylene is disclosed, including the separation of a C8+ aromatic feedstream into a steam comprising C8 aromatic species and a stream comprising C9+ aromatic species. After separation of PX from the C8 aromatic stream, a PX-depleted stream is separated and processed in a liquid phase isomerization unit and a vapor phase isomerization unit in parallel.
Description
Contriver: Dana Lynn Pilliod and John Di-Yi Ou
Prioity claim
The application requires the U.S. Provisional Application submitted on October 29th, 2010 number 61/408,097 and rights and interests and the right of priority of the EP10192327.4 that submits on November 24th, 2010.
Technical field
The equipment that the present invention relates to prepare the method that comprises xylene isomerization of p-Xylol and put into practice described method.
Background technology
Xylene isomer is important intermediate, and they have extensive and various application in chemosynthesis.As an example, p-Xylol (PX) is the raw material for the manufacture of the terephthalic acid of synthon; M-xylene (MX) is for the manufacture of dyestuff, and o-Xylol (OX) is as the raw material of Tetra hydro Phthalic anhydride, and this Tetra hydro Phthalic anhydride is for the manufacture of softening agent.
Dimethylbenzene appears at various fractions for example in coal tar fraction, petroleum reforming product and the pyrolysis liquid with the form with other compound fusion with similar boiling point.By easily aromatic component being separated with non-aromatic compound such as solvent-extracted method.Can for example easily obtain fraction (being formed by the C8 aromatic substance basically) by distillation then." C8 aromatic substance " refers to contain the aromatic hydrocarbon of 8 carbon atoms, especially comprises ethylbenzene and xylene isomer p-Xylol (PX), o-Xylol (OX) and m-xylene (MX).
Though owing to their similar chemical structures, physicals and identical molecular weight are difficult to separate, but there are the various methods that are used for separation of C 8 isomer, for example OX can separate with other C8 aromatic substance by fractionation, and PX can separate by fractional crystallization or selective adsorption.Current have very big demand also to wish MX (the main dimethylbenzene that exists in the feed stream) and OX are changed into PX to PX, to meet the need of market.Under the normal temps of processing dimethylbenzene, thermodynamic(al)equilibrium content is about 24mol%PX in typical petroleum chemical plant, and 56mol%MX and 20mol%OX are based on the total amount of dimethylbenzene in the described raw material.
The preparation of p-Xylol is energy-intensive in the conventional aromatic substance mixture.A large amount of recycled materials that reprocess owing to removing via C9+ on this part ground.Typical business method is presented among Fig. 1, it shows the materials flow that processing comprises C8+ aromatic substance (aromatic hydrocarbon of C8 aromatic hydrocarbon and Geng Gao carbon number), and such purpose is to reclaim the materials flow that comprises PX by the bigger amount of the amount of finding in the equilibrium mixture than dimethylbenzene at least in part.
One or more feed stream of using in the system shown in Figure 1 can be from various sources, for example be selected from one or more following sources: the methylate product of toluene of C8+ reformate 1, C8+ selectivity toluene disproportionation product 17, C8+ transalkylated product 2, C8+ toluene disproportionation product 15 and contain any other materials flow of C8 aromatic substance, the methyl alcohol of for example must using by oneself.In these sources each is that itself is well-known in the art.These materials flows comprise described four kinds of C8 isomer and heavy aromatic compounds (C9+ aromatic substance) more usually, and they are together with processed to remove the C9+ aromatic substance in materials flow 3 in one or more separation columns of recycle stream 10 in C8/C9+ aromatic substance fractionation 16.If described C9+ and more heavy aromatic compounds by fractionation from feed stream (one or more) do not remove may to the p-Xylol in downstream reclaim 12 and xylene isomerization 13 have disadvantageous effect.
Therefore C8/C9+ aromatic substance fractionation in 16 produces the bottom product 3 that contains the C8 aromatic stream 6 of 10-95wt% p-Xylol usually and comprise the C9+ aromatic substance.Processing C8 aromatic stream 6 is so that p-Xylol among Fig. 1 reclaims one of the selective adsorption of unit 12 or crystallization or both optionally reclaim p-Xylol by being shown as.Can comprise 99.7wt% nearly or even the p-Xylol product of higher p-Xylol reclaim as materials flow 7, allow the rest part of C8 aromatic substance flow to gas phase xylene isomerization 13 via conduit 8.Randomly, in the presence of the hydrogen that is provided by materials flow 9, gas phase xylene isomerization 13 uses and ethylbenzene can also be changed into benzene and ethane and maybe ethylbenzene can be changed near in the various catalyzer of the xylene isomer of balance one or more set up the balance near balance of xylene isomer in materials flow 19.Therefore gas phase process and catalyzer are that itself is well-known in this area.
Continue system shown in Figure 1, xylene isomerization product 19 flows to piptonychia benzene and divides and heat up in a steamer 18, its in materials flow 11, remove C7 and than light material (C7-) to produce isomerization product recycle stream 10.Isomerization product recycle stream 10 is recycled to C8/C9+ aromatic substance fractionation 16.
Improving this kind energy intensive method is the active research field, but it is not the simple thing of optimizing each individual step, because the one or more steps in the optimization of the step possibility negative impact total system.The improved example that proposes comprises following.
U.S. Patent number 3,856,874 have described the ejecta materials flow shunting that will separate from PX, allow independently materials flow process on different catalyzer, then the isomerization materials flow are merged and circulation.
U.S. Patent number 7,439,412 have instructed the method that reclaims one or more high purity xylene isomers from the materials flow of C8+ aromatic raw material, are included under the liquid-phase condition and use isomerization unit.In an embodiment, the product of liquid-phase isomerization unit is sent back to first separation column in the system.Also referring to U.S. Patent number 7,626,065.
U.S. Patent number 7,553,998 have instructed the method that reclaims one or more high purity xylene isomers from the raw material with quite big C9+ aromatic content, comprise: heavy aromatic compounds take off ethylization, then fractionation allows described materials flow flow to the C8 aromatic isomers then and reclaims to reclaim the high purity xylene isomer under the energy cost that reduces.To under the liquid isomerisation conditions, pass the materials flow shunting of isomerization unit, and a part be delivered to isomer reclaim the unit and remove a part.
U. S. application sequence number 12/612,007 (being disclosed as 2010/0152508) has been described and has been prepared the method that is rich in the PX product, and this method comprises: the materials flow of the poor PX of containing (a) is provided; (b) with at least a portion isomerization of the materials flow of the described poor PX of containing with preparation PX concentration greater than the described poor materials flow that contains PX and benzene concentration less than 1,000ppm and C
9+ hydrocarbon concentration is less than the isomerization materials flow of 5,000ppm; (c) by selective adsorption described isomerization materials flow is separated.
The provisional application of submitting on April 21st, 2010 number 61/326,445 relate to Xylene isomerization process, comprise liquid-phase isomerization, in order to produce balance or near the dimethylbenzene of balance, wherein said processing condition comprise less than 295 ℃ temperature and are enough to keep the pressure of dimethylbenzene in liquid phase.
Significant other reference comprises US publication 2008/0262282; 2009/0149686; 2009/0182182; U.S. Patent number 6,448,459; 6,872,866 and 7,368,620.
The inventor it has surprisingly been found that a kind of method, and this method has reduced the desired energy of preparation high purity xylene isomer significantly by the configuration in parallel that gas phase and liquid-phase isomerization system are provided.
Summary of the invention
Summary of the invention
The present invention relates to the preparation method of p-Xylol, comprise: the raw material that at first will comprise the C8+ aromatic substance is separated into overhead product or first materials flow and the bottom product that comprises the C9+ aromatic substance or second materials flow that comprises xylene isomer, described dimethylbenzene materials flow separation in PX recovery unit is rich in the materials flow of PX and the materials flow of the poor PX of containing with recovery, and the configuration in parallel via gas phase xylene isomerization and liquid phase xylene isomerization separates the described poor PX of containing (C8 aromatic substance) materials flow then.
In embodiments, the benzene separating step carries out between C8/C9+ fractionation and PX recovery unit, and/or the benzene separating step carries out in isomerization steps (one or more) downstream.In embodiments, the toluene separating step can also be arranged, for example at the toluene separating step in described isomerization steps (one or more) downstream.
In embodiments, the liquid-phase isomerization product is recycled to one or more in C8/C9+ fractionation, benzene separating step (when existing) and the PX recycling step.
The invention still further relates to the equipment that comprises first separation column of preparation p-Xylol, described first separation column is operated being suitable for the C8+ aromatic stream is separated into the overhead product that comprises dimethylbenzene and comprising under the condition of bottom product of C9+ aromatic substance, described overhead product materials flow is reclaimed the unit fluid with PX and is communicated with, wherein said PX reclaims the unit materials flow of being rich in PX and the materials flow of the poor PX of containing is provided, and improves the conduit that comprises the materials flow that will carry the described poor PX of containing and divides so that allow the part of materials flow of the described poor PX of containing flow to the gas phase isomerization unit and allow another part of materials flow of the described poor PX of containing flow to the liquid-phase isomerization unit.
In embodiments, the liquid-phase isomerization product circulation that described liquid-phase isomerization unit fluid is communicated with so that is provided to described first separation column and/or reclaims the unit to described PX.
In embodiments, described PX reclaims the unit and is selected from least a in crystallizer and the adsorptivity separator.
In embodiments, at least one other separation column is in the described first separation column upstream, wherein said at least one other separation column is operated under being suitable for the condition of removing benzene or removing toluene from the materials flow that comprises dimethylbenzene from the materials flow that comprises dimethylbenzene and is randomly wherein said be used to the separation column of removing benzene and the described upstream that all is provided at described first separation column be used to the separation column of removing toluene.
The objective of the invention is by making the isomerization product internal circulating load from the gas phase xylene isomerization minimize the desired energy of minimizing preparation p-Xylol significantly.
When with reference to following detailed description, embodiment preferred, embodiment and appended claims, these and other objects, feature and advantage will become apparent.
The accompanying drawing summary
In the accompanying drawings, identical Ref. No. is used for representing the identical part in whole several views.
Fig. 1 is the synoptic diagram that illustrates for the prior art flow process configuration of xylene isomerization.
Fig. 2 is the synoptic diagram that illustrates embodiment of the present invention.
The contrast of Fig. 3 and 4 two systems of expression (each embodiment of the present invention), the former sends back to rerunning tower with the liquid isomerization product, and the latter sends back to PX with the liquid isomerization product and reclaims the unit.
Describe in detail
According to the present invention, the hydrocarbon flow that will comprise the C8+ aromatic substance is separated into the materials flow that comprises the C8 aromatic substance and comprises the materials flow of C9+ aromatic substance.Allow described C8 materials flow (randomly passing the benzene separating unit) flow to PX then and reclaim the unit so that two materials flows to be provided, a materials flow has the PX concentration of increase and the PX concentration that another has reduction.Then the described poor materials flow that contains PX is divided, then in parallel at least one liquid isomerization unit and isomerization at least one gas phase isomerization unit.
Can understand the present invention better by the particular that shows with reference to figure 2.Having read it will be appreciated by those skilled in the art that of present disclosure can make many improvement and described embodiment and should not be considered as the present invention who describes in the restriction appended claims.
The feed stream (one or more) of system shown in Figure 2 can be come one or more sources of self-contained C8+ aromatic hydrocarbon: comprise C8+ reformate 1, C8+ selectivity toluene disproportionation product 17, C8+ transalkylated product 2, C8+ toluene disproportionation product 15 and contain any other materials flow of C8 aromatic substance, the methylate product of toluene of the methyl alcohol of for example must using by oneself.
In flow process configuration shown in Figure 2, following minimizing energy expenditure: make the amount that minimizes and control the C9+ aromatic substance of processing in C8/C9+ aromatic substance fractionation 16 from the amount of the isomerization product recycled material 10 of gas phase xylene isomerization 13.Described new process configurations comprises via gas phase xylene isomerization and the poor C8 aromatic stream 8 that contains p-Xylol of liquid phase xylene isomerization 20 processing in parallel.The poor flow that contains the C8 aromatic stream 8 of p-Xylol is minimized pass gas phase xylene isomerization 13 to make energy minimization with the amount of the poor C8 aromatic stream 30 that contains p-Xylol by reducing in gas phase xylene isomerization 13 gasification and the associated volume that reduces isomerization product recycle stream 10, this isomerization product recycle stream 10 contains the by product C9+ aromatic substance of the concentration more much higher than liquid phase xylene isomerization product.The LP isomerization product recycle stream 21 that at higher feed entrance point will be the product of liquid phase xylene isomerization 20 is delivered to the fractionation 16 of C8/C9+ aromatic substance with minimises power consumption, and this is owing to the C9+ aromatic substance of its low concentration.The total power consumption that the amount of energy saving can cause preparing the method for p-Xylol in the fractionation 16 of C8/C9+ aromatic substance reduces nearly 75%.
Fig. 2 shows randomly liquid-phase isomerization product recycle stream 21 to be delivered to and comprises C8 aromatic substance/C9+ aromatic substance fractionation 16, removes unit 23 (having the benzene materials flow of following 22) and directly arrive p-Xylol via conduit 60 and reclaim one or more positions of 12 to benzene via conduit 50.Determine to deliver to the amount of each position by the needs of removing the by product that comprises benzene and C9+ aromatic substance.May need to remove the by product from liquid phase xylene isomerization 20 in the liquid-phase isomerization product recycle stream 21 and be low to moderate p-Xylol and reclaim 12 acceptable levels, if when particularly selective adsorption being used for reclaiming p-Xylol.Can be in C8/C9+ aromatic substance fractionation 16 or adopting isolation technique for example to remove the C9+ aromatic substance in one or more equipment of film, extraction and absorption.Similarly, can use adopt that isolation technique is for example distilled, one or more equipment of extraction, film and absorption remove benzene.Randomly, can use adopt that isolation technique is for example distilled, one or more equipment of extraction, film and absorption remove C9+ aromatic substance and benzene simultaneously.
Randomly, in the presence of the hydrogen in materials flow 9, gas phase xylene isomerization 13 uses in this areas well-known benzene and ethane of ethylbenzene can also being changed into itself maybe ethylbenzene can be changed near in the various catalyzer of the xylene isomer of balance one or more set up balance near the xylene isomer of balance in materials flow 19.Xylene isomerization product materials flow 19 flows to piptonychia benzene divides and heats up in a steamer 18, this piptonychia benzene divide heat up in a steamer 18 in materials flow 11, remove C7 and more light material to produce isomerization product recycle stream 10.Remove processing isomerization product recycle stream 10 in the unit 16 at OX and C9+ aromatic substance.
As for the separation of dimethylbenzene in PX reclaims, two kinds of preferable methods are fractional crystallization and selective adsorption, and their detailed description itself is as known in the art.In this respect, referring to, for example, U.S. Patent number 7,439,412, and the reference of enumerating in the top background parts.The detailed description of crystallization and selective adsorption itself is not theme of the present invention.
Equally, the detailed description of gas phase xylene isomerization and liquid phase xylene isomerization also is that itself is known in this area.In this respect, referring to for example, U.S. Patent number 6,180,550; 6,448,459; 6,872,866; 7,244,409; 7,371,913; 7,495,137; 7,592,499; U.S. Patent Application Publication No. 2009-0182182; U. S. application sequence number 12/612,007; With the temporary patent application of submitting on April 21st, 2010 number 61/326,445.
Implement to use the computer simulation of Pro II program (it is commercially available software) to be intended to verify interests of the present invention.Make suitable supposition, for example U.S. Patent number 7,439, provide in 412 like that, this is those skilled in the art's technical ability.Filling apparatus with PX capacity of 540kta is worked as base case (Fig. 1).Two kinds of Process configuration of this modeling effort: method A shown in Figure 3 and method B shown in Figure 4.In these two kinds of method A and B, be split into two equal cuts with deriving from the materials flow of the poor PX of containing that PX reclaims the C8 aromatic substance of unit 12, one of them is delivered to liquid phase xylene isomerization unit 20, simultaneously another cut is delivered to gas phase xylene isomerization unit 13.As shown in the figure, method A (Fig. 3) gives rerunning tower 16 with the product of liquid phase xylene isomerization unit 20, and method B (Fig. 4) gives PX recovery unit 12 (Parex with the product of liquid phase xylene isomerization unit 20
TMThe absorptivity separating unit, itself is well-known in this area).As among Fig. 1 and 2, Fig. 3 and 4 makes the gas phase isomerization product pass from 13 to take off toluene tower 18 to remove toluene and to allow balance or flow back into rerunning tower 16 near the dimethylbenzene of balance.This analog information uses the method according to this invention, compares with the base case of Fig. 1, has 13.10MW (megawatt) and has the remarkable energy saving of 12.45MW for method A (Fig. 3) for method B (Fig. 4).
With reference to many embodiments and specific embodiment the present invention has been described above.Many changes are apparent to having read the those skilled in the art that describe in detail above.
In another embodiment, the present invention relates to:
1. prepare the method for p-Xylol, comprising:
(a) raw material that will comprise the C8+ aromatic substance is separated into first materials flow that comprises xylene isomer and second materials flow that comprises the C9+ aromatic substance in first fractionating step;
(b) reclaim in the unit at p-Xylol (PX) and described first materials flow separated to reclaim the materials flow of being rich in PX and the materials flow of the poor PX of containing;
(c) allow the described poor PX of containing materials flow first part through gas phase xylene isomerization unit with prepare the first isomerization product materials flow and allow the second section of materials flow of the described poor PX of containing through liquid phase xylene isomerization unit to prepare the second isomerization product materials flow; With
(d) randomly, also comprise the benzene separating step, wherein benzene is separated with the materials flow that comprises dimethylbenzene.
2. section 1 method, comprise at least one benzene separating step, described benzene separating step is selected from the benzene separating step between described liquid phase xylene isomerization unit and described first fractionating step, and the benzene separating step between described liquid-phase isomerization unit and the described PX recovery unit.
3. the method for section one of 1 and 2 wherein is recycled to the described second isomerization product materials flow one or more in described first fractionating step, one or more benzene separating step (when existing) and the described PX recovery unit.
4. arbitrary section method in the aforementioned paragraphs, wherein at least a portion with the product of described liquid-phase isomerization unit is recycled to described first fractionating step.
5. arbitrary section method among the section 2-4, wherein at least a portion with the product of described liquid-phase isomerization unit is recycled at least one benzene separating step.
6. arbitrary section method in the aforementioned paragraphs, wherein the product with described liquid-phase isomerization unit is recycled to described PX recycling step.
7. arbitrary section method in the aforementioned paragraphs, wherein said PX recycling step comprises crystalline element.
8. arbitrary section method in the aforementioned paragraphs, wherein said PX recycling step comprises selective adsorption.
9. arbitrary section method in the leading portion is if also comprise the fractionation of isomerization product recycle stream to remove the step that is present in the toluene in the described materials flow.
10. arbitrary section method in the aforementioned paragraphs, the raw material of the wherein said C8+ of comprising aromatic substance comprises the raw material of at least a C8+ of being selected from selectivity toluene disproportionation product, C8+ transalkylated product, C8+ reformate and C8+ toluene disproportionation product.
11. in the equipment of preparation p-Xylol (PX), described equipment comprises first separation column, described first separation column is operated being suitable for the C8+ aromatic stream is separated into the overhead product that comprises dimethylbenzene and comprising under the condition of bottoms product stream of C9+ aromatic substance, described overhead product materials flow is reclaimed the unit fluid with PX and is communicated with, wherein said PX reclaims the unit materials flow of being rich in PX and the materials flow of the poor PX of containing is provided, and improves the conduit that comprises the materials flow that will carry the described poor PX of containing and divides so that allow the part of materials flow of the described poor PX of containing flow to the gas phase isomerization unit and allow another part of materials flow of the described poor PX of containing flow to the liquid-phase isomerization unit.
12. the equipment of section 11, wherein the liquid-phase isomerization product circulation that described liquid-phase isomerization unit fluid is communicated with so that is provided to described first separation column and/or reclaims the unit to described PX.
13. section 11 equipment, wherein said PX reclaim the unit and are selected from least a in crystallizer and the adsorptivity separator.
14. the equipment of section 11, comprise that also at least one is at other separation column of the described first separation column upstream, wherein said at least one other separation column under being suitable for the condition of from the materials flow that comprises dimethylbenzene, removing benzene or from the materials flow that comprises dimethylbenzene, removing toluene or both of these case, operate and wherein said at least one other separation column in the described first separation column upstream.
The employed trade(brand)name of this paper by
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Symbolic representation shows that these titles may be protected by some trade mark right, and for example they may be the registered trademarks in the various judicial powers.All patents that this paper quotes and patent application, testing sequence (for example priority document, ASTM method, UL method etc.) are consistent with the present invention and for reference at fully introducing on the degree of all authorities that allow this introducing in this publication with other file.When numerical lower limits and numerical upper limits when this lists, the scope from arbitrary lower limit to arbitrary upper limit should be considered.
Claims (14)
1. prepare the method for p-Xylol, comprising:
(a) raw material that will comprise the C8+ aromatic substance is separated into first materials flow that comprises xylene isomer and second materials flow that comprises the C9+ aromatic substance in first fractionating step;
(b) reclaim in the unit at p-Xylol PX and described first materials flow separated to reclaim the materials flow of being rich in PX and the materials flow of the poor PX of containing;
(c) allow the described poor PX of containing materials flow first part through gas phase xylene isomerization unit with prepare the first isomerization product materials flow and allow the second section of materials flow of the described poor PX of containing through liquid phase xylene isomerization unit to prepare the second isomerization product materials flow; With
(d) randomly, also comprise the benzene separating step, wherein benzene is separated with the materials flow that comprises dimethylbenzene.
2. the method for claim 1, comprise at least one benzene separating step, described benzene separating step is selected from the benzene separating step between described liquid phase xylene isomerization unit and described first fractionating step, and the benzene separating step between described liquid-phase isomerization unit and the described PX recovery unit.
3. the method one of in the claim 1 and 2 wherein is recycled to the described second isomerization product materials flow described first fractionating step, one or more benzene separating step (when existing) and described PX and reclaims one or more in the unit.
4. each method during aforesaid right requires, wherein at least a portion with the product of described liquid-phase isomerization unit is recycled to described first fractionating step.
5. each method among the claim 2-4, wherein at least a portion with the product of described liquid-phase isomerization unit is recycled at least one benzene separating step.
6. each method during aforesaid right requires, wherein the product with described liquid-phase isomerization unit is recycled to described PX recycling step.
7. each method during aforesaid right requires, wherein said PX recycling step comprises crystalline element.
8. each method during aforesaid right requires, wherein said PX recycling step comprises selective adsorption.
9. each method during aforesaid right requires is if also comprise the fractionation of isomerization product recycle stream to remove the step that is present in the toluene in the described materials flow.
10. each method during aforesaid right requires, the raw material of the wherein said C8+ of comprising aromatic substance comprises the raw material of at least a C8+ of being selected from selectivity toluene disproportionation product, C8+ transalkylated product, C8+ reformate and C8+ toluene disproportionation product.
11. in the equipment of preparation p-Xylol (PX), described equipment comprises first separation column, described first separation column is operated being suitable for the C8+ aromatic stream is separated into the overhead product that comprises dimethylbenzene and comprising under the condition of bottoms product stream of C9+ aromatic substance, described overhead product materials flow is reclaimed the unit fluid with PX and is communicated with, wherein said PX reclaims the unit materials flow of being rich in PX and the materials flow of the poor PX of containing is provided, and improves the conduit that comprises the materials flow that will carry the described poor PX of containing and divides so that allow the part of materials flow of the described poor PX of containing flow to the gas phase isomerization unit and allow another part of materials flow of the described poor PX of containing flow to the liquid-phase isomerization unit.
12. the equipment of claim 11, wherein the liquid-phase isomerization product circulation that described liquid-phase isomerization unit fluid is communicated with so that is provided to described first separation column and/or reclaims the unit to described PX.
13. the equipment of claim 11, wherein said PX reclaim the unit and are selected from least a in crystallizer and the adsorptivity separator.
14. the equipment of claim 11, comprise that also at least one is at other separation column of the described first separation column upstream, wherein said at least one other separation column under being suitable for the condition of from the materials flow that comprises dimethylbenzene, removing benzene or from the materials flow that comprises dimethylbenzene, removing toluene or both of these case, operate and wherein said at least one other separation column in the described first separation column upstream.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US40809710P | 2010-10-29 | 2010-10-29 | |
| US61/408,097 | 2010-10-29 | ||
| EP10192327.4 | 2010-11-24 | ||
| EP10192327 | 2010-11-24 | ||
| PCT/US2011/057240 WO2012058108A2 (en) | 2010-10-29 | 2011-10-21 | Process for the production of paraxylene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103201240A true CN103201240A (en) | 2013-07-10 |
| CN103201240B CN103201240B (en) | 2015-11-25 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201180052392.0A Active CN103201240B (en) | 2010-10-29 | 2011-10-21 | The preparation method of p-Xylol |
Country Status (6)
| Country | Link |
|---|---|
| EP (1) | EP2632880A4 (en) |
| JP (1) | JP5876883B2 (en) |
| KR (2) | KR101947247B1 (en) |
| CN (1) | CN103201240B (en) |
| SG (2) | SG189261A1 (en) |
| WO (1) | WO2012058108A2 (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105579424A (en) * | 2013-07-31 | 2016-05-11 | 环球油品公司 | Processes and systems for separating streams to provide a transalkylation feed stream in an aromatics complex |
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| KR101530139B1 (en) * | 2010-10-29 | 2015-06-18 | 엑손모빌 케미칼 패턴츠 인코포레이티드 | Process for the production of purified xylene isomers |
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| US9517980B2 (en) | 2015-04-30 | 2016-12-13 | Exxonmobil Chemical Patents Inc. | Process and apparatus for the production of para-xylene |
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| US20200354293A1 (en) * | 2019-05-10 | 2020-11-12 | Uop Llc | Process and apparatus for dual feed para-xylene separation |
| WO2023244389A1 (en) * | 2022-06-14 | 2023-12-21 | Exxonmobil Chemical Patents Inc. | Production of p-xylene by liquid-phase isomerization in the presence of c9+ aromatic hydrocarbons and separation thereof |
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- 2011-10-21 JP JP2013536681A patent/JP5876883B2/en active Active
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105579424A (en) * | 2013-07-31 | 2016-05-11 | 环球油品公司 | Processes and systems for separating streams to provide a transalkylation feed stream in an aromatics complex |
| CN105579424B (en) * | 2013-07-31 | 2019-03-08 | 环球油品公司 | For separating stream to provide the method and system of the exchange feeding flow of the alkyl in aromatic compounds combined unit |
| CN106488897A (en) * | 2014-06-30 | 2017-03-08 | 埃克森美孚化学专利公司 | The method preparing dimethylbenzene |
| CN107531590A (en) * | 2015-04-30 | 2018-01-02 | 埃克森美孚化学专利公司 | Method and apparatus for producing paraxylene |
| CN107531590B (en) * | 2015-04-30 | 2020-11-06 | 埃克森美孚化学专利公司 | Process and apparatus for producing paraxylene |
| CN108484889A (en) * | 2018-01-23 | 2018-09-04 | 浙江省现代纺织工业研究院 | A kind of preparation method of differential paraxylene |
| CN110283033A (en) * | 2019-06-28 | 2019-09-27 | 中国石油天然气集团有限公司 | Multi-region association control microcirculation high capacity absorption crystallization coupling aromatics production method and system |
| CN110283033B (en) * | 2019-06-28 | 2021-11-02 | 中国石油天然气集团有限公司 | Multi-region coordinated control microcirculation high-capacity adsorption crystallization coupled aromatic hydrocarbon production method and system |
| CN112573987A (en) * | 2019-09-29 | 2021-03-30 | 中国石油化工股份有限公司 | From C containing ethylbenzene8Method for producing paraxylene and ethylbenzene by aromatic hydrocarbon |
| CN112573987B (en) * | 2019-09-29 | 2024-02-09 | 中国石油化工股份有限公司 | From C containing ethylbenzene 8 Method for producing paraxylene and ethylbenzene from aromatic hydrocarbon |
Also Published As
| Publication number | Publication date |
|---|---|
| SG10201508779UA (en) | 2015-11-27 |
| WO2012058108A3 (en) | 2012-07-12 |
| KR20160030327A (en) | 2016-03-16 |
| WO2012058108A2 (en) | 2012-05-03 |
| JP2014501704A (en) | 2014-01-23 |
| CN103201240B (en) | 2015-11-25 |
| SG189261A1 (en) | 2013-05-31 |
| JP5876883B2 (en) | 2016-03-02 |
| EP2632880A4 (en) | 2016-01-27 |
| KR20130056357A (en) | 2013-05-29 |
| EP2632880A2 (en) | 2013-09-04 |
| KR101947247B1 (en) | 2019-02-12 |
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