CN107427735A - Improve the top partition wall tower technology of dimethylbenzene processing - Google Patents
Improve the top partition wall tower technology of dimethylbenzene processing Download PDFInfo
- Publication number
- CN107427735A CN107427735A CN201680022324.2A CN201680022324A CN107427735A CN 107427735 A CN107427735 A CN 107427735A CN 201680022324 A CN201680022324 A CN 201680022324A CN 107427735 A CN107427735 A CN 107427735A
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- CN
- China
- Prior art keywords
- raw material
- method described
- xylene mixture
- xylene
- paraxylene
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/141—Fractional distillation or use of a fractionation or rectification column where at least one distillation column contains at least one dividing wall
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C15/00—Cyclic hydrocarbons containing only six-membered aromatic rings as cyclic parts
- C07C15/02—Monocyclic hydrocarbons
- C07C15/067—C8H10 hydrocarbons
- C07C15/08—Xylenes
Abstract
Top partition wall destilling tower (TDWC) is disclosed, it separates plurality of raw materials to produce with the different xylene mixtures formed from TDWC top.The product that TDWC allows to have the xylene mixture of different compositions is separated and fed to the diverse location in paraxylene recovery section.By the either side of different feedstock to TDWC, this depends on the composition of raw material or the difference of isomer ratio.By the xylene mixture that the both sides of tower produce at top by with isomer ratio different from each other, but the isomer ratio is identical with the isomer ratio of their corresponding raw materials.
Description
The cross reference of related application
The application requires the U.S. Provisional Patent Application No. 62/ of No. 17 submissions in 2 months 2015 according to 35U.S.C. § 119 (e)
117,151 rights and interests, it is herein incorporated by reference in its entirety as illustrating completely herein by quoting.
Background
Xylene isomer --- ortho-xylene (OX), meta-xylene (MX) and paraxylene (PX) and ethylbenzene (EB) come
From reforming process or the C8 aromatic compounds of other petrochemical process.Purified individual xylene product is used as on a large scale
The intermediate of industrial solvent and many products.Most important isomers PX is used to produce terephthalic acid (TPA) (TPA) and terephthaldehyde
Dimethyl phthalate (DMT), it is used to produce fiber, film and PET (PET) bottle.In such applications, it is necessary to
High-purity (>99.7%)PX.Greatly improved for high-purity PX demand in the several years in past, to meet the market of rapid growth.
Aromatic compounds and the traditional raw material of paraxylene production are catalytic reformate or drippolene (pygas).Catalysis
Cracking, or fluid catalytic cracking (FCC), including various variants such as DCC (DCC), high severity FCC (HS-
FCC), residue FCC (RFCC), be produce fuel, low-carbon alkene and similar enrichment C6 to C10+ aromatic compounds stream (referred to as
Catalytic naphtha (catalytic naphtha or cat naphtha)) another well-known method.In general, balance
The product of xylene mixture is distributed as about 40% MX, 20% PX, 20% OX and 20% EB.This tittle alterable ± 10%.
Formed in the presence of the other dimethylbenzene for causing xylene mixture content different from typical balance xylene mixture
Technology.In the presence of known technology, i.e. aromatisation, to obtain olefin stream and produce benzene, toluene and dimethylbenzene (BTX).Aromatisation
Any olefin component in the range of C4-C8 will be produced aromatic compounds as charging.The accessory substance of aromatisation is lightweight chain
Alkane and LPG waste gas.Aromatization products have the ethyl-benzene level lower than typical balance xylene mixture.
It is known that dimethylbenzene is produced by toluene and/or methylating for benzene, such as carry out toluene through catalyst using methanol
Methylate.Raw material can be mixture, drippolene raw material or the reformate raw material of toluene, benzene, toluene and benzene.Methylate has
Have than the typical balance higher paraxylene content of xylene mixture and/or lower ethyl-benzene level.
Deposit its using benzene, toluene, C9-C10 aromatic compounds or combinations thereof as raw material known in the industry
Its dimethylbenzene forms technology, for example, benzene/C9-C10 transalkylations, toluene/C9-C10 transalkylations, benzene/methylbenzene/C9-C10 alkane
Group-transfer, toluene disproportionation (TDP) and selective toluene disproportionation (STDP), it will produce different product streams, and the product stream has
Than the typical balance higher paraxylene content of xylene mixture and/or lower ethyl-benzene level.
Above-mentioned all dimethylbenzene form technology and can also produced with different C9 or the more product of heavy constituent content.
In typical paraxylene production combined unit (complex), C8+ aromatic compounds is flowed into material to C8/C9
In knockout tower, the knockout tower is sometimes referred to as benzenol hydrorefining.The logistics of C8 aromatic compounds separates in tower top from benzenol hydrorefining, and is sent
Toward downstream paraxylene recovery unit, produced for paraxylene.If exist it is multiple enter material source, feed C8+ aromatic compounds
Stream can have different ethylbenzene, paraxylene, non-aromatic compound and/or C9+ contents.A benzenol hydrorefining is only existed wherein
Typical paraxylene combined unit in, all these raw materials are mixed and are subsequently isolated with produce have it is a kind of single
The xylene mixture of composition.If desired multiple dimethylbenzene mixing of the production with different ethylbenzene and/or paraxylene content
Logistics, then using multiple benzenol hydrorefinings, this can increase the extra fund cost of technique.
But keep the different ethylbenzene being present in raw material and/or paraxylene content or ethylbenzene/paraxylene ratio
Benefit be present.For example, ethylbenzene is the C8 isomers for being most difficult to remove from the extract in paraxylene purification unit via absorption.
The concentration of ethylbenzene has big influence for the quantity for preparing the bed in the purification zone needed for high-purity paraxylene.Although tool
Have it is single enter stream be convenient, mixed feed stream needs some theory stages to be existed to regenerate before stream mixing is entered
Separation.Similarly, in the paraxylene purification unit by crystallization, it is advantageous that separation and concentration is to two from balance raw material
The raw material of toluene, such as STDP raw materials or the raw material for carrying out self-selectively toluene methylation unit.The charging of concentration can be sent to production
Thing purifies, wherein cooling down almost effortless, and balancing raw material needs to carry out depth cooling in very low temperatures, and this will be notable
Save cooling power.
The undisclosed dimethylbenzene mixing for being used for separation of the production with different compositions in single destilling tower of present system
The practical methods of logistics.
General introduction
In the present invention, separation plurality of raw materials is disclosed to produce the top partition wall with the different xylene mixtures formed
Destilling tower (TDWC).Xylene feedstock is produced by TDWC top.By using TDWC, may separate out with different compositions and different
The xylene mixture of structure body ratio, and feed to the diverse location in paraxylene recovery section.
In various embodiments, the TDWC segregative lines for producing xylene mixture by different feeds source are disclosed
System.TDWC systems include the destilling tower with vertical partition wall, and the vertical partition wall will be split into two halves at the top of destilling tower.Can
By the either side of different feedstock to TDWC, this depends on the composition of raw material or the difference of isomer ratio.From TDWC's
Both sides have different compositions in xylene mixture caused by top, but are produced and collectively constituted in TDWC bottom using TDWC
Heavy product (heavy product).Xylene mixture includes the isomer ratio identical of raw material corresponding with them
Isomer ratio.
The feature of the disclosure has rather broadly been outlined above, it is described below to be better understood.Hereinafter
The additional features and advantage of the disclosure will be described, it forms claimed subject matter.
Brief description
In order to be more fully understood from the disclosure and its advantage, referring now to the attached of the specific embodiment together with the description disclosure
Scheme the following description considered together, wherein：
Fig. 1 is represented according to the process program of embodiment of the present invention, its be used for TDWC designs with will balance xylene feedstock with
It is enriched with the raw material separation of paraxylene.
It is described in detail
In the following description, some details, such as specific raw material, amount, temperature etc. are elaborated, to provide for being disclosed herein
Embodiment of the present invention thorough explanation.But those skilled in the art will be apparent that the disclosure can not
Put into practice using such detail.In many cases, details on such consideration etc. has been ignored, because without this
Class details obtains the complete understanding for the disclosure, and such details is in the technical ability scope of person of ordinary skill in the relevant
It is interior.
Referring now to Figure 1, it illustrates be used to balance xylene feedstock with being enriched with paraxylene for TDWC 12
The process program 12 of raw material separation.The process planning of claimed invention had into high ethyl-benzene level with for separation
(original of paraxylene is enriched with Deng the balance C8A+ raw materials of C9+ contents and the STDP C8A+ raw materials with low ethyl benzene and C9+ contents
Material).
Fig. 1 process program 10 includes TDWC 12.The TDWC 12 includes the first side 16 and the second side 18.Raw material will be balanced
14 are sent to TDWC 12 the first side 16 and the raw material 20 for being enriched with paraxylene are sent into the second side 18.Vertical partition wall 22 will
TDWC 12 top is split into two halves (that is, the first side 16 and the second side 18).At TDWC 12 top, the first side 16 and condensed system
System 24 is connected and the second side 18 is connected with condenser system 26.Each condenser system 24 and 26 include condenser, receiver, reflux pump and
Equipment needed for other.
Future, the C8 vapor fractions 25 of self-balancing raw material 14 were fed to condenser system 24, and self enrichment paraxylene in future
The C8 vapor fractions 27 of raw material 20 feed to condenser system 26, wherein C8 vapor fractions 25 and 27 and are condensed, cool down and receive respectively
Collection is in the receiver of condenser system 24 and 26.Reception by liquid paraxylene mixture 28 via reflux pump from condenser system 24
Pumped out in device, and liquid paraxylene mixture 30 is pumped out from the receiver of condenser system 26 via reflux pump.By a part
Liquid paraxylene mixture 28 returns to the top of the first side 16 as backflow, and remaining liquid paraxylene mixture 28 is made
Taken out for the first xylene mixture 29, for further being handled in the first paraxylene recovery unit.Similarly, by one
Liquid separation body xylene mixture 30 returns to the top of the second side 18 as backflow, and by remaining liquid paraxylene mixture 30
Taken out as the second xylene mixture 31, for further being handled in the second paraxylene recovery unit.Therefore, leave
First and second xylene mixtures 29 and 31 at TDWC 12 top keep original in its corresponding charging in C8 cuts
Isomer ratio.Bottom of towe output of the heavy product 32 collectively constituted from TDWC 12.
In some embodiments, can also be by extra charging streaming toward the either side of tower, this is depending on consolidating in raw material
There is isomer ratio.For example, the ethylbenzene xylene mixture of the reduction from xylene isomerization unit can be sent to balance into
Expect side.Can future self-selectively toluene methylation unit the xylene mixture of enrichment paraxylene be sent to STDP feed sides.
In some embodiments of the present invention, raw material can be separated according to non-aromatic compound content or C9+ contents.
Charging with different C9+ contents can be fed into TDWC 12 in higher or lower height, this depend on into
The source of material.The height that optimization charging enters in TDWC 12 reduces energy requirement.
The general aspect of the present invention is related to following methods：It is used to reduce money in using still-process of the top every tower
Golden cost and running cost, the number of packages for reducing equipment, to obtain required effect.
From described above, those skilled in the art can be readily determined the required characteristic of the disclosure, and not inclined
In the case of from its spirit and scope, it can make various changes and modifications so that the disclosure is adapted to various uses and condition.On
The embodiment of text description only represents exemplary and is not considered as limitation the scope of the present disclosure, and the scope is following
Defined in claims.
Claims (16)
1. a kind of method that two kinds of xylene mixtures are produced by top dividing wall column, methods described include：
By the first feedstock to the first side of the top dividing wall column；
By the second feedstock to the second side of the top dividing wall column；
The first xylene mixture is separated from first raw material via the top dividing wall column, and from second raw material
The second xylene mixture of middle separation, wherein the composition of first xylene mixture and second xylene mixture
Composition is different；With
Wherein described top next door tower is included from the top of the top dividing wall column towards the bottom of the top dividing wall column
The partition wall of portion's extension.
2. the method described in claim 1, wherein first raw material includes balance raw material and second raw material includes enrichment
The raw material of paraxylene.
3. the method described in claim 1, wherein first raw material includes the balance C8A+ raw materials with high ethyl-benzene level, and
Second raw material includes medium C9+ contents and the STDP C8A+ raw materials with low ethyl benzene and C9+ contents.
4. the method described in claim 1, wherein first raw material and second raw material are separated according to ethyl-benzene level.
5. the method described in claim 1, wherein first raw material and second raw material are carried out according to paraxylene content
Separation.
6. the method described in claim 1, wherein first raw material and second raw material are according to ethylbenzene：The ratio of paraxylene
Rate is separated.
7. the method described in claim 1, wherein first raw material and second raw material are according to non-aromatic compound content
Separated.
8. the method described in claim 1, wherein first raw material and second raw material are separated according to C9+ contents.
9. the method described in claim 1, wherein first raw material includes reformate or drippolene.
10. the method described in claim 1, wherein second raw material is included from aromatisation unit, transalkylation, two
The charging of toluene isomerization unit or non-selective toluene methylation unit.
11. the method described in claim 1, wherein first raw material, which includes, comes from STDP units or selective toluene methylation
The charging of unit.
12. the method described in claim 1, further comprise feeding first xylene mixture to the first condenser system
In to form the first condensation xylene mixture, and second xylene mixture is fed into the second condenser system with shape
Into the second condensation xylene mixture.
13. the method described in claim 12, further comprises：
The Part I of described first condensation xylene mixture is fed to the first side of the top dividing wall column, and by institute
The Part II for stating the first condensation xylene mixture is fed to the first paraxylene recovery unit；With
The Part I of described second condensation xylene mixture is fed to the second side of the top dividing wall column, and by institute
The Part II for stating the second condensation xylene mixture is fed to the second paraxylene recovery unit.
14. the method described in claim 1, wherein：
First xylene mixture includes the isomer ratio identical isomer ratio with first raw material；With
Second xylene mixture includes the isomer ratio identical isomer ratio with second raw material.
15. the method described in claim 2, further comprise the ethylbenzene dimethylbenzene of the reduction from xylene isomerization unit
Mixture is fed to the first side of the top dividing wall column.
16. the method described in claim 2, further comprise the enrichment paraxylene of self-selectively toluene methylation unit in future
Mixture feed to the second side of the top dividing wall column.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US201562117151P | 2015-02-17 | 2015-02-17 | |
| US62/117151 | 2015-02-17 | ||
| PCT/US2016/018324 WO2016134055A1 (en) | 2015-02-17 | 2016-02-17 | Top dividing wall column technology to improve processing of xylenes |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107427735A true CN107427735A (en) | 2017-12-01 |
| CN107427735B CN107427735B (en) | 2020-08-11 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201680022324.2A Active CN107427735B (en) | 2015-02-17 | 2016-02-17 | Top divided wall column technology for improved xylene processing |
Country Status (3)
| Country | Link |
|---|---|
| KR (1) | KR102486214B1 (en) |
| CN (1) | CN107427735B (en) |
| WO (1) | WO2016134055A1 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9517980B2 (en) | 2015-04-30 | 2016-12-13 | Exxonmobil Chemical Patents Inc. | Process and apparatus for the production of para-xylene |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1723065A (en) * | 2002-12-12 | 2006-01-18 | 巴斯福股份公司 | Extractive distillation |
| CN101198573A (en) * | 2005-06-15 | 2008-06-11 | 环球油品公司 | Process for making xylene isomer using a deheptanizer with a side draw recycle |
| US20120103013A1 (en) * | 2010-10-28 | 2012-05-03 | Uop Llc | Vapor and liquid flow control in a dividing wall fractional distillation column |
| US20140231238A1 (en) * | 2013-02-21 | 2014-08-21 | Gtc Technology Us Llc | Separation processes using divided columns |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8631935B2 (en) * | 2009-06-03 | 2014-01-21 | Medline Industries, Inc. | Catheter tray, packaging system, and associated methods |
| US7956157B2 (en) * | 2008-12-31 | 2011-06-07 | Fina Technology, Inc. | Processes using dividing wall distillation column |
-
2016
- 2016-02-17 KR KR1020177025960A patent/KR102486214B1/en active IP Right Grant
- 2016-02-17 CN CN201680022324.2A patent/CN107427735B/en active Active
- 2016-02-17 WO PCT/US2016/018324 patent/WO2016134055A1/en active Application Filing
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1723065A (en) * | 2002-12-12 | 2006-01-18 | 巴斯福股份公司 | Extractive distillation |
| CN101198573A (en) * | 2005-06-15 | 2008-06-11 | 环球油品公司 | Process for making xylene isomer using a deheptanizer with a side draw recycle |
| US20120103013A1 (en) * | 2010-10-28 | 2012-05-03 | Uop Llc | Vapor and liquid flow control in a dividing wall fractional distillation column |
| US20140231238A1 (en) * | 2013-02-21 | 2014-08-21 | Gtc Technology Us Llc | Separation processes using divided columns |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107427735B (en) | 2020-08-11 |
| KR20170117551A (en) | 2017-10-23 |
| WO2016134055A1 (en) | 2016-08-25 |
| KR102486214B1 (en) | 2023-01-06 |
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Address after: Texas, USA Patentee after: Sulzer technologies USA Address before: Texas, USA Patentee before: GTC TECHNOLOGY US LLC |
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Effective date of registration: 20210510 Address after: Winterthur Switzerland Patentee after: SULZER MANAGEMENT AG Address before: Texas, USA Patentee before: Sulzer technologies USA |