CN105837394B - A kind of method of purification of high-purity 1,2,3-trimethylbenzene - Google Patents
A kind of method of purification of high-purity 1,2,3-trimethylbenzene Download PDFInfo
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- CN105837394B CN105837394B CN201610209495.8A CN201610209495A CN105837394B CN 105837394 B CN105837394 B CN 105837394B CN 201610209495 A CN201610209495 A CN 201610209495A CN 105837394 B CN105837394 B CN 105837394B
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- C—CHEMISTRY; METALLURGY
- 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
- C07C7/04—Purification; Separation; Use of additives by distillation
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
- C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
Abstract
The present invention provides a kind of method of purification of high-purity 1,2,3-trimethylbenzene, including pretreatment of raw material and extracting rectifying two parts, using process integration differential pressure heat Coupling Design.Pre- weight-removing column T2 tower top is pre- lightness-removing column T1 tower bottom heating, and extractive distillation column T3 tower top is pre- weight-removing column T2 tower bottom heating, and solvent recovery tower T4 tower top is extractive distillation column T3 tower bottom heating, solvent recovery tower T4 steam heating；Pre- lightness-removing column T1, pre- weight-removing column T2 and extractive distillation column T3 tower are provided with reboiler.Process uses mass ratio to make extractant for sulfolane/dimethyl sulfoxide of 10~5:1, is designed using integrated differential pressure thermal coupling extracting rectifying, reduces equipment investment and operating cost, while improving the yield of 1,2,3-trimethylbenzene.The system can be effectively from mixing C9High-purity 1,2,3-trimethylbenzene is extracted in aromatic solvent naphtha, makes product purity >=99wt%, yield is between 92~95%.
Description
Technical field
The present invention relates to a kind of method of purification of high-purity 1,2,3-trimethylbenzene, more particularly to it is a kind of from mixing C9In aromatic solvent naphtha
The method for purifying 1,2,3-trimethylbenzene.
Background technique
1,2,3-trimethylbenzene is producing aniline dyes, benzene-1,2,3-tricarboxylic acid as a kind of important medicine, chemical industry intermediate,
Musk tibetene is synthesized, the pharmaceutical preparations such as blood platelet anticoagulant tool is produced and has been widely used.Mix C9Aromatic hydrocarbons is mainly from oil refining
Factory's reformer, wherein a large amount of 1,2,3-trimethylbenzenes contained are used as the blend component of gasoline to be burned off mostly, serious waste of resources.It adopts
The 1,2,3-trimethylbenzene product that high-purity is obtained with reasonable isolation technics, has great significance to its processing and utilization, and can
Create huge economical, societal benefits.The boiling point that its separation difficult point essentially consists in the components such as 1,2,3-trimethylbenzene and indane at present differs
Very little is difficult to obtain high-purity 1,2,3-trimethylbenzene product using conventional distillation.
1900034 A of application for a patent for invention publication number CN is " from mixing C9The side of 1,2,3-trimethylbenzene is purified in aromatic solvent naphtha
Method " is using alkylation transformation approach separating-purifying 1,2,3-trimethylbenzene.It can get company's front three of 92% or more mass fraction using this method
Benzaldehyde product, but the method complex technical process, less economical, catalyst life is short, is not easy to industrialized production.
" from the heavy aromatics side of separating-purifying 1,2,3-trimethylbenzene and indane 101704706 A of application for a patent for invention publication number CN
Method " obtains the 1,2,3-trimethylbenzene product that mass fraction is not less than 95%, but this method using adsorbing separation combination precise distillation method
Process is cumbersome, and catalyst activity is low, the service life is short, at high cost, and industrialized production is difficult.
It is therefore proposed that a kind of product purity is high, process energy consumption is small, and operating procedure is simple, is easy to industrialized 1,2,3-trimethylbenzene
Process for separating and purifying is necessary.
Summary of the invention
The purpose of the present invention is to provide one kind from mixing C9The producer of high-purity 1,2,3-trimethylbenzene is obtained in aromatic solvent naphtha
Method, process use mass ratio to make extractant for sulfolane/dimethyl sulfoxide of 10~5:1, are extracted using integrated differential pressure thermal coupling
Distillation design is taken, reduces equipment investment and operating cost, while improving the yield of 1,2,3-trimethylbenzene.The system can be effectively from mixed
Close C9High-purity 1,2,3-trimethylbenzene is extracted in aromatic solvent naphtha, makes product purity >=99wt%, yield is between 92~95%.
Technical solution of the invention is as follows:
A kind of method of purification of high-purity 1,2,3-trimethylbenzene, including pretreatment of raw material and extracting rectifying two parts, using process collection
At differential pressure heat Coupling Design.
The integrated differential pressure heat Coupling Design process are as follows: pre- weight-removing column tower top is pre- lightness-removing column tower bottom heating, extracting rectifying
Column overhead is pre- weight-removing column tower bottom heating, and solvent recovery column overhead is extractive distillation column tower bottom heating, solvent recovery tower steam
Heat supply；Pre- lightness-removing column, pre- weight-removing column and extractive distillation column are provided with reboiler.
Raw material pretreatment portion includes pre- lightness-removing column and pre- weight-removing column, and extracting rectifying part includes extractive distillation column and solvent
Recovery tower；Than the component of 1,2,3-trimethylbenzene low boiling point in pre- lightness-removing column removing raw material；Pre- weight-removing column removes the group higher than indane boiling point
Point；Extractive distillation column increases the relative volatility of 1,2,3-trimethylbenzene and indane, removes indane, obtains 1,2,3-trimethylbenzene product；Solvent returns
It receives tower and recycles extractant.
Operating method are as follows: mixing C to be purified9Raw material enters the middle part of pre- lightness-removing column, sloughs most light component simultaneously
A small amount of 1,2,3-trimethylbenzene is lost, pre- lightness-removing column reboiler is condensed using pre- weight-removing column top gaseous phase logistics as heat source, through pre- de-
Overhead condensation liquid after light tower reboiler heat exchange returns to pre- weight-removing column part as reflux, and part produces；Pre- lightness-removing column tower reactor is de-
C is mixed after light9Logistics enters the middle part of pre- weight-removing column, sloughs most heavy constituent and loses a small amount of 1,2,3-trimethylbenzene, pre- de-
Weight tower reboiler condenses the tower top as heat source, after the heat exchange of pre- weight-removing column reboiler using extractive distillation column top gaseous phase logistics
Condensate liquid returns to extracting rectifying tower section as reflux, and part produces；The 1,2,3-trimethylbenzene logistics of pre- weight-removing column tower top concentration enters
In the middle part of extractive distillation column, circulation solvent stream is added on extractive distillation column top, removes indane, extractive distillation column through extracting rectifying
Tower top obtains high-purity 1,2,3-trimethylbenzene product, and extracting rectifying tower reboiler is condensed using solvent recovery tower top gaseous phase logistics as heat
Source, the overhead condensation liquid after the heat exchange of extracting rectifying tower reboiler return to solvent recovery tower section as reflux, and part produces；Extraction
The heavy constituents logistics such as agent and indane is taken to enter solvent recovery tower, solvent recovery column overhead obtains indane and heavy constituent, and tower bottom obtains
The extractant of recycling；The extractant of recycling returns to extractive distillation column after mixing with the fresh extractant of supplement.
The pre- lightness-removing column tower top 5~30KPa of operating pressure, 80~140 DEG C of tower reactor operation temperature, number of theoretical plate 30~
150, feed entrance point is theoretical plate 10~70, reflux ratio 20~70.
The pre- weight-removing column tower top 20~90KPa of operating pressure, 120~190 DEG C of tower reactor operation temperature, number of theoretical plate 40~
150, feed entrance point is theoretical plate 20~80, reflux ratio 4~40.
The extracting rectifying column overhead 70~100KPa of operating pressure, 220~280 DEG C of bottom temperature, number of theoretical plate 100~
200, feedstock position is theoretical plate 40~120, and extractant feed position is theoretical plate 5~30, and solvent is than 5~15, reflux
Than 3~12.
The solvent recovery column overhead 70~100KPa of operating pressure, 260~300 DEG C of bottom temperature, number of theoretical plate 30~
100, feed entrance point is theoretical plate 8~32, reflux ratio 5~20.
The present invention reduces mixing C by carrying out decompression step rectifying to system9Mixture in aromatic solvent naphtha material liquid
Boiling point, increase the relative volatility between each component, reduce separating difficulty, improve product yield；Process is using poor
Pressure thermal coupling rectifying also reduces the energy consumption of process.Accurate pressure difference thermal coupling extracting rectifying of the invention is relative to traditional rectifying
Separating technology, process total energy consumption reduce about 30~50%.
The invention has the advantages that
(1) it is difficult to reduce separation by decompression step rectifying using accurate pressure difference thermal coupling extracting rectifying design by the present invention
Degree and energy consumption.
(2) present invention proposes a kind of novel extraction rectification technique, using novel sulfolane/dimethyl sulfoxide (quality
Than 10~5:1) mixed extractant is done, it can be further improved the purity (>=99wt%) of 1,2,3-trimethylbenzene, decompression operation is further
Improve the yield of 1,2,3-trimethylbenzene (between 92~95%).
(3) present invention uses Precision Integrated pressure difference thermal coupling step reduced pressure distillation process, and energy consumption can be greatly lowered, compared with
Traditional rectification process saving energy 30~50%.
Detailed description of the invention
Fig. 1 is a kind of flow diagram of high-purity 1,2,3-trimethylbenzene method of purification of the present invention.
Wherein:
Illustrate: the pre- lightness-removing column of T1；The pre- weight-removing column of T2；T3 extractive distillation column；T4 solvent recovery tower；The pre- lightness-removing column of E1 boils again
Device；The pre- weight-removing column reboiler of E2；E3 extracting rectifying tower reboiler；1 mixing C to be purified9Raw material；The light component stream of 2 removings；
3 de- light rear mixing C9Logistics；4 pre- weight-removing column top gaseous phase logistics；5 overhead condensation liquid after the heat exchange of pre- lightness-removing column reboiler；6
The 1,2,3-trimethylbenzene logistics of concentration；The heavy constituent logistics of 7 removings；8 extractive distillation column top gaseous phase logistics；9 boil again through pre- weight-removing column
Overhead condensation liquid after device heat exchange；10 circulation solvent streams；11 high-purity 1,2,3-trimethylbenzene products；The heavy constituents such as 12 extractants and indane
Logistics；13 solvent recovery tower top gaseous phase logistics；14 overhead condensation liquid after the heat exchange of extracting rectifying tower reboiler；15 indanes and
Heavy constituent logistics；The extractant of 16 recycling；The fresh extractant of 17 supplements.
Specific embodiment
With reference to the attached drawing in the embodiment of the present invention, technical solution in the embodiment of the present invention carries out clear, complete
Ground description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.
One kind from mixing C9The process of high-purity 1,2,3-trimethylbenzene, including pretreatment of raw material and extraction essence are extracted in aromatic solvent naphtha
Two parts are evaporated, pre- lightness-removing column T1, pre- weight-removing column T2, extractive distillation column T3 and solvent recovery tower T4 are related to.Wherein pretreatment of raw material
Part includes pre- lightness-removing column T1 and pre- weight-removing column T2, and extracting rectifying part includes extractive distillation column T3 and solvent recovery tower T4.In advance
The purpose of lightness-removing column T1 is the component removed in raw material than 1,2,3-trimethylbenzene low boiling point；The purpose of pre- weight-removing column T2 is that indane is compared in removing
The high component of boiling point；The purpose of extractive distillation column T3 is to increase the relative volatility of 1,2,3-trimethylbenzene and indane, removes indane, obtains
1,2,3-trimethylbenzene product；The purpose of solvent recovery tower T4 is recycling extractant.
The device of the invention is as shown in Figure 1:
Mixing C to be purified9It is connect in the middle part of the feeding line of raw material 1 and pre- lightness-removing column T1, the light component stream 2 of removing
Pipeline is connected with pre- lightness-removing column T1 tower top, takes off light rear mixing C9It is connect in the middle part of the pipeline of logistics 3 and pre- weight-removing column T2, it is pre- de- light
Pre- lightness-removing column reboiler E1 is arranged in tower T1 tower reactor；The pipeline of pre- weight-removing column top gaseous phase logistics 4 and pre- lightness-removing column reboiler E1 phase
The pipeline of connection, the overhead condensation liquid 5 after the heat exchange of pre- lightness-removing column reboiler is connected with pre- weight-removing column T2 tower top, through pre- de- weight
The pipeline of the 1,2,3-trimethylbenzene logistics 6 of tower T2 concentration is connected with extractive distillation column T3, the weight of pre- weight-removing column T2 tower reactor connection removing
Pre- weight-removing column reboiler E2 is arranged in the pipeline of component streams 7, pre- weight-removing column T2 tower reactor；Extractive distillation column top gaseous phase logistics 8
Pipeline is connected with pre- weight-removing column reboiler E2, the pipeline of the overhead condensation liquid 9 after the heat exchange of pre- weight-removing column reboiler and extraction
It is connected at the top of rectifying column T3, the pipeline of circulation solvent stream 10 is connected with the top extractive distillation column T3, extractive distillation column T3
Tower top connects the pipeline of high-purity 1,2,3-trimethylbenzene product 11, the pipeline and solvent recovery tower of the heavy constituents such as extractant and indane logistics 12
T4 is connected, and extracting rectifying tower reboiler E3 is arranged in extractive distillation column T3 tower reactor；The pipe of solvent recovery tower top gaseous phase logistics 13
Line is connected with extracting rectifying tower reboiler E3, through extracting rectifying tower reboiler heat exchange after overhead condensation liquid 14 pipeline with it is molten
It is connected at the top of agent recovery tower T4, the pipeline of indane and heavy constituent logistics 15 is connected with solvent recovery tower T4 tower top, the extraction of recycling
The pipeline of agent 16 is taken to be connected with solvent recovery tower T4 tower reactor.
Whole flow process is designed using the pressure difference thermal coupling of process integration precision, i.e., high pressure column overhead provides again to lower pressure column tower reactor
Boiling hot amount had not only reduced the energy consumption of process but also had saved equipment investment, to greatest extent reduce whole flow process equipment investment and
Operating cost.
Pre- weight-removing column T2 tower top is pre- lightness-removing column T1 tower bottom heating, and extractive distillation column T3 tower top is the confession of pre- weight-removing column T2 tower bottom
Heat, solvent recovery tower T4 tower top are extractive distillation column T3 tower bottom heating, solvent recovery tower T4 steam heating.
Material flow is as follows:
Mixing C to be purified9Raw material 1 enters the middle part of pre- lightness-removing column T1, sloughs most light component and loses a small amount of
1,2,3-trimethylbenzene (logistics 2), pre- lightness-removing column reboiler E1 using pre- weight-removing column top gaseous phase logistics 4 condense as heat source, through pre-
Overhead condensation liquid 5 after the heat exchange of lightness-removing column reboiler returns to the pre- part weight-removing column T2 as reflux, and part produces；Pre- lightness-removing column T1
The de- light rear mixing C of tower reactor9Logistics 3 enters the middle part of pre- weight-removing column T2, sloughs most heavy constituent and loses a small amount of company three
Toluene (logistics 7), pre- weight-removing column reboiler E2 are condensed using extractive distillation column top gaseous phase logistics 8 as heat source, through pre- de- weight
Overhead condensation liquid 9 after tower reboiler heat exchange returns to the part extractive distillation column T3 as reflux, and part produces；Pre- weight-removing column T2 tower
The 1,2,3-trimethylbenzene logistics 6 of top concentration enters in the middle part of extractive distillation column T3, and circulation solvent stream 10 adds on the top extractive distillation column T3
Enter, removes indane through extracting rectifying, extractive distillation column T3 tower top obtains high-purity 1,2,3-trimethylbenzene product (logistics 11), extractive distillation column
Reboiler E3 condenses the tower as heat source, after the heat exchange of extracting rectifying tower reboiler using solvent recovery tower top gaseous phase logistics 13
Top condensate liquid 14 returns to the part solvent recovery tower T4 as reflux, and part produces；The heavy constituents such as extractant and indane logistics 12 into
Enter solvent recovery tower T4, solvent recovery tower T4 tower top obtains indane and heavy constituent (logistics 15), the extractant that tower bottom is recycled
(logistics 16) and extractive distillation column T3 is returned to, the fresh extractant of supplement is realized by logistics 17.
The present invention in order to preferably match the heat between each tower, control pre- lightness-removing column T1 tower top operating pressure 5~
30KPa, 80~140 DEG C of tower reactor operation temperature, number of theoretical plate 30~150, feed entrance point 10~70 (theoretical plate), reflux ratio 20~
70；Pre- weight-removing column T2 tower top 20~90KPa of operating pressure, 120~190 DEG C of tower reactor operation temperature, number of theoretical plate 40~150, into
Discharge position 20~80 (theoretical plate), reflux ratio 4~40；Extractive distillation column T3 tower top 70~100KPa of operating pressure, bottom temperature
220~280 DEG C, number of theoretical plate 100~200, feedstock position 40~120 (theoretical plate), extractant feed position 5~30
(theoretical plate), solvent is than 5~15, reflux ratio 3~12；Solvent recovery tower T4 tower top 70~100KPa of operating pressure, bottom temperature
260~300 DEG C, number of theoretical plate 30~100, feed entrance point 8~32 (theoretical plate), reflux ratio 5~20.
Embodiment one:
Feedstock amount is 1000kg/h, and sulfolane/dimethyl sulfoxide mass ratio is 10:1, feed composition such as following table institute
Show:
Process conditions are as follows:
The 1,2,3-trimethylbenzene product purity produced under above-mentioned process conditions is 99.2%, product recovery rate are as follows: 93.9%.
Embodiment two:
Feedstock amount is 1200kg/h, and sulfolane/dimethyl sulfoxide mass ratio is 8:1, and feed composition is as shown in the table:
Process conditions are as follows:
The 1,2,3-trimethylbenzene product purity produced under above-mentioned process conditions is 99.3%, product recovery rate are as follows: 94.4%.
Embodiment three:
Feedstock amount is 1200kg/h, and sulfolane/dimethyl sulfoxide mass ratio is 5:1, and feed composition is as shown in the table:
Process conditions are as follows:
The 1,2,3-trimethylbenzene product purity produced under above-mentioned process conditions is 99.5%, product recovery rate are as follows: 92.8%.
A kind of method of purification for high-purity 1,2,3-trimethylbenzene that the present invention is disclosed and proposed, those skilled in the art can pass through reference
Present disclosure, the appropriate links such as condition route that change are realized, are preferably implemented although method and technology of preparing of the invention has passed through
Example is described, related technical personnel obviously can not depart from the content of present invention, in spirit and scope to as described herein
Methods and techniques route is modified or reconfigures, to realize final technology of preparing.In particular, it should be pointed out that Suo Youxiang
Similar replacement and change is apparent to those skilled in the art, they are considered as being included in essence of the invention
In mind, range and content.
Claims (2)
1. a kind of method of purification of high-purity 1,2,3-trimethylbenzene, it is characterised in that: including pretreatment of raw material and extracting rectifying two parts, adopt
With process integration differential pressure heat Coupling Design；
Wherein, the integrated differential pressure heat Coupling Design process are as follows: pre- weight-removing column tower top is pre- lightness-removing column tower bottom heating, extracting rectifying
Column overhead is pre- weight-removing column tower bottom heating, and solvent recovery column overhead is extractive distillation column tower bottom heating, solvent recovery tower steam
Heat supply；Pre- lightness-removing column, pre- weight-removing column and extractive distillation column are provided with reboiler；
The raw material pretreatment portion includes pre- lightness-removing column and pre- weight-removing column, and extracting rectifying part includes extractive distillation column and solvent
Recovery tower；Than the component of 1,2,3-trimethylbenzene low boiling point in pre- lightness-removing column removing raw material；Pre- weight-removing column removes the group higher than indane boiling point
Point；Extractive distillation column increases the relative volatility of 1,2,3-trimethylbenzene and indane, removes indane, obtains 1,2,3-trimethylbenzene product；Solvent returns
It receives tower and recycles extractant；
Extractant selected by extracting rectifying part is mass ratio 5:1~10:1 sulfolane/dimethyl sulfoxide；
Pre- lightness-removing column tower top 5~30KPa of operating pressure, 80~140 DEG C of tower reactor operation temperature, number of theoretical plate 30~150, feed position
It is set to theoretical plate 10~70, reflux ratio 20~70；
Pre- weight-removing column tower top 20~90KPa of operating pressure, 120~190 DEG C of tower reactor operation temperature, number of theoretical plate 40~150, charging
Position is theoretical plate 20~80, reflux ratio 4~40；
Extracting rectifying column overhead 70~100KPa of operating pressure, 220~280 DEG C of bottom temperature, number of theoretical plate 100~200, raw material
Feed entrance point is theoretical plate 40~120, and extractant feed position is theoretical plate 5~30, and solvent is than 5~15, reflux ratio 3~12；
Solvent recovery column overhead 70~100KPa of operating pressure, 260~300 DEG C of bottom temperature, number of theoretical plate 30~100 is fed
Position is theoretical plate 8~32, reflux ratio 5~20.
2. method according to claim 1, which is characterized in that mixing C to be purified9Raw material enters the middle part of pre- lightness-removing column, takes off
It goes most light component and loses a small amount of 1,2,3-trimethylbenzene, pre- lightness-removing column reboiler is cold using pre- weight-removing column top gaseous phase logistics
Solidifying as heat source, the overhead condensation liquid after the heat exchange of pre- lightness-removing column reboiler returns to pre- weight-removing column part as flowing back, and partially adopts
Out；The de- light rear mixing C of pre- lightness-removing column tower reactor9Logistics enters the middle part of pre- weight-removing column, sloughs most heavy constituent and loses few
The 1,2,3-trimethylbenzene of amount, pre- weight-removing column reboiler are condensed using extractive distillation column top gaseous phase logistics as heat source, through pre- weight-removing column
Overhead condensation liquid after reboiler heat exchange returns to extracting rectifying tower section as reflux, and part produces；Pre- weight-removing column tower top concentration
1,2,3-trimethylbenzene logistics enter in the middle part of extractive distillation column, circulation solvent stream is added on extractive distillation column top, through extracting rectifying
Indane is removed, extracting rectifying column overhead obtains high-purity 1,2,3-trimethylbenzene product, and extracting rectifying tower reboiler utilizes solvent recovery tower tower
It pushes up gaseous stream condensation and is used as heat source, the overhead condensation liquid after the heat exchange of extracting rectifying tower reboiler returns to solvent recovery tower section
As reflux, part is produced；The heavy constituents logistics such as extractant and indane enters solvent recovery tower, and solvent recovery column overhead obtains indenes
Full and heavy constituent, the extractant that tower bottom is recycled；The extractant of recycling returns to extraction after mixing with the fresh extractant of supplement
Rectifying column.
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| US10287512B2 (en) * | 2017-06-29 | 2019-05-14 | Uop Llc | Process and apparatus for desorbent recovery |
| CN107501049A (en) * | 2017-09-19 | 2017-12-22 | 天津大学 | A kind of extracting rectifying removing low-temp methanol washes the device and method of sulfide in recycle methanol |
| CN111202999B (en) * | 2020-02-10 | 2021-12-24 | 南京炼油厂有限责任公司 | Rectification device and method for extracting high-purity mesitylene product from oil generated by isomerization reaction of trimethylbenzene |
| CN111348998A (en) * | 2020-04-17 | 2020-06-30 | 湖北三里枫香科技有限公司 | Energy-saving environment-friendly acetic acid production process |
| CN112194553B (en) * | 2020-11-04 | 2023-04-28 | 成都宏鼎石化有限公司 | Method and device for separating mixture of carbon nine aromatic hydrocarbon |
| CN112457879A (en) * | 2020-11-12 | 2021-03-09 | 河北中化鑫宝化工科技有限公司 | Method and device for extracting high-purity indene from coal tar indene fraction |
| CN114292155A (en) * | 2021-12-31 | 2022-04-08 | 黄河三角洲京博化工研究院有限公司 | Method for thermally coupling and purifying mesitylene |
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