CN106631668B - Ethylbenzene separation method and ethylbenzene manufacturing processes and the device for producing ethylbenzene and the method using device production ethylbenzene - Google Patents
Ethylbenzene separation method and ethylbenzene manufacturing processes and the device for producing ethylbenzene and the method using device production ethylbenzene Download PDFInfo
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Abstract
The invention discloses a kind of ethylbenzene separation methods, this method includes separating the mixture containing benzene, ethylbenzene and more ethylbenzene in divided-wall distillation column, obtain ethylbenzene, wherein the feed zone of the bulkhead section of divided-wall distillation column includes at least one reaction zone with transalkylation reaction catalyst.The invention also discloses the ethylbenzene manufacturing processes using above-mentioned separation method and the ethylbenzene production plants including above-mentioned divided-wall distillation column.Compared with common divided-wall distillation column, the present invention can effectively improve the purity of ethylbenzene product by the way that transalkylation reaction catalyst is arranged in the feed zone of partition wall side in divided-wall distillation column.
Description
Technical field
The present invention relates to a kind of separation method of ethylbenzene and a kind of production methods of ethylbenzene, and the invention further relates to a kind of use
Device in production ethylbenzene and the method using device production ethylbenzene.
Background technique
Ethylbenzene is important industrial chemicals, is mainly used for dehydrogenation production styrene, and a small amount of ethylbenzene is also used for solvent, dilution
Agent and production diethylbenzene etc..In ethylbenzene production plants, benzene and ethylene are alkylated reaction under the effect of the catalyst
Ethylbenzene is generated, while more ethylbenzene components and a small amount of heavy aromatics such as generate diethylbenzene, triethylbenzene (TEB), using isolated high-purity
Ethylbenzene product.
Traditional ethylbenzene isolation technics is generally made of benzene column, cut light tower, ethylbenzene tower and more ethylbenzene towers.Contain light group
Point, benzene, ethylbenzene, more ethylbenzene and heavy constituent mixture initially enter benzene column, to recycle the excessive benzene in reaction process.By benzene column
The benzene that tower top is isolated is recycled back to alkylation reactor, and materials at bottom of tower enters ethylbenzene tower and separated.Ethylbenzene column overhead separates
To the ethylbenzene product (ethylbenzene mass fraction is usually > 99.9%) of high-purity, materials at bottom of tower is mainly more ethylbenzene and heavy aromatics,
More ethylbenzene towers are entered back into, transalkylation reactor is recycled to by more ethylbenzene that tower top is isolated and further reacts, and tower bottom obtains
High boiling component (such as heavy aromatics) can be used as Residual oil carrying device.Part benzene vapour will be usually isolated by benzene column tower top to send
Enter cut light tower, to remove the light component in recycle benzene, avoids its aggregation in recycle benzene.
Rectifying column main body is divided by the way that a vertical partition wall is arranged inside rectifying column and is located at separation by divided-wall distillation column
Public rectifying section above wall, the public stripping section below partition wall and the feed zone positioned at partition wall two sides and side line go out
Expect section, for needing the three compositions system of two conventional rectification towers separation, can be completed in a divided-wall distillation column.Due to
The equipment can be by the separation task merging of two towers or three towers to a tower, therefore greatly reduces equipment investment expense.In addition,
Due to high-energy utilization rate, divided-wall distillation column is widely used in separating three compositions system, at home and abroad all by extensive
Concern.
With separating deepening continuously for all kinds of object systems research using divided-wall distillation column, divided-wall distillation column is industrially
Using also increasingly wider.Currently, divided-wall distillation column is recycling benzene, benzene and toluene from reformed oil or hydropyrolysis gasoline
And dimethylbenzene separation, tetrahydrofuran, butanone and the substances such as butanediol, propylene and butylene, propylene and hexene, pentamethylene, cyclohexene
There is the report of application in the fields such as the separation of synthesis process.The Uop Inc. in the U.S. and middle petrochemical industry Shanghai engineering company also taste respectively
Divided-wall distillation column is applied to ethylbenzene or isopropylbenzene separation process by examination.
US7525004 discloses the method for a kind of ethylene and benzene alkylation production ethylbenzene.In this method, alkylate and
Transalkylated product still initially enters the benzene column using conventional rectification, isolates benzene respectively as alkylation by tower top and side line
And transalkylation raw material, and benzene column materials at bottom of tower is sent into a divided-wall distillation column, it is obtained by divided-wall distillation column tower top
Ethylbenzene product, side line isolate more ethylbenzene and are recycled to transalkylation reactor, and tower bottom is the Residual oil rich in heavy aromatics.Benzene column tower top
Operating pressure be 620-724kPa, temperature be 149-166 DEG C；Divided-wall distillation column operating pressure is 103-241kPa, tower top
Temperature is 88-104 DEG C.
US7525003 discloses another scheme that reaction production ethylbenzene is alkylated by ethylene and benzene.In the party
In the product separation process of case, alkylate and transalkylated product initially enter a divided-wall distillation column, by tower top and divide
Next door rectifier side line isolates benzene, respectively as alkylation and transalkylation raw material；By divided-wall distillation column medial side
Line isolates ethylbenzene as product；Divided-wall distillation column materials at bottom of tower is mainly more ethylbenzene and heavy aromatics component, is sent into more ethylbenzene
Tower is separated.More ethylbenzene that more ethylbenzene column overheads obtain are recycled to transalkylation reactor, and tower bottom product is sent out as Residual oil
Device.The operating pressure of divided-wall distillation column tower top is 103-241kPa (absolute pressure), and temperature is 88-104 DEG C；More ethylbenzene column overheads
Operating pressure is 21-23kPa, and tower top temperature is 121-138 DEG C.
US7498472 discloses a kind of technique for being alkylated reaction production ethylbenzene by ethylene and benzene.In the technique
In, alkylate and transalkylated product are only separated by a divided-wall distillation column.By tower top and divided-wall distillation column
Top side line isolates benzene, respectively as alkylation and transalkylation raw material, isolates second by side line in the middle part of divided-wall distillation column
Benzene isolates more ethylbenzene as product, by divided-wall distillation column lower part side line, is recycled to transalkylation reactor, and tower bottom product is made
For Residual oil carrying device.The operating pressure of divided-wall distillation column tower top is 103-241kPa (absolute pressure), and temperature is 88-104 DEG C.
US7713386 discloses a kind of device for preparing ethylbenzene or isopropylbenzene.In this scenario, alkylate and alkyl
Transfer product initially enters a divided-wall distillation column, isolates benzene by tower top and divided-wall distillation column top side line, respectively as
Alkylation and transalkylation feedstock circulation are to alkylation reactor and transalkylation reactor；By side line in the middle part of divided-wall distillation column
Ethylbenzene or isopropylbenzene are isolated as product；Divided-wall distillation column materials at bottom of tower is mainly polyalkylbenzene component, is sent into more alkyl
Benzene column is separated.The polyalkylbenzene that polyalkylbenzene column overhead obtains is recycled to transalkylation reactor, and tower bottom product is as residual
Oily carrying device.The operating pressure of divided-wall distillation column tower top is 103-241kPa (absolute pressure), and temperature is 88-104 DEG C；More alkyl
Benzene column tower top operating pressure is 21-23kPa, and tower top temperature is 121-138 DEG C.
CN104027995A, which is disclosed, a kind of utilizes double partition divided-wall distillation column Separation of Benzene, ethylbenzene, more ethylbenzene and recombination
Divide the method for mixture.Double partition divided-wall distillation columns are two sections of vertical partition plates of setting inside rectifying column, by rectifying column from upper
Rectifying section, the first bulkhead section, interlude, the second bulkhead section and the second bulkhead section for being divided into the first bulkhead section or more down are below
Five part of stripping section.After alkylation reaction product enters divided-wall distillation column, recycle benzene, the first bulkhead section side line are obtained by tower top
Ethylbenzene product is obtained, the second bulkhead section side line obtains recycling more ethylbenzene, and tower bottom is Residual oil.The divided-wall distillation column has 90-130 block
Theoretical plate, operating pressure 430-550kPa.The partition wall essence proposed in the divided-wall distillation column and US7498472 of this structure
It evaporates tower to compare, although more ethyl-benzene levels of side take-off can be improved, the number of plates is excessive, increases the difficulty of device fabrication；
And higher operating pressure also implies that tower reactor is not available high steam as heat source and meets temperature requirement, further increases
Cost of equipment.
Also, although current divided-wall distillation column technology efficiently solves conventional ethylene and benzene alkylation product separation process
The high problem of middle energy consumption, but found in actual mechanical process, the overall purity of ethylbenzene product still needs to be further improved.
Summary of the invention
It is an object of the invention to the existing ethylene using divided-wall distillation column and benzene alkylation product separating technique
It improves, to further increase the overall purity of ethylbenzene product.
According to the first aspect of the invention, the present invention provides a kind of ethylbenzene separation method, this method includes will be a kind of
Mixture is sent into divided-wall distillation column and carries out rectifying, and the mixture contains ethylbenzene, benzene and more ethylbenzene, the partition wall rectifying
Bulkhead section in tower includes by the adjacent feed zone of partition wall and intermediate species lateral line discharging section, and the feed zone includes charging
Mouthful, the intermediate species lateral line discharging section includes intermediate species side line discharge, and the mixture is entered by the feed inlet
The divided-wall distillation column is separated, and exports extraction ethylbenzene from the intermediate species side line, wherein the feed zone includes extremely
A few reaction zone, the reaction zone have at least one transalkylation reaction catalyst.
According to the second aspect of the invention, the present invention provides a kind of ethylbenzene manufacturing processes, this method includes alkylation
Reaction step, separating step, optional transalkylation reaction step and optional more ethylbenzene separating steps,
In the alkylated reaction step, ethylene is contacted with benzene and is alkylated reaction, obtain containing ethylbenzene, benzene and
The mixture of more ethylbenzene；
In the separating step, isolated from the mixture using method described in first aspect of the present invention to
Small part ethylbenzene is alternatively separated out at least partly benzene and at least partly more ethylbenzene, and optionally sends out part kettle material
Separating step；
In more ethylbenzene separating steps, isolated at least partly from the kettle material exported by the separating step
More ethylbenzene；
In transalkylation reaction step, benzene is contacted with more ethylbenzene and carries out transalkylation reaction, more ethylbenzene come from
In the separating step and/or more ethylbenzene separating steps, at least partly benzene is optionally in the separating step by light group
Divide the benzene of side line outlet extraction.
According to the third aspect of the present invention, the present invention provides a kind of for producing the device of ethylbenzene, which includes
Alkylated reaction unit, separative unit, optional more ethylbenzene separative units and optional transalkylation reaction unit,
The alkylated reaction unit is used to obtain ethylene and benzene haptoreaction mixed containing benzene, ethylbenzene and more ethylbenzene
Close object；
The separative unit is optional for isolating at least partly ethylbenzene from the mixture that alkylated reaction unit exports
More ethylbenzene and benzene are isolated in ground, optionally export part kettle material；
More ethylbenzene separative units from the kettle material that separative unit exports for isolating more ethylbenzene；
The transalkylation reaction unit carries out transalkylation reaction, more ethylbenzene for contacting benzene with more ethylbenzene
From the separative unit and/or more ethylbenzene separative units；
The separative unit includes divided-wall distillation column subelement, for being separated to the mixture, the separation
The bulkhead section of wall rectifying column includes the feed zone abutted by partition wall and product discharge section, and the feed zone is provided with for inciting somebody to action
The mixture introduces the feed inlet of the divided-wall distillation column, and the centre that the product discharge section is provided with for producing ethylbenzene evaporates
Divide side line outlet, the divided-wall distillation column is optionally provided with the outlet of the light component side line for producing benzene and for producing
The heavy constituent side line of more ethylbenzene exports, position locating for lower end of the heavy constituent side line outlet present position lower than the partition wall
It sets, light component side line outlet present position is not less than the upper end present position of the partition wall, wherein the feed zone packet
At least one reaction zone is included, the reaction zone has transalkylation reaction catalyst.
According to the fourth aspect of the present invention, the present invention provides a kind of method for producing ethylbenzene, this method is in the present invention
It is carried out in device described in terms of third, comprising:
By ethylene and benzene in alkylated reaction unit haptoreaction, obtain the mixture containing benzene, ethylbenzene and more ethylbenzene；
In separative unit, at least partly ethylbenzene is isolated from the mixture that alkylated reaction unit exports, optionally
More ethylbenzene and benzene are isolated, optionally exports part kettle material；
In more ethylbenzene separative units, more ethylbenzene are isolated from the kettle material that separative unit exports；
In transalkylation reaction unit, benzene is contacted with more ethylbenzene, carry out transalkylation reaction, more ethylbenzene are point
At least partly more ethylbenzene that at least partly more ethylbenzene and/or more ethylbenzene separative units isolated from unit are isolated.
Compared with traditional ethylbenzene isolation technics (being separated by benzene column, ethylbenzene tower and more ethylbenzene towers), using this hair
Bright method and apparatus separate the mixture containing benzene, ethylbenzene and more ethylbenzene, have the advantage that divided-wall distillation column
It is thermodynamically equivalent to the rectifying column being thermally integrated completely, is thermally integrated operation by the way that partition wall is arranged in tower to realize,
The three-component system that two rectifying columns could be completed needed for conventional separation techniques can be completed using a divided-wall distillation column
Separation, not only saves equipment investment, and significantly reduce energy consumption.
Compared with common divided-wall distillation column, feed zone that the present invention passes through the partition wall side in divided-wall distillation column
Middle setting transalkylation reaction catalyst, can effectively improve the purity of ethylbenzene product.
Detailed description of the invention
The drawings are intended to provide a further understanding of the invention, and constitutes part of specification, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.
Fig. 1 is for illustrating ethylbenzene separation method of the invention.
Fig. 2 is for illustrating ethylbenzene production plants and production method of the invention.
Description of symbols
1: 21: the first reaction zone of mixture containing benzene, ethylbenzene and more ethylbenzene
22: second reaction zone 3: partition wall
4: ethylbenzene 5: more ethylbenzene
51: more ethylbenzene 6 for circulation: benzene
7: overhead stream 8: kettle material
81: the kettle material 82 for boiling again: the kettle material for output
9: cooler 10: overhead stream return tank
11: benzene vapour and light component 12: overhead stream reflux pump
13: reflux benzene 14: recycle benzene
15: reboiler
Specific embodiment
According to the first aspect of the invention, the present invention provides a kind of ethylbenzene separation methods, including by a kind of mixture
It is sent into divided-wall distillation column and carries out rectifying.
The mixture contains ethylbenzene, benzene and more ethylbenzene.Depending on the composition of the mixture is with the source of the mixture.One
As, on the basis of the total amount of the mixture, the content of benzene can be 40-70 weight %, preferably 50-65 weight %, such as
55-65 weight %；The content of ethylbenzene can be 20-50 weight %, preferably 22-40 weight %, such as 25-35 weight %；More second
The content of benzene can be 2-25 weight %, preferably 5-13 weight %, such as 7-10 weight %.More ethylbenzene refer to diethylbenzene and
Triethylbenzene (TEB).According to the difference in source, the mixture can also contain some heavy constituents, the heavy constituent be generally four ethylbenzene or
Boiling point is higher than the ingredient (such as heavy aromatics) of four ethylbenzene.On the basis of the total amount of the mixture, the content of the heavy constituent is general
For 0.1-1 weight %, such as 0.2-0.5 weight %.
The mixture be specifically as follows ethylene contacted with benzene reaction mixture obtained from being alkylated reaction and/
Or more ethylbenzene are contacted to mixture obtained from carrying out transalkylation reaction with benzene.For ethylene and benzene haptoreaction are prepared second
The concrete technology condition of benzene and the concrete technology condition that more ethylbenzene and benzene haptoreaction are prepared to ethylbenzene, will carry out in detail below
Describe in detail bright, and will not be described here in detail.
The inner space of the divided-wall distillation column includes rectifying section, bulkhead section and stripping section, and the rectifying section is located at institute
The top of bulkhead section is stated, the stripping section is located at the lower section of the bulkhead section.The bulkhead section refers to the space with partition wall.
The bulkhead section includes by the adjacent feed zone of partition wall and intermediate species lateral line discharging section, the feed zone packet
Feed inlet is included, for receiving the mixture, and the mixture is made to carry out pre-separation in feed zone.The partition wall is two
Side is separately fixed at the plate on the inner wall of rectifying column, and generally, the partition wall passes through the central axes of the rectifying column, so that
Feed zone and intermediate species lateral line discharging section are the identical or essentially identical two spaces of volume.The feed zone and the centre
The upper and lower ends of component lateral line discharging section are opening.The intermediate species lateral line discharging section includes intermediate species lateral line discharging
Mouthful, ethylbenzene is produced from the intermediate species side line discharge.
Divided-wall distillation column according to the present invention, the feed zone further include at least one reaction zone, the reaction zone tool
There is at least one transalkylation reaction catalyst.The reaction zone refers in feed zone, and there is (being filled with) transalkylation reaction to urge
The space of agent.By feed zone be arranged reaction zone can effectively improve the purity of ethylbenzene, while can also effectively inhibit by
The influence to ethylbenzene purity is fluctuated in feed composition and/or rectifying column operating condition.
The quantity of the reaction zone is more than one.Preferably, the feed zone includes the first reaction zone and the second reaction
Area, first reaction zone and the second reaction zone along the longitudinal direction (that is, axial direction of divided-wall distillation column) of the feed zone by
It is set gradually under.Preferably, the lower end present position of first reaction zone is not less than the feed inlet, and described second is anti-
The upper end present position in area is answered to be not higher than the lower end present position of first reaction zone.The lower end of first reaction zone and institute
The upper end for stating second reaction zone can be to connect, or there is interval.It is steady from the purity for the ethylbenzene for further increasing extraction
Qualitative angle is set out, and the theoretical cam curve of first reaction zone lower end present position is tR1 L, the second reaction zone upper end
The theoretical cam curve of present position is tR2 U, the theoretical cam curve of the feed inlet present position is tI, tR1 L/tIIt is excellent for 0.8-1
It is selected as 0.9-1, more preferably 0.95-0.98, further preferably 0.96-0.97；tR2 U/tIFor 1-1.2, preferably 1-1.1,
More preferably 1-1.05, most preferably 1.As a preferred example, the theoretical cam curve of the feed inlet present position with
The difference of the theoretical cam curve of first reaction zone lower end present position is 1 (that is, first reaction zone lower end present position
One block of theoretical tray lower than the feed inlet present position), the theoretical cam curve of second reaction zone upper end present position with
The theoretical cam curve of the feed inlet present position is identical.In the present invention, theoretical cam curve be using the tower top of rectifying column as rise
Beginning position (being calculated as 1), the theoretical cam curve counted downwards.In the present invention, the height of present position be using the tower bottom of rectifying column as
The relative position of benchmark.
The upper end present position of first reaction zone and the lower end present position of the second reaction zone can bases
The height of feed zone is selected.Preferably, the theoretical cam curve of first reaction zone upper end present position is tR1 U, described
The theoretical cam curve of second reaction zone lower end present position is tR2 L, the theoretical cam curve of the feed inlet present position is tI,
tR1 U/tI=0.7-0.9, tR2 L/tI=1.1-1.5, in this way can be between the purity stability and operating cost of the ethylbenzene of extraction
Obtain good balance.Preferably, tR1 U/tI=0.8-0.9, tR2 L/tI=1.2-1.4.It is highly preferred that tR2 L/tI=1.25-
1.35。
From the angle of the purity stability for the ethylbenzene for further increasing extraction, the theoretical tray of the second reaction zone
Number (that is, the theoretical cam curve in the section as defined by second reaction zone upper end to second reaction zone lower end) is preferably not less than first
The theoretical cam curve of reaction zone is (that is, the theoretical tower in the section as defined by the upper end to the first reaction zone lower end of the first reaction zone
Plate number).It is highly preferred that the theoretical cam curve of the second reaction zone is 2-3 times of the theoretical cam curve of the first reaction zone.
The transalkylation reaction catalyst can be the common catalyst to transalkylation reaction with catalytic action.
From the angle of operation convenience, the transalkylation reaction catalyst, which is selected from, has catalytic action to transalkylation reaction
Solid acid catalyst.Specifically, the transalkylation reaction catalyst can be molecular sieve and/or supported solid acid catalysis
Agent, preferably molecular sieve.
The specific example of the molecular sieve can include but is not limited to faujasite, modenite, zeolite L, ZSM-5 point
Sub- sieve, ZSM-20 molecular sieve, beta-molecular sieve, MCM-22 molecular sieve, MCM-36 molecular sieve, MCM-49 molecular sieve, MCM-56 molecular sieve
And Y molecular sieve.Preferably, the molecular sieve is Y molecular sieve.
The molecular sieve can be molecular screen primary powder, or molded molecular sieve.For molded molecular sieve, can also wrap
Include at least one carrier as binder.The carrier can be conventional selection, such as heat-resistant inorganic oxide.Specifically, institute
Aluminium oxide, silica, magnesia and titanium oxide can be selected from by stating carrier.The content of the carrier can be wanted according to specific use
It asks to determine, as long as the catalytic activity and intensity of final molded molecular sieve meet requirement.Preferably, with molding point
On the basis of the total amount of son sieve, the content of the molecular sieve can be 30-95 weight %, preferably 50-90 weight %, more preferably
70-80 weight %；The content of the heat-resistant inorganic oxide can be 5-70 weight %, preferably 10-50 weight %, more preferably
For 20-30 weight %.
The load-type solid acid catalyst, which can be negative, is loaded with the supported solid acid catalysis of super acids and/or heteropoly acid
Agent.The super acids can be super for bronsted super acid, Lewis superacids, the bronsted-Lewis superacids of conjugation and solid
Acid.The specific example of the super acids can include but is not limited to HSO3Cl、HSO3F、HSO3CF3、H2SO4·SO3、H2SO4·B
(OH)3、HSO3F·SbF5、TiO2·H2SO4And ZrO2·H2SO4.The specific example of the heteropoly acid can include but is not limited to
Phosphotungstic acid, phosphomolybdic acid, silico-tungstic acid, silicomolybdic acid and P-Mo-Wo acid.Sour content can be in the load-type solid acid catalyst
Conventional selection, generally with the difference of sour type depending on, this is not particularly limited in the present invention.
The transalkylation reaction catalyst is commercially available, and can also be prepared using conventional method, herein no longer in detail
It states.
The transalkylation reaction catalyst can be placed in feed zone in a variety of manners, to form the reaction
Area.Specifically, the transalkylation reaction catalyst can be packed (that is, transalkylation reaction catalyst is placed in packed
In container) form be placed in feed zone, can also by the transalkylation reaction catalyst by dissipate heap in the form of be placed in charging
The transalkylation catalyst can also be made integral catalyzer and be placed on feed zone by Duan Zhong, in addition can also will be described
Transalkylation catalyst is arranged on partition wall (for example, being arranged transalkylation catalyst in the form of coating in partition wall
On).Aforesaid way can be used alone, and two or more modes can also be applied in combination.
The loadings of the transalkylation reaction catalyst can be selected according to the treating capacity of divided-wall distillation column.One
As, relative to the inlet amount of the mixture, the weight (hourly) space velocity (WHSV) of the transalkylation reaction catalyst can be 2-120h-1,
Preferably 5-95h-1, more preferably 10-40h-1, such as can be 15-25h-1。
It according to the method for the present invention, is 99.9 weight % or more by the purity of the ethylbenzene of intermediate species side line outlet extraction,
Such as 99.92 weight % or more.
The mixture is separated using divided-wall distillation column, while can isolate ethylbenzene, moreover it is possible to isolate
Benzene and/or more ethylbenzene.
Method according to the invention it is possible to be exported by the heavy constituent side line of the divided-wall distillation column more by what is isolated
Ethylbenzene extraction.The heavy constituent side line outlet is located at stripping section, i.e., the described heavy constituent side line outlet present position is not higher than described
The lower end present position of partition wall.From the angle for the purity for further increasing more ethylbenzene, the heavy constituent side line exports institute
The theoretical cam curve for locating position is tH, the theoretical cam curve of partition wall lower end present position is t2 L, tH/t2 LPreferably 1-5,
More preferably 1-3.5, further preferably 1-2 are still more preferably 1-1.5, particularly preferably 1.05-1.2, most preferably
1.05-1.15, such as 1.1.
Amount from more ethylbenzene of heavy constituent side line outlet extraction can be conventional selection.According to the method for the present invention,
The amount of more ethylbenzene from heavy constituent side line outlet extraction is adjusted, so that the content of diethylbenzene is 50-90 weight in kettle material
% is measured, the bottom temperature of divided-wall distillation column can be controlled within the appropriate range in this way.Preferably, it adjusts from the heavy constituent
The amount of more ethylbenzene of side line outlet extraction, so that the content of diethylbenzene is 50-90 weight %, preferably 60-85 in kettle material
Weight %, such as 65-80 weight %.
It according to the method for the present invention, is 95 weight % or more by the purity of more ethylbenzene of heavy constituent side line outlet extraction.
It can be exported, can also be sent into transalkylation reaction unit by more ethylbenzene of heavy constituent side line outlet extraction
It is contacted with benzene, transalkylation reaction is carried out, to produce more ethylbenzene.With the method for the invention it is preferred to will at least partly by
More ethylbenzene of heavy constituent side line outlet extraction are sent into the divided-wall distillation column together with the mixture, with further
Improve the purity of the ethylbenzene of extraction.Preferably, it on the basis of the total amount of more ethylbenzene by more ethylbenzene side line outlets extraction, follows
The amount that ring is sent into more ethylbenzene of the divided-wall distillation column is 0.5-30 weight %.It is highly preferred that with by more ethylbenzene side lines
On the basis of the total amount for exporting more ethylbenzene of extraction, circulation is sent into the amount of more ethylbenzene of the divided-wall distillation column as 1-20 weight
Measure %.It is further preferred that on the basis of the total amount of more ethylbenzene by more ethylbenzene side line outlets extraction, described in circulation feeding
The amount of more ethylbenzene of divided-wall distillation column is 0.8-15 weight %.It is further preferred that be exported by more ethylbenzene side lines
On the basis of the total amount of more ethylbenzene of extraction, the amount that circulation is sent into more ethylbenzene of the divided-wall distillation column is 1-10 weight %.It can
The more ethylbenzene isolated to be sent into divided-wall distillation column together with the mixture.Except circulation is sent into divided-wall distillation column
Except more ethylbenzene, it can be sent by the more ethylbenzene of residue of heavy constituent side line outlet extraction in transalkylation reaction unit and/or defeated
Out.
According to the method for the present invention, the benzene isolated can be produced individually, can not also be produced, but with remaining light component
It is exported together as overhead stream.When individually producing the benzene isolated, the light component side of divided-wall distillation column can be passed through
Line outlet extraction benzene.The light component side line outlet is located in rectifying section, and light component side line exports present position and is higher than described point
The upper end present position in next door.From the angle of the purity for the benzene for further increasing extraction, the light component side line exports institute
The theoretical cam curve for locating position is tL, the theoretical cam curve of partition wall upper end present position is t2 U, tL/t2 UPreferably
0.05-0.95, more preferably 0.1-0.9, further preferably 0.2-0.6 are still more preferably 0.3-0.4.
It can be sent into transalkylation reaction unit from the benzene of light component side line outlet extraction and be contacted instead with more ethylbenzene
It answers, can also recycle with ethylene reaction in feeding alkylated reaction unit, can also be the combination of above two mode.It is preferred that
Ground will be at least partly sent into transalkylation reaction unit from the benzene of light component side line outlet extraction.
It according to the method for the present invention, is 99.5 weight % or more by the purity of the benzene of light component side line outlet extraction,
The mass content of water is not higher than 100ppm.
Benzene and a small amount of other light components are contained by the overhead stream that the tower top of the divided-wall distillation column obtains.It can adopt
Overhead stream is cooled down with conventional method, such as is exchanged heat with water, thus overhead stream is cooling, while generating low pressure
Steam (pressure is generally 0.02-0.5MPa, such as 0.03-0.2MPa or 0.04-0.1MPa).Overhead stream after cooling, can
Will at least partly be sent into through cooling overhead stream circulation as reflux benzene in divided-wall distillation column and/or be sent as recycle benzene
Enter in alkylated reaction unit as reaction raw materials.
The kettle material of the divided-wall distillation column contains more ethylbenzene and some heavy constituents.Kettle material can be sent into more
Further progress separates in ethylbenzene separative unit, and to isolate at least partly more ethylbenzene, the more ethylbenzene isolated can be exported,
It can be sent into transalkylation reaction unit and carry out transalkylation reaction, to increase the yield of ethylbenzene.
According to the method for the present invention, in the divided-wall distillation column, the theoretical tray of bulkhead section, rectifying section and stripping section
Number can be selected according to the composition of isolated mixture.Generally, the theoretical cam curve of the bulkhead section is t2, position
The theoretical cam curve of stripping section below the bulkhead section is t1, the theoretical tray of the rectifying section above the bulkhead section
Number is t3, total theoretical cam curve of the divided-wall distillation column is t, t1/ t can be 0.1-0.6, preferably 0.15-0.5, it is more excellent
It is selected as 0.2-0.3；t2/ t can be 0.1-0.8, preferably 0.2-0.7, more preferably 0.4-0.6；t3/ t can be 0.1-0.6,
Preferably 0.15-0.5, more preferably 0.2-0.3.
According to the method for the present invention, total theoretical cam curve of divided-wall distillation column can be conventional selection.According to the present invention
Method by feed zone be arranged reaction zone so that divided-wall distillation column have higher separative efficiency, there is no need to excessive
The number of plates, the purity and purity stability of the ethylbenzene isolated can be effectively improved.According to the method for the present invention, described point
The theoretical cam curve of next door rectifying column can be 30-90, preferably 40-80, more preferably 50-75, further preferably 60-
70。
It pays close attention to according to the method for the present invention and reaction zone is set in the feed zone of divided-wall distillation column, to improve simultaneously
The purity for stablizing the ethylbenzene isolated, for the other parameters for the divided-wall distillation column that do not address herein, those skilled in the art
Member is understandable that these parameters are not particularly limited in the present invention, can use the conventional selection of this field.
According to the method for the present invention, in terms of absolute pressure, the tower top pressure of the divided-wall distillation column can be 142-420kPa,
Preferably 150-380kPa, more preferably 200-360kPa, further preferably 260-350kPa.The divided-wall distillation column
Column bottom temperature can be 225-275 DEG C, preferably 235-265 DEG C.
According to the method for the present invention, when not passing through light component side line outlet extraction benzene, by weight percentage, tower top
Reflux ratio can be 0.8-3, preferably 0.85-2, more preferably 1-1.5.According to the method for the present invention, passing through light component side
When line outlet extraction benzene, reflux ratio can be adjusted according to the amount of extraction benzene.In a preferred implementation of the method for the present invention
In mode, on the basis of the total amount of benzene in the mixture separated into divided-wall distillation column, exported by light component side line
The amount of the benzene of extraction is 10-70 weight %, preferably 10-35 weight %, and by weight percentage, the reflux ratio of tower top can be
1-10, preferably 1.5-5, more preferably 1.5-3.
Fig. 1 shows the one kind separated using method of the invention to the mixture containing benzene, ethylbenzene and more ethylbenzene
Selection process process.As shown in Figure 1, the mixture 1 containing benzene, ethylbenzene and more ethylbenzene to be sent into the feed zone of divided-wall distillation column
In, pre-separation is carried out, upward logistics passes through the first reaction zone 21 during moving up；Downward logistics then passes through
Two reaction zones 22.By the intermediate species outlet extraction ethylbenzene that the intermediate species lateral line discharging section of 3 other side of partition wall is arranged in
4；Produce more ethylbenzene 5 by the outlet of heavy constituent side line, a part 51 in more ethylbenzene of extraction with contain benzene, ethylbenzene and more ethylbenzene
Mixture 1 recycle together be sent into divided-wall distillation column in separated, remaining more ethylbenzene can be contacted with benzene, carry out alkyl
Transfer reaction, with yield increase of ethylbenzene.Optionally, extraction benzene 6 is exported by light component side line.It is exported from the tower top of divided-wall distillation column
Overhead stream 7 enter in cooler 9 carry out it is cooling after enter in overhead stream return tank 10.Wherein, discharge part benzene vapour
With light component 11, with reduce reflux benzene impurity content.Material in overhead stream return tank 10 is pressurized through tower top return pump 12
Afterwards, it is divided into reflux benzene 13 and recycle benzene 14, wherein reflux benzene 13 returns in divided-wall distillation column, and recycle benzene 14 is as alkylation
The raw material and contact ethylene of reaction, are alkylated reaction.The kettle material 8 of the tower reactor output of divided-wall distillation column, a part
After being boiled again in the entrance reboiler 15 of kettle material 81, returns and be used as heat medium, another part kettle material 82 in tower reactor
It sends out divided-wall distillation column to be separated, obtains more ethylbenzene, the more ethylbenzene isolated can be contacted with benzene, and it is anti-to carry out transalkylation
It answers.
It can be used for separating the mixture containing benzene, ethylbenzene and more ethylbenzene various needs according to the method for the present invention
Occasion, especially suitable for preparing the process flow of ethylbenzene by ethylene and benzene.The second of ethylbenzene separation method of the invention is coupled
Benzene process process can obtain the higher ethylbenzene of purity with lower energy consumption.
According to the second aspect of the invention, the present invention provides a kind of ethylbenzene manufacturing processes, this method includes alkylation
Reaction step, separating step, optional transalkylation reaction step and optional more ethylbenzene separating steps.
In alkylated reaction step, ethylene is contacted with benzene and is alkylated reaction, obtained containing ethylbenzene, benzene and more second
The mixture of benzene.
It, can be under alkylation reaction condition by ethylene and benzene haptoreaction, to obtain in alkylated reaction step
Mixture containing benzene, ethylbenzene and more ethylbenzene.It specifically, can be in 100-400 DEG C, preferably 150-350 DEG C, more preferable 180-
Ethylene is contacted with benzene at 300 DEG C of temperature (reactor inlet temperatures).Pressure (reactor in terms of gauge pressure, when being contacted
Outlet pressure) it can be 0.1-10MPa, preferably 1-5MPa, more preferably 2-4MPa.
When benzene and contact ethylene, benzene is usually used with the amount for being more than stoichiometric ratio.Generally, the molar ratio of benzene and ethylene
It can be 1-15:1, preferably 2-10:1, more preferably 2-8:1, further preferably 3-6:1.
Ethylene can be carried out with benzene in the presence of having the catalyst for alkylation reaction of catalytic action to alkylated reaction
Contact.The catalyst for alkylation reaction is specifically as follows selected from the solid acid catalysis to alkylated reaction with catalytic action
Agent.Specifically, the catalyst for alkylation reaction can be molecular sieve and/or load-type solid acid catalyst.Preferably, described
Catalyst for alkylation reaction is molecular sieve.
The specific example of the molecular sieve can include but is not limited to faujasite, modenite, zeolite L, ZSM-5 point
Sub- sieve, ZSM-11 molecular sieve, ZSM-20 molecular sieve, beta-molecular sieve, MCM-22 molecular sieve, MCM-36 molecular sieve, MCM-49 molecular sieve
With MCM-56 molecular sieve.
The molecular sieve can be molecular screen primary powder, or molded molecular sieve.For molded molecular sieve, can also wrap
Include at least one carrier as binder.The carrier can be conventional selection, such as heat-resistant inorganic oxide.Specifically, institute
Aluminium oxide, silica, magnesia and titanium oxide can be selected from by stating carrier.The content of the carrier can be wanted according to specific use
It asks to determine, as long as the catalytic activity and intensity of final molded molecular sieve meet requirement.Preferably, with molding point
On the basis of the total amount of son sieve, the content of the molecular sieve can be 30-95 weight %, preferably 50-90 weight %, more preferably
70-80 weight %；The content of the heat-resistant inorganic oxide can be 5-70 weight %, preferably 10-50 weight %, more preferably
For 20-30 weight %.
The load-type solid acid catalyst, which can be negative, is loaded with the supported solid acid catalysis of super acids and/or heteropoly acid
Agent.The super acids can be super for bronsted super acid, Lewis superacids, the bronsted-Lewis superacids of conjugation and solid
Acid.The specific example of the super acids can include but is not limited to HSO3Cl、HSO3F、HSO3CF3、H2SO4·SO3、H2SO4·B
(OH)3、HSO3F·SbF5、TiO2·H2SO4And ZrO2·H2SO4.The specific example of the heteropoly acid can include but is not limited to
Phosphotungstic acid, phosphomolybdic acid, silico-tungstic acid, silicomolybdic acid and P-Mo-Wo acid.Sour content can be in the load-type solid acid catalyst
Conventional selection, generally with the difference of sour type depending on, this is not particularly limited in the present invention.
Alkylated reaction can carry out in common reactor, carry out preferably in fixed bed reactors.In fixed bed
In reactor, the loadings of the catalyst for alkylation reaction can be selected according to the treating capacity of reactor.Generally, phase
For the inlet amount of benzene, the weight (hourly) space velocity (WHSV) of catalyst for alkylation reaction can be 1-10h-1, preferably 1-5h-1, more preferably 2-
4h-1。
In separating step, at least portion is isolated from the mixture using method described in first aspect of the present invention
Divide ethylbenzene, be alternatively separated out at least partly benzene and at least partly more ethylbenzene, and optionally part kettle material is sent out and is separated
Step.
In more ethylbenzene separating steps, at least partly more second are isolated from the kettle material exported by the separating step
Benzene.More ethylbenzene can be isolated from kettle material using conventional method.It generally, can be using the method for rectifying to tower reactor object
Material is separated, to isolate at least partly more ethylbenzene therein.The separation condition of rectifying column can be according to kettle material
Composition is selected.Specifically, the tower top pressure of the rectifying column can be 10-90kPa (absolute pressure), preferably 15-80kPa
(absolute pressure)；Column bottom temperature can be 200-260 DEG C, preferably 210-250 DEG C.
More ethylbenzene that more ethylbenzene separating steps are isolated can export, and at least partly more ethylbenzene can also be sent into alkyl and turned
It with benzene haptoreaction to produce more ethylbenzene can also be the combination of above two mode during walk is rapid.
In transalkylation reaction step, benzene is contacted with more ethylbenzene and carries out transalkylation reaction, to prepare ethylbenzene.It is described
More ethylbenzene that more ethylbenzene are isolated from the separating step can also include at least portion that more ethylbenzene separating steps are isolated
Divide more ethylbenzene.In transalkylation reaction step, the benzene can be in separating step from the benzene of light component side line outlet extraction
And/or fresh benzene.Preferably, at least partly benzene is in separating step from the benzene of light component side line outlet extraction.
In transalkylation reaction step, benzene and the catalytic condition of more ethylbenzene can be conventional selection.Generally, benzene
Weight ratio with more ethylbenzene can be 1-10:1, preferably 2-8:1, more preferably 3-6:1.Haptoreaction can temperature (into
Mouthful temperature) it is 100-400 DEG C, preferably 120-300 DEG C, more preferably 150-200 DEG C and pressure (gauge pressure, outlet pressure) is
It is carried out under conditions of 0.1-10MPa, preferably 1-5MPa, more preferably 2-3MPa.Relative to the inlet amount of benzene, transalkylation is anti-
The weight (hourly) space velocity (WHSV) for answering catalyst can be 0.1-10h-1, preferably 1-5h-1, more preferably 1.5-3h-1。
In transalkylation reaction step, benzene and the contact of more ethylbenzene are preferably in the presence of transalkylation reaction catalyst
It carries out.The type of the transalkylation reaction catalyst can be for above to the transalkylation reaction catalysis in divided-wall distillation column
Mentioned transalkylation reaction catalyst when agent is described, and will not be described here in detail.Transalkylation reaction step is mixed
Object contains benzene, ethylbenzene and more ethylbenzene, can be sent into the separating step and be separated, to obtain ethylbenzene product.
Ethylbenzene is produced using method of the invention, the ethylbenzene of high-purity on the one hand can be obtained, on the other hand can also obtain more
High ethylbenzene yield.
According to the third aspect of the present invention, the present invention provides a kind of for producing the device of ethylbenzene, as shown in Fig. 2,
The device includes alkylated reaction unit, separative unit, optional more ethylbenzene separative units and optional transalkylation reaction
Unit.
The alkylated reaction unit is used to ethylene and benzene haptoreaction obtaining the alkane containing benzene, ethylbenzene and more ethylbenzene
Glycosylation reaction mixture.The alkylated reaction unit may include at least one fixed bed reactors, be used for ethylene and benzene
Haptoreaction in the presence of catalyst for alkylation reaction obtains the mixture containing benzene, ethylbenzene and more ethylbenzene.By ethylene and benzene
Detailed description has been carried out above with the condition for preparing ethylbenzene for haptoreaction, and and will not be described here in detail.
The separative unit is used for the alkyl exported from alkylated reaction unit and optional transalkylation reaction unit
Change in reaction mixture and isolate at least partly ethylbenzene, more ethylbenzene and benzene is alternatively separated out, optionally by part kettle material
Output.
The separative unit includes divided-wall distillation column subelement, for being separated to the mixture, the separation
The bulkhead section of wall rectifying column includes the feed zone abutted by partition wall and product discharge section, and the feed zone is provided with for inciting somebody to action
The mixture introduces the feed inlet of the divided-wall distillation column, and the centre that the product discharge section is provided with for producing ethylbenzene evaporates
Divide side line outlet, the divided-wall distillation column is optionally provided with the outlet of the light component side line for producing benzene and for producing
The heavy constituent side line of more ethylbenzene exports, position locating for lower end of the heavy constituent side line outlet present position not higher than the partition wall
It sets, light component side line outlet present position is higher than the upper end present position of the partition wall, wherein the feed zone includes
At least one reaction zone, the reaction zone have transalkylation reaction catalyst.The specific configuration of the divided-wall distillation column with
The divided-wall distillation column of first aspect description of the present invention is identical, and and will not be described here in detail.
The separative unit can also include that more ethylbenzene recycle subelement, for isolating at least divided-wall distillation column
The more ethylbenzene in part are sent into divided-wall distillation column with together with the mixture that alkylated reaction unit exports.
More ethylbenzene separative units from the kettle material that separative unit exports for isolating more ethylbenzene.More second
Benzene separative unit may include at least one rectifying column, to separate to kettle material, obtain more ethylbenzene.From kettle material
In more ethylbenzene are separated by rectifying the ethylbenzene manufacturing processes part of condition second part above have been carried out specifically
Bright, and will not be described here in detail.
The transalkylation reaction unit carries out transalkylation reaction, more ethylbenzene for contacting benzene with more ethylbenzene
From the separative unit and/or more ethylbenzene separative units.The transalkylation reaction unit can have at least one
A fixed bed reactors, for benzene and more ethylbenzene to be carried out transalkylation reaction in the presence of a transalkylation catalyst.
The benzene that the transalkylation reaction unit uses can export to pass through light component side line in separative unit from separation
The benzene and/or fresh benzene of wall rectifying column extraction.Preferably, at least partly benzene be separative unit in by light component side line outlet from
The benzene of divided-wall distillation column extraction.Benzene and more ethylbenzene are subjected to transalkylation reaction in the presence of transalkylation reaction catalyst
Condition above, detailed description is had been carried out in ethylbenzene manufacturing processes part, and will not be described here in detail.
The mixture that the transalkylation reaction unit obtains is the mixture containing benzene, ethylbenzene and more ethylbenzene, can be sent
Enter in separative unit and separated, to obtain ethylbenzene product.
The apparatus according to the invention further includes benzene cycling element, and at least partly benzene for exporting separative unit carries out
Purification is sent into alkylated reaction unit and/or transalkylation reaction unit after removing water therein and light component.
According to the fourth aspect of the present invention, the present invention provides a kind of methods for producing ethylbenzene, and this method is according to this
It is carried out in device described in terms of invention third, comprising:
By ethylene and benzene in alkylated reaction unit haptoreaction, obtain the mixture containing benzene, ethylbenzene and more ethylbenzene；
In separative unit, at least partly ethylbenzene is isolated from the mixture that alkylated reaction unit exports, optionally
More ethylbenzene and benzene are isolated, optionally exports part kettle material；
In more ethylbenzene separative units, more ethylbenzene are isolated from the kettle material that separative unit exports；
In transalkylation reaction unit, benzene is contacted with more ethylbenzene, carry out transalkylation reaction, more ethylbenzene are point
At least partly more ethylbenzene that at least partly more ethylbenzene and/or more ethylbenzene separative units isolated from unit are isolated.
The method of 4th aspect according to the present invention is the separation for the mixture that alkylated reaction, alkylated reaction obtain, more
The separation of ethylbenzene and the condition of transalkylation reaction are described in detail respectively above.And will not be described here in detail.
The invention will be further described by the following examples, but the range being not intended to limit the present invention.
Comparative example 1
This comparative example separates ethylbenzene using conventional method, and concrete technology flow process is as follows.
Separator is made of benzene column, ethylbenzene tower and more ethylbenzene towers.
On the basis of the separative unit of 400,000 tons/year of Benzene Devices, exported to alkylation reaction unit as shown in Table 1 is formed
Mixture separated, inlet amount 162662kg/h.The mass percent of the operating condition of each tower and the benzene isolated
The mass percent of (that is, purity of benzene, similarly hereinafter), the mass percent of ethylbenzene (that is, purity of ethylbenzene, similarly hereinafter) and more ethylbenzene
(that is, purity of more ethylbenzene, similarly hereinafter) is listed in table 2, and the energy consumption of separative unit is listed in table 3.
Mixture containing light component, benzene, ethylbenzene, more ethylbenzene and heavy constituent initially enters the benzene column (theory of feed entrance point
The number of plates is 20) to be separated, and isolating benzene by benzene column tower top, (extraction benzene amount is 97950kg/h, the mass content of water
184ppm).The materials at bottom of tower of benzene column enters ethylbenzene tower (theoretical cam curve of feed entrance point is 25) and is separated, by ethylbenzene tower tower
Push up isolated ethylbenzene product (extraction amount of ethylbenzene is 50010kg/h).The materials at bottom of tower of ethylbenzene tower enters more ethylbenzene towers, by ethylbenzene
The isolated more ethylbenzene of the tower top of tower (producing more amount of ethylbenzene is 4942kg/h).
1 feed composition of table (mass fraction)
| Water | Non-aromatic component before benzene | Benzene | Toluene | Ethylbenzene | Diethylbenzene | Triethylbenzene (TEB) | Four ethylbenzene | Butylbenzene | Heavy aromatics * |
| 111ppm | 0.004 | 0.598 | 248ppm | 0.307 | 0.08 | 0.006 | 74ppm | 0.003 | 0.002 |
*: boiling point is higher than the aromatic component of four ethylbenzene
Table 2
| Benzene column | Ethylbenzene tower | More ethylbenzene towers | |
| Tower top operating pressure, kPa (absolute pressure) | 600 | 210 | 30 |
| Theoretical cam curve | 38 | 45 | 15 |
| Column bottom temperature, DEG C | 230 | 226 | 228 |
| Tower bottom reboiler thermic load, kW | 13810 | 6914 | 1220 |
| Tower top cooler thermic load, kW | 16727 | 9300 | 2112 |
| Overhead benzene mass percent, wt% | 99.3 | - | - |
| Overhead ethylbenzene mass percent, wt% | - | 99.85 | - |
| The more ethylbenzene mass percents of tower top, wt% | - | - | 96.3 |
Table 3
| Unit | Consumption per hour | Product consumption per ton | The energy consumption of ethylbenzene per ton | |
| Consume high-pressure saturated steam | Ton | 46.75 | 0.935 | 3445 |
| Low-pressure steam occurs | Ton | - 41.20 | - 0.824 | - 1897.5 |
| Comprehensive energy consumption | Million is burnt | - | - | 1547.5 |
Embodiment 1-6 is for illustrating the present invention.
Embodiment 1
The separator that the present embodiment uses includes a divided-wall distillation column and ethylbenzene tower more than one.
Using divided-wall distillation column shown in Fig. 1, on the basis of the separative unit of 400,000 tons/year of Benzene Devices, to raw material group
It is separated at material as shown in Table 1, inlet amount 162662kg/h.
Divided-wall distillation column shares 60 blocks of theoretical trays, is from top to bottom followed successively by rectifying section, bulkhead section and stripping section, in tower
The upper end of partition wall 3 is located at the 15th block of column plate, and lower end is located at the 45th block of column plate.Transalkylation reaction zone 21 is located at feed position
The 20th block of column plate in top is set between the 24th block of column plate, transalkylation reaction zone 22 is located at the 25th block of column plate in feed entrance point lower section extremely
Between 33rd block of column plate.Feed inlet is located at the 25th block of column plate, and the outlet of intermediate species side line is located at the 25th block of column plate, light component
Side line outlet is located at the 5th block of column plate, and the outlet of heavy constituent side line is located at the 50th block of column plate.
The active component of transalkylation catalyst is Y molecular sieve, carrier Al2O3(on the basis of the total amount of catalyst, Y points
The content of son sieve is 80 weight %).Catalyst is placed on column plate with packing pattern.
Mixture 1 containing benzene, ethylbenzene and more ethylbenzene enters divided-wall distillation column from feed inlet and is separated (relative to mixed
The inlet amount of object 1 is closed, the weight (hourly) space velocity (WHSV) of transalkylation catalyst is 15h-1), extraction ethylbenzene (extraction is exported from intermediate species side line
Amount of ethylbenzene is 50010kg/h).The stream vapor isolated by tower top through cooler 9 it is cooling generate low-pressure steam (low-pressure steam
Pressure is 0.04MPa) enter return tank of top of the tower 10 afterwards.Tower top return pump 12 by partial reflux benzene 13 (reflux benzene amount be
209760kg/h) it is sent into divided-wall distillation column；It is remaining that as recycle benzene 14, (amount of recycle benzene is 10925kg/h, and the quality of water contains
Amount is 1370ppm) output.
Extraction benzene (extraction benzene amount is 87025kg/h, and the mass content of water is 36ppm) is exported by light component side line, is led to
It crosses the outlet of heavy constituent side line and produces more ethylbenzene (producing more amount of ethylbenzene is 9500kg/h).Heavy constituent side line outlet extraction will be passed through
The more ethylbenzene in part, which pass through feed inlet together with raw material and recycle together, is sent into divided-wall distillation column that (amount of more ethylbenzene of circulation is
500kg/h)。
By kettle material (produced quantity of kettle material be 5702kg/h, on the basis of the total amount of kettle material, diethylbenzene
Content is sent into more ethylbenzene towers (more ethylbenzene towers are identical as comparative example 1) for 70 weight %) and is separated.
The mass fraction of the benzene of the operating parameter and extraction of divided-wall distillation column and more ethylbenzene towers, ethylbenzene and more ethylbenzene
As shown in table 4, the energy consumption of separative unit is as shown in table 5.
Table 4
| Divided-wall distillation column | More ethylbenzene towers | |
| Tower top operating pressure, kPa (absolute pressure) | 280 | 30 |
| Theoretical cam curve | 60 | 15 |
| Column bottom temperature, DEG C | 240 | 226 |
| Tower bottom reboiler thermic load, kW | 15424 | 471 |
| Tower top cooler thermic load, kW | 23216 | 827 |
| The mass percent of overhead benzene, wt% | 98.0 | - |
| The mass percent of side line benzene, wt% | 99.4 | - |
| The mass percent of side line ethylbenzene, wt% | 99.92 | - |
| The mass percent of the more ethylbenzene of side line, wt% | 95.45 | - |
| The mass percent of the more ethylbenzene of tower top, wt% | - | 96.3 |
Table 5
| Unit | Consumption per hour | Product consumption per ton | The energy consumption of ethylbenzene per ton | |
| Consume high-pressure saturated steam | Ton | 33.86 | 0.677 | 2495.3 |
| Low-pressure steam occurs | Ton | - 36.19 | - 0.724 | - 1666.8 |
| Comprehensive energy consumption | Million is burnt | - | - | 828.5 |
Comparative example 2
This comparative example the difference from embodiment 1 is that, do not loaded in the feed zone of divided-wall distillation column transalkylation catalysis
Agent.
Mixture 1 containing benzene, ethylbenzene and more ethylbenzene enters divided-wall distillation column from feed inlet and is separated, from middle groups
Divide side line outlet extraction ethylbenzene (extraction amount of ethylbenzene is 50010kg/h).The stream vapor isolated by tower top is cooling through cooler 9
It generates low-pressure steam (pressure of low-pressure steam is 0.04MPa) and enters return tank of top of the tower 10 afterwards.Tower top return pump 12 goes back to part
It flows benzene 13 (reflux benzene amount is 209760kg/h) and is sent into divided-wall distillation column；It is remaining that as recycle benzene 14, (amount of recycle benzene is
10925kg/h, the mass content of water are 1385ppm) output.
Extraction benzene (extraction benzene amount is 87025kg/h, and the mass content of water is 36ppm) is exported by light component side line, is led to
It crosses the outlet of heavy constituent side line and produces more ethylbenzene (producing more amount of ethylbenzene is 9500kg/h).Heavy constituent side line outlet extraction will be passed through
The more ethylbenzene in part, which pass through feed inlet together with raw material and recycle together, is sent into divided-wall distillation column that (amount of more ethylbenzene of circulation is
500kg/h)。
By kettle material (produced quantity of kettle material be 5702kg/h, on the basis of the total amount of kettle material, diethylbenzene
Content is sent into more ethylbenzene towers (more ethylbenzene towers are identical as comparative example 1) for 73 weight %) and is separated.
The purity such as table of the benzene of the operating parameter and extraction of divided-wall distillation column and more ethylbenzene towers, ethylbenzene and more ethylbenzene
Shown in 6.
Table 6
| Divided-wall distillation column | More ethylbenzene towers | |
| Tower top operating pressure, kPa (absolute pressure) | 280 | 30 |
| Theoretical cam curve | 60 | 15 |
| Column bottom temperature, DEG C | 240 | 226 |
| Tower bottom reboiler thermic load, kW | 15424 | 385 |
| Tower top cooler thermic load, kW | 22861 | 692 |
| The mass percent of overhead benzene, wt% | 98.0 | - |
| The mass percent of side line benzene, wt% | 99.4 | - |
| The mass percent of side line ethylbenzene, wt% | 99.85 | - |
| The mass percent of the more ethylbenzene of side line, wt% | 95.4 | - |
| The mass percent of the more ethylbenzene of tower top, wt% | - | 96.3 |
Embodiment 1 and comparative example 1 are compared as can be seen that by using method of the invention to containing benzene, ethylbenzene
It is separated with the mixture of more ethylbenzene, separating energy consumption can be substantially reduced；Also, the purity for the ethylbenzene isolated can reach 99.9
Weight % or more.Embodiment 1 is compared with comparative example 2 as can be seen that by setting in the feed zone of divided-wall distillation column
Reaction zone is set, the ethylbenzene of higher purity can be obtained, such as purity is the ethylbenzene of 99.9 weight % or more.
Embodiment 2
Raw material same as Example 1 is separated using process flow same as Example 1 and condition, it is different
It is that light component side take-off benzene amount is different.Concrete technology flow process is as follows.
Mixture 1 containing benzene, ethylbenzene and more ethylbenzene enters divided-wall distillation column from feed inlet and is separated, from middle groups
Divide side line outlet extraction ethylbenzene (extraction amount of ethylbenzene is 50010kg/h).The stream vapor isolated by tower top is cooling through cooler 9
It generates low-pressure steam (pressure of low-pressure steam is 0.04MPa) and enters return tank of top of the tower 10 afterwards.Tower top return pump 12 goes back to part
It flows benzene 13 (reflux benzene amount is 157737kg/h) and is sent into divided-wall distillation column；As recycle benzene 14, (recycle benzene amount is residue
67990kg/h, the mass content 252ppm of water) output.
Extraction benzene (extraction benzene amount is 30000kg/h, and the mass content of water is 32ppm) is exported by light component side line, is led to
It crosses the outlet of heavy constituent side line and produces more ethylbenzene (producing more amount of ethylbenzene is 9500kg/h).Heavy constituent side line outlet extraction will be passed through
The more ethylbenzene in part, which pass through feed inlet together with raw material and recycle together, is sent into divided-wall distillation column that (amount of more ethylbenzene of circulation is
500kg/h)。
By kettle material (produced quantity of kettle material be 5662kg/h, on the basis of the total amount of kettle material, diethylbenzene
Content is sent into more ethylbenzene towers (more ethylbenzene towers are identical as comparative example 1) for 70 weight %) and is separated.
The purity such as table of the benzene of the operating parameter and extraction of divided-wall distillation column and more ethylbenzene towers, ethylbenzene and more ethylbenzene
Shown in 7.
Table 7
| Divided-wall distillation column | More ethylbenzene towers | |
| Tower top operating pressure, kPa (absolute pressure) | 280 | 30 |
| Theoretical cam curve | 60 | 15 |
| Column bottom temperature, DEG C | 241 | 226 |
| Tower bottom reboiler thermic load, kW | 15526 | 467 |
| Tower top cooler thermic load, kW | 23328 | 820 |
| The mass percent of overhead benzene, wt% | 99.1 | - |
| The mass percent of side line benzene, wt% | 99.4 | - |
| The mass percent of side line ethylbenzene, wt% | 99.92 | - |
| The mass percent of the more ethylbenzene of side line, wt% | 95.45 | - |
| The mass percent of the more ethylbenzene of tower top, wt% | - | 96.9 |
Embodiment 3
Raw material same as Example 1 is separated using process flow same as Example 1 and condition, it is different
It is dividing wall column tower top operating pressure.Concrete technology flow process is as follows.
Mixture 1 containing benzene, ethylbenzene and more ethylbenzene enters divided-wall distillation column from feed inlet and is separated, from middle groups
Divide side line outlet extraction ethylbenzene (extraction amount of ethylbenzene is 50010kg/h).The stream vapor isolated by tower top is cooling through cooler 9
It generates low-pressure steam (pressure of low-pressure steam is 0.08MPa) and enters return tank of top of the tower 10 afterwards.Tower top return pump 12 goes back to part
It flows benzene 13 (reflux benzene amount is 240350kg/h) and is sent into divided-wall distillation column；As recycle benzene 14, (recycle benzene amount is residue
10925kg/h, the mass content of water are 1385ppm) output.
Extraction benzene (extraction benzene amount is 87025kg/h, and the mass content of water is 35ppm) is exported by light component side line, is led to
It crosses the outlet of heavy constituent side line and produces more ethylbenzene (producing more amount of ethylbenzene is 50010kg/h).It will be exported and be produced by heavy constituent side line
The more ethylbenzene in part pass through feed inlet together with raw material and recycle together and be sent into divided-wall distillation column that (amount of more ethylbenzene of circulation is
500kg/h)。
By kettle material (produced quantity of kettle material be 5702kg/h, on the basis of the total amount of kettle material, diethylbenzene
Content is sent into more ethylbenzene towers (more ethylbenzene towers are identical as comparative example 1) for 76 weight %) and is separated.
The purity such as table of the benzene of the operating parameter and extraction of divided-wall distillation column and more ethylbenzene towers, ethylbenzene and more ethylbenzene
Shown in 8.
Table 8
| Divided-wall distillation column | More ethylbenzene towers | |
| Tower top operating pressure, kPa (absolute pressure) | 340 | 30 |
| Theoretical cam curve | 60 | 15 |
| Column bottom temperature, DEG C | 250 | 226 |
| Tower bottom reboiler thermic load, kW | 19025 | 435 |
| Tower top cooler thermic load, kW | 25958 | 827 |
| The mass percent of overhead benzene, wt% | 98.2 | - |
| The mass percent of side line benzene, wt% | 99.4 | - |
| The mass percent of side line ethylbenzene, wt% | 99.94 | - |
| The mass percent of the more ethylbenzene of side line, wt% | 95.4 | - |
| The mass percent of the more ethylbenzene of tower top, wt% | - | 96.9 |
Embodiment 4
The separator that the present embodiment uses includes a divided-wall distillation column and ethylbenzene tower more than one.
Using divided-wall distillation column shown in Fig. 1, on the basis of the separative unit of 400,000 tons/year of Benzene Devices, to raw material
It forms material as shown in table 9 to be separated, inlet amount 182664kg/h.
Divided-wall distillation column and transalkylation catalyst and its loadings are same as Example 1.
Mixture 1 containing benzene, ethylbenzene and more ethylbenzene enters divided-wall distillation column from feed inlet and is separated, from middle groups
Divide side line outlet extraction ethylbenzene (extraction amount of ethylbenzene is 50010kg/h).The stream vapor isolated by tower top is cooling through cooler 9
It generates low-pressure steam (pressure of low-pressure steam is 0.04MPa) and enters return tank of top of the tower 10 afterwards.Tower top return pump 12 goes back to part
It flows benzene 13 (reflux benzene amount is 231045kg/h) and is sent into divided-wall distillation column；As recycle benzene 14, (produce benzene amount is residue
10950kg/h, the mass content of water are 1337ppm) output.
Extraction benzene (extraction benzene amount is 107020kg/h, and the mass content of water is 32ppm) is exported by light component side line, is led to
It crosses the outlet of heavy constituent side line and produces more ethylbenzene (producing more amount of ethylbenzene is 50010kg/h).It will be exported and be produced by heavy constituent side line
The more ethylbenzene in part pass through feed inlet together with raw material and recycle together and be sent into divided-wall distillation column that (amount of more ethylbenzene of circulation is
500kg/h)。
By kettle material (produced quantity of kettle material be 5684kg/h, on the basis of the total amount of kettle material, diethylbenzene
Content is sent into more ethylbenzene towers (more ethylbenzene towers are identical as comparative example 1) for 70 weight %) and is separated.
The purity such as table of the benzene of the operating parameter and extraction of divided-wall distillation column and more ethylbenzene towers, ethylbenzene and more ethylbenzene
Shown in 10, the energy consumption of separative unit is as shown in table 11.
9 feed composition of table (mass fraction)
| Water | Non-aromatic component before benzene | Benzene | Toluene | Ethylbenzene | Diethylbenzene | Triethylbenzene (TEB) | Four ethylbenzene | Butylbenzene | Heavy aromatics * |
| 201ppm | 0.003 | 0.642 | 221ppm | 0.274 | 0.071 | 0.005 | 66ppm | 0.003 | 0.002 |
*: boiling point is higher than the aromatic component of four ethylbenzene
Table 10
| Divided-wall distillation column | More ethylbenzene towers | |
| Tower top operating pressure, kPa (absolute pressure) | 280 | 30 |
| Theoretical cam curve | 60 | 15 |
| Column bottom temperature, DEG C | 240 | 226 |
| Tower bottom reboiler thermic load, kW | 15823 | 459 |
| Tower top cooler thermic load, kW | 25466 | 824 |
| The mass percent of overhead benzene, wt% | 98.3 | - |
| The mass percent of side line benzene, wt% | 99.5 | - |
| The mass percent of side line ethylbenzene, wt% | 99.93 | - |
| The mass percent of the more ethylbenzene of side line, wt% | 96.0 | - |
| The mass percent of the more ethylbenzene of tower top, wt% | - | 96.9 |
Table 11
| Unit | Consumption per hour | Product consumption per ton | The energy consumption of ethylbenzene per ton, million is burnt | |
| Consume high-pressure saturated steam | Ton | 35.73 | 0.715 | 2634.3 |
| Low-pressure steam occurs | Ton | - 38.58 | - 0.772 | - 1777.7 |
| Comprehensive energy consumption | Million is burnt | - | - | 856.6 |
Embodiment 5
(1) ethylene and benzene are sent into alkylation reactor in a manner of upstriker, wherein benzene is (for fresh benzene and circulation
The mixture of benzene, recycle benzene are part by the benzene of the overhead extraction of divided-wall distillation column) it with the molar ratio of ethylene is 5:1, relatively
In the inlet amount of benzene, the weight space velocity of catalyst for alkylation reaction is 3.5h-1.Alkylation reactor is four fixed bed reactors
Two catalyst beds are arranged in every reactor for series connection, and the height of each catalyst bed is 2.4 meters, catalyst bed it
Between between be divided into 2 meters, the inlet temperature of each reactor is 210 DEG C, and the outlet pressure of each reactor is 4.0MPa (gauge pressure).
The catalyst for alkylation reaction used is shaped to round bar shape using beta-molecular sieve as active component, with aluminium oxide, with 100 parts by weight
On the basis of catalyst, the content of aluminium oxide is 20 weight %, and the content of beta-molecular sieve is 80 weight %.
(2) separator that the present embodiment uses includes a divided-wall distillation column and ethylbenzene tower more than one.
Using divided-wall distillation column shown in Fig. 1, wherein benzene is all from overhead extraction.With 400,000 tons/year of Benzene Devices
On the basis of separative unit, inlet amount 162662kg/h.
Divided-wall distillation column shares 70 blocks of theoretical trays, and the upper end of partition wall 3 is located at the 20th block of column plate in tower, lower end position
At the 50th block of column plate.Transalkylation reaction zone 21 is located above feed entrance point the 30th block of column plate between the 34th block of column plate, alkane
Group-transfer reaction zone 22 is located at the 35th block of column plate in feed entrance point lower section between the 45th block of column plate.Feed inlet is located at the 35th block of column plate
Place, the outlet of intermediate species side line are located at the 35th block of column plate, and the outlet of light component side line is located at the 6th block of column plate, heavy constituent side line
Outlet is located at the 55th block of column plate.
The active component of transalkylation catalyst is Y molecular sieve, carrier Al2O3(on the basis of the total amount of catalyst, Y points
The content of son sieve is 75 weight %).Catalyst is placed on column plate with packing pattern.
In divided-wall distillation column, the mixture 1 containing benzene, ethylbenzene and more ethylbenzene from feed inlet enter divided-wall distillation column into
(relative to the inlet amount of mixture 1, the weight (hourly) space velocity (WHSV) of transalkylation catalyst is 20h for row separation-1), go out from intermediate species side line
Mouth extraction ethylbenzene (extraction amount of ethylbenzene is 50005kg/h).The stream vapor isolated by tower top generates low pressure through cooler 9 is cooling
Steam (pressure of low-pressure steam is 0.04MPa) enters return tank of top of the tower 10 afterwards.Tower top return pump 12 by partial reflux benzene 13 (time
Stream benzene amount is 127397kg/h) it is sent into divided-wall distillation column；As recycle benzene 14, (amount of recycle benzene is 97998kg/ to remainder
H, the mass content of water are 185ppm) the middle raw material as alkylated reaction of circulation feeding step (1).
The more ethylbenzene isolated pass through heavy constituent side line outlet extraction (producing more amount of ethylbenzene is 10000kg/h).It will pass through
More ethylbenzene (amount of more ethylbenzene of circulation is 1000kg/h) of heavy constituent side line outlet extraction pass through feed inlet one together with raw material
Circulation is played to be sent into divided-wall distillation column.
By kettle material (produced quantity of kettle material be 5659kg/h, on the basis of the total amount of kettle material, diethylbenzene
Content is sent into more ethylbenzene towers for 74 weight %) and is separated.
The purity such as table of the benzene of the operating parameter and extraction of divided-wall distillation column and more ethylbenzene towers, ethylbenzene and more ethylbenzene
Shown in 12.
(3) by the more of the heavy constituent side line outlet extraction of the more ethylbenzene and divided-wall distillation column isolated from more ethylbenzene towers
Ethyl benzene mixtures and benzene (for part by divided-wall distillation column overhead extraction recycle benzene) carry out alkane in transalkylation reactor
Group-transfer reaction, transalkylation reactor are a fixed bed reactors, and there are two catalyst beds for setting in the reactor, often
The height of a catalyst bed is 3 meters, between catalyst bed between be divided into 1.8 meters, the inlet temperature of reactor is 170 DEG C,
Reactor outlet pressure is 2.8MPa (gauge pressure), and the weight ratio of benzene and more ethylbenzene is 4.5:1, relative to the inlet amount of benzene, alkyl
The weight space velocity of transfer reaction activator is 2h-1.Catalyst used in transalkylation reactor is using Y molecular sieve as active group
Point, it is shaped to round bar shape with aluminium oxide, on the basis of 100 part by weight of catalyst, the content of aluminium oxide is 10 weight %, Y point
The content of son sieve is 90 weight %.
More ethylbenzene tower tower bottom output heavy constituents are as Residual oil carrying device.
Table 12
| Divided-wall distillation column | More ethylbenzene towers | |
| Tower top operating pressure, kPa (absolute pressure) | 280 | 30 |
| Theoretical cam curve | 70 | 15 |
| Column bottom temperature, DEG C | 240 | 226 |
| Tower bottom reboiler thermic load, kW | 155201 | 459 |
| Tower top cooler thermic load, kW | 23414 | 824 |
| The mass percent of overhead benzene, wt% | 99.2 | - |
| The mass percent of side line benzene, wt% | - | - |
| The mass percent of side line ethylbenzene, wt% | 99.94 | - |
| The mass percent of the more ethylbenzene of side line, wt% | 95.9 | - |
| The mass percent of the more ethylbenzene of tower top, wt% | - | 96.9 |
Embodiment 6
(1) ethylene and benzene are sent into alkylation reactor in a manner of upstriker, wherein benzene is (for fresh benzene and circulation
The mixture of benzene, recycle benzene are the benzene of divided-wall distillation column overhead extraction) with the molar ratio of ethylene be 5:1, relative to benzene into
Doses, the weight space velocity of catalyst for alkylation reaction are 3.5h-1.Alkylation reactor is four fixed bed reactors series connection, often
Two catalyst beds are set in platform reactor, and the height of each catalyst bed is 2.4 meters, the interval between catalyst bed
It is 2 meters, the inlet temperature of reactor is 210 DEG C, and the outlet pressure of reactor is 4.0MPa (gauge pressure).The alkylated reaction used
Catalyst is shaped to round bar shape using beta-molecular sieve as active component, with aluminium oxide, on the basis of 100 part by weight of catalyst, oxidation
The content of aluminium is 20 weight %, and the content of beta-molecular sieve is 80 weight %.
(2) separator that the present embodiment uses includes a divided-wall distillation column and ethylbenzene tower more than one.
Using divided-wall distillation column shown in Fig. 1, on the basis of the separative unit of 400,000 tons/year of Benzene Devices, inlet amount
For 162662kg/h.
Divided-wall distillation column shares 60 blocks of theoretical trays, and the upper end of partition wall 3 is located at the 15th block of column plate in tower, lower end position
At the 45th block of column plate.Transalkylation reaction zone 21 is located above feed entrance point the 26th block of column plate between the 29th block of column plate, alkane
Group-transfer reaction zone 22 is located at the 30th block of column plate in feed entrance point lower section between the 38th block of column plate.Feed inlet is located at the 30th block of column plate
Place, the outlet of intermediate species side line are located at the 30th block of column plate, and the outlet of light component side line is located at the 6th block of column plate, heavy constituent side line
Outlet is located at the 50th block of column plate.
The active component of transalkylation catalyst is Y molecular sieve, carrier Al2O3(on the basis of the total amount of catalyst, Y points
The content of son sieve is 90 weight %).Catalyst is placed on column plate with packing pattern.
Mixture 1 containing benzene, ethylbenzene and more ethylbenzene enters divided-wall distillation column from feed inlet and is separated (relative to mixed
The inlet amount of object 1 is closed, the weight (hourly) space velocity (WHSV) of transalkylation catalyst is 18h-1), extraction ethylbenzene (extraction is exported from intermediate species side line
Amount of ethylbenzene is 50010kg/h).The stream vapor isolated by tower top through cooler 9 it is cooling generate low-pressure steam (low-pressure steam
Pressure is 0.04MPa) enter return tank of top of the tower 10 afterwards.Tower top return pump 12 by partial reflux benzene 13 (reflux benzene amount be
157737kg/h) it is sent into divided-wall distillation column；As recycle benzene 14, (amount of recycle benzene is 67990kg/h, the matter of water to remainder
Amount content is 225ppm) the middle raw material as alkylated reaction of circulation feeding step (1).
Extraction recycle benzene (produced quantity 30000kg/h, the mass content of water are 100ppm) is exported by light component side line,
Pass through heavy constituent side line outlet extraction (producing more amount of ethylbenzene is 9500kg/h).More second of heavy constituent side line outlet extraction will be passed through
Benzene (amount of more ethylbenzene of circulation is 500kg/h) passes through feed inlet together with raw material and is recycled in feeding divided-wall distillation column together.
By kettle material (produced quantity of kettle material be 5662kg/h, on the basis of the total amount of kettle material, diethylbenzene
Content is sent into more ethylbenzene towers for 74 weight %) and is separated.
The purity such as table of the benzene of the operating parameter and extraction of divided-wall distillation column and more ethylbenzene towers, ethylbenzene and more ethylbenzene
Shown in 13.
(3) by the more of the heavy constituent side line outlet extraction of the more ethylbenzene and divided-wall distillation column isolated from more ethylbenzene towers
The mixture and recycle benzene (for the benzene of the light component side line outlet extraction of divided-wall distillation column) of ethylbenzene are in transalkylation reactor
Transalkylation reaction is carried out, transalkylation reactor is a fixed bed reactors, and there are two catalyst for setting in the reactor
Bed, the height of each catalyst bed are 3 meters, and the inlet temperature of reactor is 170 DEG C, and reactor outlet pressure is 2.8MPa
The weight ratio of (gauge pressure), benzene and more ethylbenzene is 4.5:1, relative to the inlet amount of benzene, the weight of transalkylation catalysts
Air speed is 2h-1.Catalyst used in transalkylation reactor is shaped to round bar using Y molecular sieve as active component, with aluminium oxide
Shape, on the basis of 100 part by weight of catalyst, the content of aluminium oxide is 10 weight %, and the content of Y molecular sieve is 90 weight %.
More ethylbenzene tower tower bottom output heavy constituents are as Residual oil carrying device.
Table 13
| Divided-wall distillation column | More ethylbenzene towers | |
| Tower top operating pressure, kPa (absolute pressure) | 280 | 30 |
| Theoretical cam curve | 60 | 15 |
| Column bottom temperature, DEG C | 241 | 226 |
| Tower bottom reboiler thermic load, kW | 15526 | 435 |
| Tower top cooler thermic load, kW | 23328 | 827 |
| The mass percent of overhead benzene, wt% | 99.1 | - |
| The mass percent of side line benzene, wt% | 99.4 | - |
| The mass percent of side line ethylbenzene, wt% | 99.92 | - |
| The mass percent of the more ethylbenzene of side line, wt% | 95.45 | - |
| The mass percent of the more ethylbenzene of tower top, wt% | - | 96.9 |
Embodiment 5 and 6 as a result, it was confirmed that separator of the invention is coupled with ethylbenzene production plants, can obtain high-purity
The ethylbenzene of degree.
The preferred embodiment of the present invention has been described above in detail, still, during present invention is not limited to the embodiments described above
Detail within the scope of the technical concept of the present invention can be with various simple variants of the technical solution of the present invention are made, this
A little simple variants all belong to the scope of protection of the present invention.
It is further to note that specific technical features described in the above specific embodiments, in not lance
In the case where shield, can be combined in any appropriate way, in order to avoid unnecessary repetition, the present invention to it is various can
No further explanation will be given for the combination of energy.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should also be regarded as the disclosure of the present invention.
Claims (107)
1. a kind of ethylbenzene manufacturing processes, this method includes alkylated reaction step, separating step, optional transalkylation reaction step
Rapid and optional more ethylbenzene separating steps,
In the alkylated reaction step, ethylene is contacted with benzene and is alkylated reaction, obtained containing ethylbenzene, benzene and more second
The mixture of benzene；
In the separating step, at least partly ethylbenzene is isolated from the mixture, is alternatively separated out at least partly benzene
At least partly more ethylbenzene, and part kettle material is optionally sent out into separating step, the isolated method includes will be described
Mixture is sent into divided-wall distillation column and carries out rectifying, and the bulkhead section in the divided-wall distillation column includes adjacent by partition wall
Feed zone and intermediate species lateral line discharging section, the feed zone include feed inlet, the intermediate species lateral line discharging section includes
Intermediate species side line discharge, the mixture enters the divided-wall distillation column by the feed inlet and is separated, from institute
State intermediate species side line outlet extraction ethylbenzene, wherein the feed zone includes at least one reaction zone, and the reaction zone has extremely
A kind of few transalkylation reaction catalyst；
In more ethylbenzene separating steps, at least partly more second are isolated from the kettle material exported by the separating step
Benzene；
In transalkylation reaction step, benzene is contacted with more ethylbenzene and carries out transalkylation reaction, more ethylbenzene are from institute
Separating step and/or more ethylbenzene separating steps are stated, at least partly benzene is optionally in the separating step by light component side
The benzene of line outlet extraction.
2. according to the method described in claim 1, wherein, the feed zone includes the first reaction zone and second reaction zone, described
The lower end present position of first reaction zone is not less than the feed inlet, and the upper end present position of the second reaction zone is not higher than institute
State the lower end present position of the first reaction zone.
3. according to the method described in claim 2, wherein, the theoretical cam curve of first reaction zone lower end present position is
tR1 L, the theoretical cam curve of second reaction zone upper end present position is tR2 U, the theoretical tray of the feed inlet present position
Number is tI, tR1 L/tIFor 0.8-1, tR2 U/tIFor 1-1.2.
4. according to the method described in claim 3, wherein, the theoretical cam curve of the feed inlet present position is anti-with described first
The difference of the theoretical cam curve of the lower end Ying Qu present position is 1, the theoretical cam curve of second reaction zone upper end present position
It is identical as the theoretical cam curve of the feed inlet present position.
5. the method according to any one of claim 2-4, wherein the reason of first reaction zone upper end present position
It is t by the number of platesR1 U, the theoretical cam curve of second reaction zone lower end present position is tR2 L, the feed inlet present position
Theoretical cam curve be tI, tR1 U/tIFor 0.7-0.9, tR2 L/tIFor 1.1-1.5.
6. according to the method described in claim 5, wherein, tR1 U/tIFor 0.8-0.9, tR2 L/tIFor 1.2-1.4.
7. the method according to any one of claim 2-4, wherein the theoretical cam curve of the second reaction zone is preferred
Not less than the theoretical cam curve of the first reaction zone.
8. according to the method described in claim 7, wherein, the theoretical cam curve of the second reaction zone is the reason of the first reaction zone
By 2-3 times of the number of plates.
9. method described in any one of -4 according to claim 1, wherein the transalkylation reaction catalyst is selected to alkane
Group-transfer reaction has the solid acid catalyst of catalytic action.
10. according to the method described in claim 9, wherein, the transalkylation reaction catalyst is molecular sieve.
11. according to the method described in claim 10, wherein, the transalkylation reaction catalyst is Y molecular sieve.
12. method described in any one of -4 according to claim 1, wherein produce more ethylbenzene, institute from the outlet of heavy constituent side line
State the lower end present position that heavy constituent side line outlet present position is not higher than the partition wall.
13. according to the method for claim 12, wherein the theoretical cam curve of heavy constituent side line outlet present position is
tH, the theoretical cam curve of partition wall lower end present position is t2 L, tH/t2 LFor 1-5.
14. according to the method for claim 13, wherein tH/t2 LFor 1-3.5.
15. according to the method for claim 14, wherein tH/t2 LFor 1-2.
16. according to the method for claim 15, wherein tH/t2 LFor 1-1.5.
17. according to the method for claim 12, wherein will be at least partly by more second of heavy constituent side line outlet extraction
Benzene is sent into the divided-wall distillation column together with the mixture.
18. according to the method for claim 17, wherein by the total amount of more ethylbenzene of more ethylbenzene side line outlets extraction
On the basis of, the amount that circulation is sent into more ethylbenzene of the divided-wall distillation column is 0.5-30 weight %.
19. according to the method for claim 18, wherein by the total amount of more ethylbenzene of more ethylbenzene side line outlets extraction
On the basis of, the amount that circulation is sent into more ethylbenzene of the divided-wall distillation column is 1-20 weight %.
20. according to the method for claim 19, wherein by the total amount of more ethylbenzene of more ethylbenzene side line outlets extraction
On the basis of, the amount that circulation is sent into more ethylbenzene of the divided-wall distillation column is 0.8-15 weight %.
21. according to the method for claim 20, wherein by the total amount of more ethylbenzene of more ethylbenzene side line outlets extraction
On the basis of, the amount that circulation is sent into more ethylbenzene of the divided-wall distillation column is 1-10 weight %.
22. according to claim 1 with the method described in any one of 17-21, wherein export extraction benzene from light component side line,
Light component side line outlet present position is higher than the upper end present position of the partition wall.
23. according to the method for claim 22, wherein the theoretical cam curve of light component side line outlet present position is
tL, the theoretical cam curve of partition wall upper end present position is t2 U, tL/t2 UFor 0.05-0.95.
24. according to the method for claim 23, wherein tL/t2 UFor 0.1-0.9.
25. according to the method for claim 24, wherein tL/t2 UFor 0.2-0.6.
26. according to the method for claim 25, wherein tL/t2 UFor 0.3-0.4.
27. method described in any one of -4 and 17-21 according to claim 1, wherein by the tower of the divided-wall distillation column
In the kettle material that bottom obtains, the content of diethylbenzene is 50-90 weight %.
28. according to the method for claim 27, wherein the kettle material obtained by the tower bottom of the divided-wall distillation column
In, the content of diethylbenzene is 60-85 weight %.
29. according to the method for claim 28, wherein the kettle material obtained by the tower bottom of the divided-wall distillation column
In, the content of diethylbenzene is 65-80 weight %.
30. method described in any one of -4 and 17-21 according to claim 1, wherein in the divided-wall distillation column, institute
The theoretical cam curve for stating bulkhead section is t2, the theoretical cam curve of the stripping section below the bulkhead section is t1, it is located at described point
The theoretical cam curve of rectifying section above wall section is t3, total theoretical cam curve of the divided-wall distillation column is t, t1/ t is 0.1-
0.6, t2/ t is 0.1-0.8, t3/ t is 0.1-0.6.
31. according to the method for claim 30, wherein t1/ t is 0.15-0.5, t2/ t is 0.2-0.7, t3/ t is 0.15-
0.5。
32. according to the method for claim 31, wherein t1/ t is 0.2-0.3, t2/ t is 0.4-0.6, t3/ t is 0.2-
0.3。
33. method described in any one of -4 and 17-21 according to claim 1, wherein the theory of the divided-wall distillation column
The number of plates is 30-90.
34. according to the method for claim 33, wherein the theoretical cam curve of the divided-wall distillation column is 40-80.
35. according to the method for claim 34, wherein the theoretical cam curve of the divided-wall distillation column is 50-75.
36. according to the method for claim 35, wherein the theoretical cam curve of the divided-wall distillation column is 60-70.
37. method described in any one of -4 and 17-21 according to claim 1, wherein in divided-wall distillation column, relatively
In the inlet amount of the mixture, the weight (hourly) space velocity (WHSV) of the transalkylation reaction catalyst is 2-120h-1。
38. according to the method for claim 37, wherein the charging in divided-wall distillation column, relative to the mixture
Amount, the weight (hourly) space velocity (WHSV) of the transalkylation reaction catalyst are 4-60h-1。
39. according to the method for claim 38, wherein the charging in divided-wall distillation column, relative to the mixture
Amount, the weight (hourly) space velocity (WHSV) of the transalkylation reaction catalyst are 5-95h-1。
40. according to the method for claim 39, wherein the charging in divided-wall distillation column, relative to the mixture
Amount, the weight (hourly) space velocity (WHSV) of the transalkylation reaction catalyst are 10-40h-1。
41. method described in any one of -4 and 17-21 according to claim 1, wherein the tower top of the divided-wall distillation column
Pressure is 142-420kPa, and column bottom temperature is 225-275 DEG C, and the tower top pressure is gauge pressure；
When not passing through light component side line outlet extraction benzene, by weight percentage, the reflux of the divided-wall distillation column tower top
Than for 0.8-3；
When through light component side line outlet extraction benzene, to enter the total amount of benzene in the mixture that divided-wall distillation column is separated
On the basis of, the amount by the benzene of light component side line outlet extraction is 10-70 weight %, by weight percentage, the reflux of tower top
Than for 1-10.
42. according to the method for claim 41, wherein the tower top pressure of the divided-wall distillation column is 150-380kPa,
Column bottom temperature is 235-265 DEG C, and the tower top pressure is gauge pressure.
43. according to the method for claim 42, wherein the tower top pressure of the divided-wall distillation column is 200-360kPa,
The tower top pressure is gauge pressure.
44. according to the method for claim 43, wherein the tower top pressure of the divided-wall distillation column is 260-350kPa,
The tower top pressure is gauge pressure.
45. according to the method for claim 41, wherein when not passing through light component side line outlet extraction benzene, with weight hundred
Divide than meter, the reflux ratio of the divided-wall distillation column tower top is 0.85-2.
46. according to the method for claim 45, wherein when not passing through light component side line outlet extraction benzene, with weight hundred
Divide than meter, the reflux ratio of the divided-wall distillation column tower top is 1-1.5.
47. according to the method for claim 41, wherein when through light component side line outlet extraction benzene, separated with entering
In the mixture that wall rectifying column is separated on the basis of the total amount of benzene, the amount by the benzene of light component side line outlet extraction is 10-
35 weight %, by weight percentage, the reflux ratio of tower top are 1.5-5.
48. according to the method for claim 47, wherein when through light component side line outlet extraction benzene, with weight percent
Than meter, the reflux ratio of tower top is 1.5-3.
49. according to the method described in claim 1, wherein, in the alkylated reaction step, the molar ratio of ethylene and benzene is 1:
1-15。
50. according to the method for claim 49, wherein in the alkylated reaction step, the molar ratio of ethylene and benzene is
2-10:1.
51. according to the method for claim 50, wherein in the alkylated reaction step, the molar ratio of ethylene and benzene is
2-8:1.
52. method according to claim 51, wherein in the alkylated reaction step, the molar ratio of ethylene and benzene is
3-6:1.
53. according to claim 1 with the method described in any one of 49-52, wherein in the alkylated reaction step, second
Alkene is contacted in the presence of at least one catalyst for alkylation reaction with benzene, and the catalyst for alkylation reaction is selected from solid acid
Catalyst.
54. method according to claim 53, wherein the catalyst for alkylation reaction is molecular sieve.
55. method according to claim 54, wherein the catalyst for alkylation reaction is beta-molecular sieve.
56. according to claim 1 with the method described in any one of 49-52, wherein in the alkylated reaction step, instead
The inlet temperature for answering device is 100-400 DEG C, and the outlet pressure of reactor is 0.1-10MPa, and the pressure is gauge pressure.
57. method according to claim 56, wherein in the alkylated reaction step, the inlet temperature of reactor is
150-350 DEG C, the outlet pressure of reactor is 1-5MPa, and the pressure is gauge pressure.
58. method according to claim 57, wherein in the alkylated reaction step, the inlet temperature of reactor is
180-300℃；The outlet pressure of reactor is 2-4MPa, and the pressure is gauge pressure.
59. a kind of for producing the device of ethylbenzene, which includes alkylated reaction unit, separative unit, optional more ethylbenzene
Separative unit and optional transalkylation reaction unit,
The alkylated reaction unit is used to ethylene and benzene haptoreaction obtaining the mixture containing benzene, ethylbenzene and more ethylbenzene；
The separative unit optionally divides for isolating at least partly ethylbenzene from the mixture that alkylated reaction unit exports
More ethylbenzene and benzene are separated out, optionally exports part kettle material；
More ethylbenzene separative units from the kettle material that separative unit exports for isolating more ethylbenzene；
The transalkylation reaction unit carries out transalkylation reaction, more ethylbenzene come from for contacting benzene with more ethylbenzene
In the separative unit and/or more ethylbenzene separative units；
The separative unit includes divided-wall distillation column subelement, for being separated to the mixture, the partition wall essence
The bulkhead section for evaporating tower includes the feed zone abutted by partition wall and product discharge section, and the feed zone is provided with for will be described
Mixture introduces the feed inlet of the divided-wall distillation column, and the product discharge section is provided with the midbarrel side for producing ethylbenzene
Line outlet, the divided-wall distillation column are optionally provided with the outlet of the light component side line for producing benzene and for producing more second
The heavy constituent side line of benzene exports, and heavy constituent side line outlet present position is not higher than the lower end present position of the partition wall,
Light component side line outlet present position is higher than the upper end present position of the partition wall, which is characterized in that the feed zone
Including at least one reaction zone, the reaction zone has transalkylation reaction catalyst.
60. device according to claim 59, wherein the feed zone includes the first reaction zone and second reaction zone, institute
The lower end present position of the first reaction zone is stated not less than the feed inlet, the upper end present position of the second reaction zone is not higher than
The lower end present position of first reaction zone.
61. the device according to claim 59 or 60, wherein the theoretical tray of first reaction zone lower end present position
Number is tR1 L, the theoretical cam curve of second reaction zone upper end present position is tR2 U, the theory of the feed inlet present position
The number of plates is tI, tR1 L/tIFor 0.8-1, tR2 U/tIFor 1-1.2.
62. device according to claim 61, wherein the theoretical cam curve of the feed inlet present position and described first
The difference of the theoretical cam curve of reaction zone lower end present position is 1, the theoretical tray of second reaction zone upper end present position
Number is identical as the theoretical cam curve of the feed inlet present position.
63. the device according to claim 59 or 60, wherein the theoretical tray of first reaction zone upper end present position
Number is tR1 U, the theoretical cam curve of second reaction zone lower end present position is tR2 L, the theory of the feed inlet present position
The number of plates is tI, tR1 U/tIFor 0.7-0.9, tR2 L/tIFor 1.1-1.5.
64. device according to claim 63, wherein tR1 U/tIFor 0.8-0.9, tR2 L/tIFor 1.2-1.4.
65. the device according to claim 59 or 60, wherein the transalkylation reaction catalyst is selected to transalkylation
React the solid acid catalyst with catalytic action.
66. device according to claim 65, wherein the transalkylation reaction catalyst is molecular sieve.
67. device according to claim 66, wherein the transalkylation reaction catalyst is Y molecular sieve.
68. device according to claim 59, wherein the theoretical cam curve of heavy constituent side line outlet present position is
tH, the theoretical cam curve of partition wall lower end present position is t2 L, tH/t2 LFor 1-5；
The theoretical cam curve of light component side line outlet present position is tL, the theoretical tower of partition wall upper end present position
Plate number is t2 U, tL/t2 UFor 0.05-0.95.
69. device according to claim 68, wherein tH/t2 LFor 1-3.5, tL/t2 UFor 0.1-0.9.
70. device according to claim 69, wherein tH/t2 LFor 1-2, tL/t2 UFor 0.2-0.6.
71. device according to claim 70, wherein tH/t2 LFor 1-1.5, tL/t2 UFor 0.3-0.4.
72. the device according to any one of claim 59 and 68-71, wherein described in the divided-wall distillation column
The theoretical cam curve of bulkhead section is t2, the theoretical cam curve of the stripping section below the bulkhead section is t1, it is located at the bulkhead
The theoretical cam curve of the rectifying section of Duan Shangfang is t3, total theoretical cam curve of the divided-wall distillation column is t, t1/ t is 0.1-
0.6, t2/ t is 0.1-0.8, t3/ t is 0.1-0.6.
73. the device according to claim 72, wherein t1/ t is 0.15-0.5, t2/ t is 0.2-0.7, t3/ t is 0.15-
0.5。
74. the device according to claim 73, wherein t1/ t is 0.2-0.3, t2/ t is 0.4-0.6, t3/ t is 0.2-
0.3。
75. the device according to any one of claim 59 and 68-71, wherein the theory of the divided-wall distillation column
The number of plates is 30-90.
76. the device according to claim 75, wherein the theoretical cam curve of the divided-wall distillation column is 40-80.
77. the device according to claim 76, wherein the theoretical cam curve of the divided-wall distillation column is 50-75.
78. the device according to claim 77, wherein the theoretical cam curve of the divided-wall distillation column is 60-70.
79. the device according to any one of claim 59 and 68-71, wherein the separative unit further includes more second
Benzene recycles subelement, at least partly more ethylbenzene that the more ethylbenzene circulation subelements are used to isolate divided-wall distillation column with from
The mixture of alkylated reaction unit output is sent into divided-wall distillation column together.
80. the device according to any one of claim 59 and 68-71, wherein the device further includes benzene cycling element,
At least partly benzene for exporting separative unit is sent into alkylated reaction unit and/or transalkylation reaction unit.
81. a kind of method for producing ethylbenzene, this method carries out in the device described in any one of claim 59-80, packet
It includes:
By ethylene and benzene in alkylated reaction unit haptoreaction, obtain the mixture containing benzene, ethylbenzene and more ethylbenzene；
In separative unit, at least partly ethylbenzene is isolated from the mixture that alkylated reaction unit exports, is alternatively separated
More ethylbenzene and benzene out optionally export part kettle material；
In more ethylbenzene separative units, more ethylbenzene are isolated from the kettle material that separative unit exports；
In transalkylation reaction unit, benzene is contacted with more ethylbenzene, carry out transalkylation reaction, more ethylbenzene are that separation is single
At least partly more ethylbenzene that at least partly more ethylbenzene and/or more ethylbenzene separative units that member is isolated are isolated.
82. the method according to claim 81, wherein in the alkylated reaction unit, by ethylene and benzene with molar ratio
It is contacted for 1:1-15.
83. the method according to claim 82, wherein in the alkylated reaction unit, by ethylene and benzene with molar ratio
It is contacted for 2-10:1.
84. the method according to claim 83, wherein in the alkylated reaction unit, by ethylene and benzene with molar ratio
It is contacted for 2-8:1.
85. the method according to claim 84, wherein in the alkylated reaction unit, by ethylene and benzene with molar ratio
It is contacted for 3-6:1.
86. the method according to any one of claim 81-85, wherein in the alkylated reaction step, ethylene with
Benzene is contacted in the presence of at least one catalyst for alkylation reaction, and the catalyst for alkylation reaction is selected from solid acid catalysis
Agent.
87. the method according to claim 86, wherein in the alkylated reaction step, the alkylated reaction catalysis
Agent is molecular sieve.
88. the method according to claim 87, wherein in the alkylated reaction step, the alkylated reaction catalysis
Agent is beta-molecular sieve.
89. the method according to any one of claim 81-85, wherein in the alkylated reaction step, reactor
Inlet temperature be 100-400 DEG C, the outlet pressure of reactor is 0.1-10MPa, and the pressure is gauge pressure.
90. the method according to claim 89, wherein in the alkylated reaction step, the inlet temperature of reactor is
150-350 DEG C, the outlet pressure of reactor is 1-5MPa, and the pressure is gauge pressure.
91. the method according to claim 90, wherein in the alkylated reaction step, the inlet temperature of reactor is
180-300 DEG C, the outlet pressure of reactor is 2-4MPa, and the pressure is gauge pressure.
92. the method according to any one of claim 81-85, wherein from the heavy constituent side line of divided-wall distillation column
Outlet produces more ethylbenzene, will be at least partly sent into together with the mixture by more ethylbenzene of heavy constituent side line outlet extraction
In the divided-wall distillation column.
93. the method according to claim 92, wherein by the total amount of more ethylbenzene of more ethylbenzene side line outlets extraction
On the basis of, the amount that circulation is sent into more ethylbenzene of the divided-wall distillation column is 0.5-30 weight %.
94. the method according to claim 93, wherein by the total amount of more ethylbenzene of more ethylbenzene side line outlets extraction
On the basis of, the amount that circulation is sent into more ethylbenzene of the divided-wall distillation column is 1-20 weight %.
95. the method according to claim 94, wherein by the total amount of more ethylbenzene of more ethylbenzene side line outlets extraction
On the basis of, the amount that circulation is sent into more ethylbenzene of the divided-wall distillation column is 0.8-15 weight %.
96. the method according to claim 95, wherein by the total amount of more ethylbenzene of more ethylbenzene side line outlets extraction
On the basis of, the amount that circulation is sent into more ethylbenzene of the divided-wall distillation column is 1-10 weight %.
97. the method according to any one of claim 81-85, wherein from the light component side line of divided-wall distillation column
Extraction benzene in outlet at least partly will be sent into alkylated reaction unit and/or transalkylation reaction unit by benzene.
98. the method according to any one of claim 81-85, wherein obtained by the tower bottom of the divided-wall distillation column
To kettle material in, the content of diethylbenzene is 50-90 weight %.
99. the method according to claim 98, wherein the kettle material obtained by the tower bottom of the divided-wall distillation column
In, the content of diethylbenzene is 60-85 weight %.
100. the method according to claim 99, wherein the kettle material obtained by the tower bottom of the divided-wall distillation column
In, the content of diethylbenzene is 65-80 weight %.
101. the method according to any one of claim 81-85, wherein in divided-wall distillation column, relative to institute
The inlet amount of mixture is stated, the weight (hourly) space velocity (WHSV) of the transalkylation reaction catalyst is 2-120h-1。
102. method described in 01 according to claim 1, wherein in divided-wall distillation column, relative to the mixture into
Doses, the weight (hourly) space velocity (WHSV) of the transalkylation reaction catalyst are 5-95h-1。
103. method described in 02 according to claim 1, wherein in divided-wall distillation column, relative to the mixture into
Doses, the weight (hourly) space velocity (WHSV) of the transalkylation reaction catalyst are 10-40h-1。
104. the method according to any one of claim 81-85, wherein the tower top pressure of the divided-wall distillation column
For 142-420kPa, column bottom temperature is 225-275 DEG C, and the tower top pressure is gauge pressure；
When not passing through light component side line outlet extraction benzene, by weight percentage, the reflux of the divided-wall distillation column tower top
Than for 0.8-3；
When through light component side line outlet extraction benzene, to enter the total amount of benzene in the mixture that divided-wall distillation column is separated
On the basis of, the amount by the benzene of light component side line outlet extraction is 10-70 weight %, by weight percentage, the reflux of tower top
Than for 1-10.
105. method described in 04 according to claim 1, wherein the tower top pressure of the divided-wall distillation column is 150-
380kPa, column bottom temperature are 235-265 DEG C, and the tower top pressure is gauge pressure；
When not passing through light component side line outlet extraction benzene, by weight percentage, the reflux of the divided-wall distillation column tower top
Than for 0.85-2；
When through light component side line outlet extraction benzene, to enter the total amount of benzene in the mixture that divided-wall distillation column is separated
On the basis of, the amount by the benzene of light component side line outlet extraction is 10-35 weight %, by weight percentage, the reflux of tower top
Than for 1.5-5.
106. method described in 05 according to claim 1, wherein the tower top pressure of the divided-wall distillation column is 200-
360kPa, the tower top pressure are gauge pressure；
When not passing through light component side line outlet extraction benzene, by weight percentage, the reflux of the divided-wall distillation column tower top
Than for 1-1.5；
When through light component side line outlet extraction benzene, by weight percentage, the reflux ratio of tower top is 1.5-3.
107. method described in 06 according to claim 1, wherein the tower top pressure of the divided-wall distillation column is 260-
350kPa, the tower top pressure are gauge pressure.
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| US7498472B2 (en) * | 2007-05-23 | 2009-03-03 | Uop Llc | Process for producing ethylbenzene |
| US7525003B2 (en) * | 2007-05-23 | 2009-04-28 | Uop Llc | Process for producing ethylbenzene |
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| CN102188832A (en) * | 2010-03-03 | 2011-09-21 | 中国石油化工股份有限公司 | Separation column body for reaction distillation |
| CN104027995B (en) * | 2013-05-30 | 2015-11-25 | 中石化上海工程有限公司 | The method of Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system |
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|---|---|---|---|---|
| US7498472B2 (en) * | 2007-05-23 | 2009-03-03 | Uop Llc | Process for producing ethylbenzene |
| US7525003B2 (en) * | 2007-05-23 | 2009-04-28 | Uop Llc | Process for producing ethylbenzene |
| CN101429089A (en) * | 2007-11-07 | 2009-05-13 | 中国石油化工股份有限公司 | Bulkhead type rectification column for separating materials containing ethylbenzene and vinyl benzene |
| CN102188832A (en) * | 2010-03-03 | 2011-09-21 | 中国石油化工股份有限公司 | Separation column body for reaction distillation |
| CN104027995B (en) * | 2013-05-30 | 2015-11-25 | 中石化上海工程有限公司 | The method of Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system |
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