CN101429089A - Bulkhead type rectification column for separating materials containing ethylbenzene and vinyl benzene - Google Patents
Bulkhead type rectification column for separating materials containing ethylbenzene and vinyl benzene Download PDFInfo
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- CN101429089A CN101429089A CNA200710047887XA CN200710047887A CN101429089A CN 101429089 A CN101429089 A CN 101429089A CN A200710047887X A CNA200710047887X A CN A200710047887XA CN 200710047887 A CN200710047887 A CN 200710047887A CN 101429089 A CN101429089 A CN 101429089A
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Abstract
The invention relates to a bulkhead type rectifying tower used for separation material containing styrene and phenylethane , and mainly solves the technical problems of large number of styrene rectifying towers, large investment, high energy consumption, long heating time of the styrene and severe aggregation loss in the prior production process of the styrene. The bulkhead type rectifying tower well solves the technical problems through adopting the technical proposal that the bulkhead rectifying tower comprises a separation section under a bulkhead section, the bulkhead section and a separation section above the bulkhead section; a material inlet is positioned on one side of the bulkhead section; a material outlet for heavy compositions is arranged on the bottom of the separation section under the bulkhead section; the bulkhead section is provided with at least one outlet of product styrene; and the separation section above the bulkhead section is provided with at least one outlet of product phenylethane; the top of the separation section above the bulkhead section is also provided with an outlet for light compositions; the bulkhead section is provided with at least one clapboard to divide the bulkhead section into at least two zones along axial direction; and column plates or stuffing is arranged inside each zone. The bulkhead type rectifying tower solves the technical problems well and can be used in industrial production of producing the styrene by dehydrogenating the phenylethane.
Description
Technical field
The present invention relates to a kind of bulkhead type rectification column that is used to contain ethylbenzene, vinylbenzene feed separation, particularly be used for from containing the bulkhead type rectification column that ethylbenzene separates ethylbenzene, vinylbenzene simultaneously with styrene stream and saves investment and energy about a kind of.
Background technology
Vinylbenzene is one of most important alkene, and 99% vinylbenzene all obtains by the ethylbenzene dehydrogenation production technique.The Technology of dehydrogenation of ethylbenzene to styrene mainly contains adiabatic dehydrogenation technology, isothermal dehydrogenating technology and dehydrogenation selective oxidation processes.Wherein ripe, the most most widely used is negative pressure adiabatic dehydrogenation technology.The energy consumption of production of styrene process mainly concentrates on reaction member, rectification cell and general facilities part (mainly being the energy consumption of water coolant and air cooler).The dehydrogenation reaction of ethylbenzene is the thermo-negative reaction of carrying out under than (～1.3) and high-temperature (～600 ℃) at bigger water, and isolating pure vinylbenzene from the reaction product that reactor comes out generally needs 3～4 rectifying tower.The isolating 3 tower flow processs of vinylbenzene are to isolate ethylbenzene and the light component lower than ethylbenzene boiling point at first rectifying tower (crude styrene tower) cat head earlier, by second rectifying tower ethylbenzene is separated with light component again, ethylbenzene loops back reactor as charging, the crude styrene that the first rectifying tower still obtains in the 3rd rectifying tower again rectifying obtain styrene product from cat head, the tower still obtains heavy components such as isopropyl benzene, p-Diethylbenzene, tert-butyl catechol, α-vinyl toluene, no sulphur stopper, styrene oligomer and tar.Because vinylbenzene at normal temperatures promptly can polymerization, and 10 ℃ of its polymerization velocitys of the every rising of temperature promptly double, so the process need of rectifying and separating phenylethylene is operated under the rectifying tower of high vacuum, high number of theoretical plate and big reflux ratio condition, energy consumption is very big, and needs to consume a large amount of water coolants.The crude styrene tower is the tower of energy consumption maximum, and its low-pressure steam consumption accounts for 38% of whole production of styrene device, and cooling water amount accounts for 33% of whole device, and comprehensive energy consumption accounts for 30% of whole device.
Recovery at the low-temperature heat quantity of crude styrene cat head, all carried out number of research projects both at home and abroad, having proposed the multiple technologies scheme, is indirect cycle heat pump techniques, double tower variable-pressure rectification power-saving technology, azeotropic heat recovery technology and the second class lithiumbromide heat pump techniques of compression working medium comprising the heat pump techniques of: vapo(u)r blasting technology, open steam compression, with water.
Sulzer reported adopt vapo(u)r blasting technology, steam directly compression the heat pump distillation technology and be that the indirect cycle heat pump techniques of compression working medium carries out the energy-conservation technology of rectifying raw styrene tower (Hydrocarbon Processing, 1998.12) with water.The vapo(u)r blasting energy-saving effect is not obvious, but invests low; The heat pump distillation technical energy saving of open steam compression is effective, but needs to increase compressor.(cat head absolute pressure 8～12KPa), and reflux ratio is up to about 7, so the suction port flow of vapour compressor is very big, needs huge compressor and needs at least three grades of compressions could be with the cat head heat recuperation because the crude styrene tower adopts negative-pressure operation.This formula investing is big, and compressor power consumption height has limited its using value, especially more can use large-scale styrene device.CN102732 also discloses similar heat pump distillation technology.Though employing is the indirect heat pump distillation technology of working medium with water the compression ratio of compressor is reduced, the investment of compressor is still very big, so this technology also fails to be used widely.US4628136 and CN108625 disclose the energy-conservation technology of mixture that the azeotropic of a kind of overhead vapours vaporization reactor charging ethylbenzene that utilizes the crude styrene tower and water is formed, when adopting this technology, the crude styrene tower top pressure need be increased to 50～170KPa has enough temperature heads to guarantee cat head interchanger both sides, can make the low-pressure steam of saving 90% vaporization ethylbenzene and water like this.Owing to need the working pressure of rising crude styrene tower, so service temperature also can correspondingly raise,, need to increase the consumption of stopper if will avoid the excessive polymerization losses of vinylbenzene, this will partly offset energy-conservation economic benefit.US6171449 discloses a kind of variable-pressure rectification power-saving technology, its technical essential is toluene contained in the mixture flow of autoreactor earlier in the future and removes than the low-boiling light component of toluene, remaining logistics is divided into two stocks does not in proportion enter two rectifying tower that working pressure is different, with the overhead vapours of high top pressure operation rectifying tower thermal source as low voltage operated rectifying Tata still, compare with common rectification process and can save energy 40%～50%, but vinylbenzene need be heated three times in this rectification process, increased cinnamic polymerization losses, increased a rectifying tower simultaneously, flow process is complicated, and investment has also increased greatly.
Though more than various technical schemes the energy consumption of phenyl ethylene rectification is decreased, but all do not change need be heated present situation more than 2 times of vinylbenzene, and the not minimizing of table of equipment number, some technical scheme also will increase facility investment because of reclaiming heat.
The bulkhead rectifying tower is by establishing a vertical wall at rectifying tower middle part, with tower be divided into epimere, hypomere, the integrated tower of complete heat of the rectifying feed zone that separates by dividing plate and the tetrameric novel texture of rectifying extraction section a kind of.With the bulkhead rectifying tower ternary mixture being separated into pure product only needs a tower, a reboiler, a condenser and a reflux splitter, and energy consumption and facility investment can be minimized.Therefore, the application of bulkhead rectifying tower in recent years is more and more.US5335504 and US5709780 disclose a kind of technology that adopts bulkhead rectifying tower Separation and Recovery carbonic acid gas; European patent EP 1413571, EP1371633 and U.S. Pat 20030230476 disclose a kind of technology that adopts the bulkhead rectifying tower to separate TDI; Uop Inc. has applied for the novel process of multinomial employing bulkhead rectifying tower, discloses the technology that adopts bulkhead rectifying tower separation simulation moving-bed fractionation by adsorption isomerization high-octane rating raffinate as US6395950, US6395951, US6407303 and US6472578; US6483002 and US6552242 disclose the technology that adopts bulkhead rectifying tower Separation and Recovery desorbing agent; Uop Inc. has also applied for being used for the bulkhead rectifying tower technology (US6417420) of alkylbenzene production and the bulkhead distillation technology (US6540907 and US20030116474) of whole-distillate gasoline desulfurization simultaneously.In addition, bulkhead rectifying tower technology α-, (US20020183565), tetrahydrofuran (THF)/gamma-butyrolactone/1 in the production process of beta unsaturated alcohol, (US20030106786), C in the sepn process of 4-butyleneglycol
5+In the separation of fraction (US20030230476), 1,6-hexylene glycol/1, in the separation of 5-hexylene glycol/hexanolactam (US20040040829), 1, in the sepn process of 3-divinyl (US20040065538, US20040045804) and the production of trimethoxy propane (US20040267055), high-purity trivinyl diamines (US20040220046) all obtained application in producing.US20050211541 also discloses a kind of bulkhead distillation technology that is used for separating the production of propylene oxide solvent for use with US20050245037.Total about 70 the above bulkhead rectifying tower in the whole world have carried out commercial operation at present.Though can adopt the bulkhead rectifying tower of any a plurality of side line extraction in theory, industrialized in fact divided wall column has only a side line discharging, and is located at a bulkhead section side opposite with opening for feed.Conventional side line discharging is not appeared in the newspapers as yet with the bulkhead rectifier unit that the discharging of bulkhead section side line combines, do not see the bulkhead rectifying tower is used for the isolating report of vinylbenzene yet, more do not see the technology report that adopts bulkhead rectifying tower while separation and purification ethylbenzene and two kinds of products of vinylbenzene.
In above-mentioned existing vinylbenzene isolation technique, all adopt independent knockout tower commercial benzene ethene and reclaim ethylbenzene, need at least three knockout towers, investment is big, the energy consumption height; Vinylbenzene repeatedly is heated in rectifying, and polymerization losses is big; And the concentration of styrene in the vinylbenzene treating tower still discharge material is up to 40%, and the vinylbenzene loss is big; Contain vinylbenzene in the ethylbenzene that reclaims, ethylbenzene purity is low, and concentration expressed in percentage by weight has only 97～98%, has not only lost vinylbenzene, and the ethylbenzene of recovery is worked the mischief to the catalyzer that reactive system uses when recycling.
Summary of the invention
Technical problem to be solved by this invention is in the existing cinnamic production process, phenyl ethylene rectification control tower number is many, investment is big, energy consumption is high and the vinylbenzene heated time is long, polymerization losses is serious, reclaim the low technical problem of ethylbenzene purity, and a kind of new bulkhead type rectification column that is used to contain ethylbenzene, vinylbenzene feed separation is provided.Separate with this bulkhead type rectification column and to contain ethylbenzene and cinnamic material has less investment, the low and high advantage of product purity of energy consumption.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of bulkhead type rectification column that is used to contain ethylbenzene, vinylbenzene feed separation comprises the following segregation section of bulkhead section, bulkhead section and the above segregation section of bulkhead section from the bottom up successively; Material inlet is positioned at bulkhead section one side, and the following segregation section of bulkhead section bottom is provided with the material outlet of heavy component; The bulkhead section is provided with the cinnamic outlet of at least one product; On the above segregation section of bulkhead section, be provided with the outlet of a product ethylbenzene at least; The above segregation section of bulkhead section top also is provided with the outlet of light component; The bulkhead section is provided with a dividing plate at least, vertically the bulkhead section is divided at least two districts, and inside, these two districts all is provided with column plate or filler.
In the technique scheme, the dividing plate in the bulkhead type rectification column is installed or is not installed along the tower medullary ray along the tower medullary ray.Bulkhead type rectification column has 100～150 theoretical stages, and the bulkhead section has 40～70 theoretical stages, and the above segregation section of bulkhead section has 20～60 theoretical stages, and the following segregation section of bulkhead section has 5～30 theoretical stages.The above segregation section of bulkhead section of preferred bulkhead type rectification column has 35～55 theoretical stages, and the following segregation section of bulkhead section has 5～20 theoretical stages.Contain ethylbenzene, cinnamic stock liquid enters from the middle part opening for feed of bulkhead type rectification column bulkhead section one side, from removed overhead than the low-boiling light component of ethylbenzene; Extract ethylbenzene out from the outlet side line of the above segregation section ethylbenzene of bulkhead section.Remove oligopolymer, tar and other heavy component heavier than vinylbenzene from the tower still of bulkhead type rectification column, vinylbenzene is from the opposite side middle and lower part extraction of bulkhead section dividing plate.It is several from the top down the 10th～15 theoretical stages of the above segregation section of bulkhead section that ethylbenzene is extracted a mouthful optimum seeking site scheme out; Vinylbenzene outlet preferred version is several the 5th～20 theoretical stages that make progress from the dividing plate bottom.
When the method that adopts rectifying is separated the concentration of mixture that the material more than three kinds forms and middle distillate when big, adopting conventional order separation process still is that all inevitable middle distillate of backward separation process axially produces remix along tower, this is disadvantageous on thermodynamics, is equivalent to the waste of a part of separation work.The bulkhead rectifying tower is equivalent to an integrated rectifying tower of heat fully on thermodynamics, different is that the bulkhead rectifying tower is only used a tower shell, by the centre fire wall is set and realizes that the complete heat of rectifying is integrated.Charging is in a side of separator segment, middle distillate part in the charging is entered the opposite side of dividing plate by the upper end of dividing plate with light component, another part is then entered the opposite side of dividing plate by the lower end of dividing plate with heavy component, thereby make middle distillate obtain enrichment at the opposite side of dividing plate, avoid the remix of middle distillate in tower, thereby realized effect energy-conservation and raising intermediates purity.Simultaneously, owing to the bulkhead rectifying tower only adopt a tower shell realize two conventional distillations function, the investment also can significantly reduce.
Adopt technology of the present invention, the concentration of styrene in the extraction of bulkhead type rectification column top is by weight less than 200ppm, and the concentration of styrene in the cat head extraction logistics is about 1% or higher by weight percentage when adopting common rectification under vacuum; Concentration of styrene is minimum by weight percentage in the tower still extraction of bulkhead rectifying tower can be low to moderate about 1.5%, and the concentration of styrene in the logistics of tower still is about 40% by weight percentage when adopting common rectification under vacuum.This shows the loss of adopting the bulkhead distillation technology can significantly reduce the phenyl ethylene rectification process.Adopt a divided wall column can finish the separation task of three common rectifying towers, saved investment greatly.Simultaneously, adopt the bulkhead distillation technology to compare with adopting common rectification under vacuum, tower still thermal load and cat head refrigeration duty can reduce by 15～30%, and the purity of styrene product 〉=99.8%.Therefore, adopt technology of the present invention can solve technical problem in the existing phenyl ethylene rectification technology preferably, obtained better technical effect.
Description of drawings
Accompanying drawing 1 is existing phenyl ethylene rectification technology typical process example.
Accompanying drawing 3 is the vertical views in A-A cross section in the accompanying drawing 2.
Pump and heat transmission equipment have also been omitted among Fig. 1 and Fig. 2. In the bulkhead rectifying shown in Figure 2 filler has been installed, although in the tower Liquid distribution trough and redistributor do not draw, but do not need in the rectifying tower with bulkhead not represent.
Among Fig. 11 is the rectifying raw styrene tower, the 2nd, and ethylbenzene tower, the 3rd, styrene treating column; Logistics 101 is to contain benzene second The ethylbenzene dehydrogenation product of alkene, except containing styrene, it is low also to contain the light component such as part ethylbenzene, toluene, benzene and a small amount of styrene The heavy components such as the diethylbenzene of polymers, reaction by-product, tar; The 102nd, the discharging of crude styrene cat head, mainly contain ethylbenzene, Toluene, the low-boiling light component of benzene geometric ratio ethylbenzene and a small amount of styrene; The 103rd, weight concentration is greater than 95% crude styrene, Also have the heavy components such as a small amount of styrene oligomer, the diethylbenzene that reacts by-product, tar, polymerization inhibitor; Polymerization inhibitor is from 1 tower Cat head adds, and is not shown in FIG.; The 104th, the light component such as toluene and benzene; The 105th, ethylbenzene loops back reactor as raw material; The 106th, weight concentration is greater than 99.7% styrene product; The 107th, the diethylbenzene of styrene oligomer, reaction by-product, The heavy component such as tar, polymerization inhibitor.
Among Fig. 2 22 is rectifying tower with bulkheads, and logistics 201 is chargings of rectifying tower with bulkhead, 101 among composition and Fig. 1 Identical, 202 with accompanying drawing 1 in 102 identical, the 203rd, styrene product, the 204th, the tower reactor discharging of rectifying tower with bulkhead, group One-tenth is the heavy components such as styrene oligomer, the diethylbenzene that reacts by-product, tar, polymerization inhibitor.
301 is tower walls among Fig. 3, the 302nd, and demarcation strip. Demarcation strip among the figure three is installed along the tower center line, but in fact Also can eccentricly install.
Below in conjunction with accompanying drawing the present invention is elaborated.
In Fig. 1, contain cinnamic material liquid 101 and enter tower 1 middle part. Tower 1 is a rectifying column that operates under negative pressure, The about 12KPa of tower top pressure, 85～100 of theoretical stages, reflux ratio is about 7. Isolate ethylbenzene and ratio by the cat head of this tower The light component logistics 102 that the ethylbenzene boiling point is lower obtains concentration expressed in percentage by weight greater than 95% crude styrene thing by the tower reactor of this tower Stream 103. The 102 middle part chargings by the tower 2 of micro-pressure operation contain toluene, benzene and than toluene boiling point by tower 2 top extraction Lower light component logistics 104, by the tower reactor extraction concentration expressed in percentage by weight of tower 2 greater than 99% ethylbenzene stream 105,105 Loop back reaction system. Tower 2 has 50 theoretical stages, and reflux ratio is about 6. The tower reactor discharging 103 of tower 1 enters tower 3 The middle part, and contain the styrene concentration expressed in percentage by weight greater than 99.7% styrene product 106, by tower by the overhead extraction of tower 3 3 tower reactor extraction contain the logistics 107 of the heavy components such as styrene oligomer, the diethylbenzene that reacts by-product, tar, polymerization inhibitor, Also contain a certain amount of styrene in 107. Tower 3 also is the rectifying column of a negative-pressure operation, and operating pressure is close with tower 1, 45 theoretical stages are arranged, reflux ratio about 0.8. For reducing cinnamic polymerization losses, in the overhead reflux of tower 1 and tower 3, add Enter an amount of polymerization inhibitor, not shown in FIG..
In Fig. 2, form intermediate membrane one side that the stock liquid 201 identical with logistics 101 among Fig. 1 enters bulkhead rectifying tower 22, the bulkhead rectifying tower has 90～150 theoretical stages, and respectively there are 40～70 theoretical stages the dividing plate both sides.20～60 theoretical stages are arranged more than the baffle region of bulkhead rectifying tower, 35～55 theoretical stages are preferably arranged.5～40 theoretical stages are arranged below the baffle region of bulkhead rectifying tower, 5～20 theoretical stages are preferably arranged.The bulkhead rectifying tower is operated under negative pressure, and the working pressure scope is 1～101KPa, and preferred working pressure is 5～50KPa.The bulkhead rectifying tower be 5～20, preferred reflux ratio scope is that the tower 1 in 6.0～13 operating reflux ratios and the accompanying drawing 1 is close.Cat head extraction by the bulkhead rectifying tower contains ethylbenzene, toluene, benzene and the light component logistics 202 lower than ethylbenzene boiling point, wherein contains small amounts of styrene; Differ from the middle part or the middle and lower part extraction styrene product 203 of charging one side by the bulkhead partition in tower, the tower still extraction of bulkhead rectifying tower contains styrene oligomer, the diethylbenzene, tar of reaction by-product, the heavy component logistics 204 that stopper geometric ratio vinylbenzene boiling point is high, and logistics 205 is ethylbenzene product.
The invention will be further elaborated below by embodiment.Raw material used in all comparative examples and embodiment is formed as shown in table 1.
Table 1 contains the weight of ethylbenzene, styrene stream and forms
Embodiment
[comparative example]
Adopting flow process shown in Figure 1, is that the device in 150,000 tons of vinylbenzene every year is a benchmark with throughput, and the material as shown in table 1 to the raw material weight percentage composition separates, and the operational condition and the separating resulting of each tower are all listed in the table 2.The cat head thermal load is the refrigeration duty of overhead condenser in the table, and tower still thermal load is the thermal load of tower still reboiler.
Table 2150Kt/a styrene device rectifying separation result
Wherein the total heat exchange load of the cat head of tower 1 and tower 3 is-17579.66 kilowatts, and tower still total heat duties is 17415.78 kilowatts.
[embodiment 1]
Adopting flow process shown in Figure 2, is that the device in 150,000 tons of vinylbenzene every year is a benchmark with throughput, and the material as shown in table 1 to the raw material weight percentage composition separates.The bulkhead rectifying tower that adopts has 120 theoretical stages, and respectively there are 65 theoretical stages bulkhead section dividing plate both sides, and the lower partition segregation section has 10 theoretical stages, and working pressure is 12KPa, and the trim the top of column ratio is 200.Separating resulting is listed in the table 3.
[embodiment 2]
Adopt flow process shown in Figure 2, other condition is constant, changes number of theoretical plate and the working pressure and the reflux ratio of the dividing plate both sides of bulkhead rectifying tower.The number of theoretical plate of bulkhead section dividing plate both sides is increased to 70, and working pressure is 138 for the 5KPa reflux ratio.For ease of comparing, separating resulting is also listed in the table 3.
[embodiment 3]
With flow process shown in Figure 2, other condition changes bulkhead rectifying tower theoretical stage and working pressure with embodiment 1.Divided wall column premier's opinion progression becomes 150, and working pressure becomes 50KPa, and for ease of comparing, separating resulting is also listed in the table 3.
[embodiment 4]
Adopt flow process shown in Figure 2, feed conditions just adopts the bulkhead type rectification column of 100 theoretical stages with embodiment 1, and the number of theoretical plate of dividing plate both sides is 45, and reflux ratio is increased to 185, and working pressure is 5KPa.For ease of comparing, separating resulting is also listed in the table 3.
Table 3 adopts the vinylbenzene separation simulation calculation result of bulkhead distillation technology
Adopt the bulkhead rectifying tower to be equivalent to tower in the former technology 1 and tower 3 have been synthesized a tower, under the situation of operation conditions optimization, cat head can save energy 20%, and the tower still can save energy 14%.Simultaneously, under the arbitrary operational condition shown in the embodiment, the purity of ethylbenzene is greater than 99%, and the overhead benzene ethylene loss is also much smaller than former technology.
Claims (9)
1, a kind of bulkhead type rectification column that is used to contain ethylbenzene, vinylbenzene feed separation comprises the following segregation section of bulkhead section, bulkhead section and the above segregation section of bulkhead section from the bottom up successively; Material inlet is positioned at bulkhead section one side, and the following segregation section of bulkhead section bottom is provided with the material outlet of heavy component; The bulkhead section is provided with the cinnamic outlet of at least one product; On the above segregation section of bulkhead section, be provided with the outlet of a product ethylbenzene at least; The above segregation section of bulkhead section top also is provided with the outlet of light component; The bulkhead section is provided with a dividing plate at least, vertically the bulkhead section is divided at least two districts, and inside, these two districts all is provided with column plate or filler.
2, the bulkhead type rectification column that is used to contain ethylbenzene, vinylbenzene feed separation according to claim 1 is characterized in that the dividing plate in the tower is installed or do not installed along the tower medullary ray along the tower medullary ray.
3, the bulkhead type rectification column that is used to contain ethylbenzene, vinylbenzene feed separation according to claim 1, it is characterized in that bulkhead type rectification column has 100～150 theoretical stages, the bulkhead section has 40～70 theoretical stages, the above segregation section of bulkhead section has 20～60 theoretical stages, and the following segregation section of bulkhead section has 5～30 theoretical stages.
4, the bulkhead type rectification column that is used to contain ethylbenzene, vinylbenzene feed separation according to claim 3 is characterized in that the above segregation section of bulkhead section of bulkhead type rectification column has 35～55 theoretical stages.
5, the bulkhead type rectification column that is used to contain ethylbenzene, vinylbenzene feed separation according to claim 3 is characterized in that the following segregation section of bulkhead section of bulkhead type rectification column has 5～20 theoretical stages.
6, the bulkhead type rectification column that is used to contain ethylbenzene, vinylbenzene feed separation according to claim 1 is characterized in that stock liquid enters from the middle part opening for feed of bulkhead type rectification column bulkhead section one side, from removed overhead than the low-boiling light component of ethylbenzene; Extract ethylbenzene out from the outlet side line of the above segregation section ethylbenzene of bulkhead section.
7, the bulkhead type rectification column that is used to contain ethylbenzene, vinylbenzene feed separation according to claim 1, it is characterized in that removing oligopolymer, tar and other heavy component heavier than vinylbenzene from the tower still of bulkhead type rectification column, vinylbenzene is from the opposite side middle and lower part extraction of bulkhead section dividing plate.
8, the bulkhead type rectification column that is used to contain ethylbenzene, vinylbenzene feed separation according to claim 1 is characterized in that it is several from the top down the 10th～15 theoretical stages of the above segregation section of bulkhead section that ethylbenzene is extracted a mouthful position out.
9, the bulkhead type rectification column that is used to contain ethylbenzene, vinylbenzene feed separation according to claim 1 is characterized in that the vinylbenzene outlet is several the 5th～20 theoretical stages that make progress from the dividing plate bottom.
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| CN104016823A (en) * | 2013-03-01 | 2014-09-03 | 中石化上海工程有限公司 | Method for separating ethylbenzene and styrene mixture |
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| DE10233387A1 (en) * | 2002-07-23 | 2004-02-12 | Basf Ag | Process for the continuous distillation of oxiranes, especially propylene oxide |
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