CN101633597B - Method for saving energy in rectification of styrene - Google Patents
Method for saving energy in rectification of styrene Download PDFInfo
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- CN101633597B CN101633597B CN200810032924A CN200810032924A CN101633597B CN 101633597 B CN101633597 B CN 101633597B CN 200810032924 A CN200810032924 A CN 200810032924A CN 200810032924 A CN200810032924 A CN 200810032924A CN 101633597 B CN101633597 B CN 101633597B
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Abstract
The invention relates to a method for saving energy in rectification of styrene. The method aims to solve the technical problems existing in the prior production of the styrene that the rectification of styrene is big in investment and high in energy consumption, and that the polymerization losses caused when the styrene is repeatedly heated are huge. The method comprise the following steps of: taking a mixture of ethylbenzene and styrene as a raw material; allowing the raw material to enter one side of a bulkhead segment of a bulkhead rectification tower for separation to obtain a styrene material flow I on the other side of the bulkhead segment, obtain heavy components such as tar and the like on the bottom part of a separation segment below the bulkhead segment of the bulkhead rectification tower and obtain the ethylbenzene containing the material flow II on the top part of the separation segment above the bulkhead segment of the bulkhead rectification tower; and allowing the material flow II to enter the middle part of an ethylbenzene recycling tower for separation to obtain the ethylbenzene on the bottom part of the ethylbenzene recycling tower and obtain light components on the top part of the ethylbenzene recycling tower. The technical scheme solves the technical problems. The method can be applied to separation and purification of the styrene in a process of producing the styrene by ethylbenzene dehydrogenation.
Description
Technical field
The present invention relates to a kind of phenyl ethylene rectification power-economizing method, particularly about a kind of from contain ethylbenzene, styrene stream separation and purification ethylbenzene and vinylbenzene and practice thrift the rectificating method of investment and energy.
Background technology
Vinylbenzene is one of most important alkene, and 99% vinylbenzene all obtains through 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 the most ripe, to use the widest be 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 from the reaction product that reactor drum comes out, isolating pure vinylbenzene 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; Through second rectifying tower ethylbenzene is separated with light component again; Ethylbenzene loops back reactor drum 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, alpha-methyl styrene, 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 maximum tower of energy consumption, and its LP 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.Because the crude styrene tower is under high vacuum, to operate, so the hot grade of cat head is lower, tower top temperature is merely about 71 ℃, is difficult to utilize, and all adopts the mode of water-cooled heat exchange at present, does not reclaim the heat of this part.Because it is this part tow taste heat is very big,, very favourable with the increase economic benefit to the energy consumption that reduces the production of styrene process if can fully utilize this part heat energy.
Recovery to 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 second type of 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 the compressor power consumption is high, 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, therefore should technology also fail 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 employing should 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 LP steam of practicing thrift 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 get into two rectifying tower that working pressure is different, with the overhead vapours of the 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, has increased cinnamic polymerization losses, has 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 the vinylbenzene present situation more than 2 times of need being heated; 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 through 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 condensing surface and a reflux splitter, and energy consumption and facility investment can be minimized.Therefore, the applied more and more of bulkhead rectifying tower in recent years.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 isomerizing high-octane rating raffinate like 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 korenyl production and the bulkhead distillation technology (US6540907 and US20030116474) of whole-distillate gasoline desulfurization simultaneously.In addition, bulkhead rectifying tower technology α-, (US20020183565), 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-pinakon/1; In the separation of 5-pinakon/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, but Shang Weijian is used for the isolating report of vinylbenzene with the bulkhead rectifying tower.
In above-mentioned existing vinylbenzene stripping technique, all adopt independent knockout tower commercial benzene ethene and reclaim ethylbenzene, need at least three knockout towers, investment is big, and energy consumption is high; 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 that the phenyl ethylene rectification energy consumption that exists in the prior art is high, and the problem that the vinylbenzene loss is big provides a kind of new phenyl ethylene rectification power-economizing method.It is high that this method has the vinylbenzene recovery, advantage of low energy consumption.
In order to solve the problems of the technologies described above, the technical scheme that the present invention adopts is following: a kind of power-economizing method of phenyl ethylene rectification may further comprise the steps:
A) with contain ethylbenzene, cinnamic mixture is a raw material; Raw material at first gets into bulkhead section one side of a bulkhead rectifying tower; Through separating; Opposite side in the bulkhead section gets styrene stream I, gets the tar heavy component in the following segregation section of bulkhead rectifying tower bulkhead section bottom, must contain the stream I I of ethylbenzene at the above segregation section of bulkhead rectifying tower bulkhead section top;
B) stream I I gets into the middle part of ethylbenzene regenerating column, through separating, gets ethylbenzene in the bottom of ethylbenzene regenerating column, gets light component at the top of ethylbenzene regenerating column.
In the technique scheme, containing cinnamic weight percentage in the liquid stock is 20～93%, and the weight percentage of light component is 0.1～10%, and the weight percentage of heavy component is 1～20%; Preferred version is that to contain cinnamic weight percentage in the liquid stock be 40～70%, and the weight percentage of heavy component is 1～10%.The bulkhead rectifying tower has 80～150 theoretical stages, and the bulkhead section has 30～70 theoretical stages, and the above segregation section of bulkhead rectifying tower bulkhead section has 20～60 theoretical stages, and 5～30 theoretical stages of segregation section are arranged below the bulkhead rectifying tower bulkhead section; Preferred version is that the above segregation section of bulkhead rectifying tower bulkhead section has 35～55 theoretical stages, and the following segregation section of bulkhead rectifying tower bulkhead section has 5～20 theoretical stages.The working pressure of bulkhead rectifying tower is 1.0～101KPa, and bulkhead rectifying tower cat head reflux ratio by weight is 5～20; Preferred version is that the working pressure of bulkhead rectifying tower is 5～50KPa, and bulkhead rectifying tower cat head reflux ratio by weight is 6.5～13.The material feeding mouth is positioned at the middle part of bulkhead rectifying tower bulkhead section one side, and the extraction mouth of styrene product is positioned at the middle and lower part of the opposite side of bulkhead rectifying tower bulkhead section; Preferred version is that styrene product is extracted mouth out and is positioned at 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, through 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 got into the opposite side of dividing plate by the upper end of dividing plate with light component; Another part is then got into the opposite side of dividing plate by the lower end of dividing plate with heavy component; Thereby make middle distillate obtain enrichment, avoided the remix of middle distillate in tower, thereby realize energy-conservation effect at the opposite side of dividing plate.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 rectifying tower top is merely about 200ppm, and the concentration of styrene about 1% in the cat head extraction logistics when adopting common rectification under vacuum; Concentration of styrene is merely about 10% in the tower still extraction of bulkhead rectifying tower, and the concentration of styrene about 40% in the logistics of tower still when adopting common rectification under vacuum.This shows the loss of adopting the bulkhead distillation technology can significantly reduce the phenyl ethylene rectification process.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 25～30%.The purity of styrene product >=99.8%.Therefore, adopt technology disclosed by the invention can solve the 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 2 is phenyl ethylene rectification technical process typical cases of the present invention.
Attach and omitted pump and heat-exchange equipment among Fig. 1 and 2.
In the accompanying drawing 11 is the rectifying raw styrene tower, the 2nd, and ethylbenzene tower, the 3rd, vinylbenzene treating tower; Logistics 101 is to contain cinnamic ethylbenzene dehydrogenation product, except that containing vinylbenzene, also contains heavy components such as light component such as part ethylbenzene, toluene, benzene and small amounts of styrene oligopolymer, the diethylbenzene that reacts by-product, tar; The 102nd, the discharging of crude styrene cat head mainly contains ethylbenzene, toluene, the low-boiling light component of benzene geometric ratio ethylbenzene and small amounts of styrene; The 103rd, weight concentration is greater than 95% crude styrene, also has the heavy components such as diethylbenzene, tar, stopper of small amounts of styrene oligopolymer, reaction by-product; Stopper adds from the cat head of 1 tower, does not draw among the figure; The 104th, light component such as toluene and benzene; The 105th, ethylbenzene loops back reactor drum as raw material; The 106th, weight concentration is greater than 99.7% styrene product; The 107th, heavy components such as the diethylbenzene of styrene oligomer, reaction by-product, tar, stopper.
In the accompanying drawing 2 22 is bulkhead rectifying tower, the 33rd, and the ethylbenzene regenerating column.Logistics 201 is chargings of bulkhead rectifying tower, form with Fig. 1 in 101 identical, 202 with accompanying drawing 1 in 102 identical; The 203rd, styrene product; The 204th, the tower still discharging of bulkhead rectifying tower, composition is heavy components such as styrene oligomer, the diethylbenzene that reacts by-product, tar, stopper, the 205th, the light component of the cat head of ethylbenzene regenerating column; Be benzene and toluene main the composition, the 206th, and the ethylbenzene that reclaims.
Below in conjunction with accompanying drawing the present invention is elaborated.
In accompanying drawing 1, contain cinnamic liquid stock 101 and get into tower 1 middle part.Tower 1 is a rectifying tower of under negative pressure, operating, the about 12KPa of tower top pressure, and 85～100 of theoretical stages, reflux ratio is about 7.Isolate ethylbenzene and the light component logistics 102 lower by the cat head of this tower, obtain concentration expressed in percentage by weight greater than 95% crude styrene logistics 103 by the tower still of this tower than ethylbenzene boiling point.The 102 middle part chargings by the tower 2 of micro-pressure operation contain toluene, benzene and the light component logistics 104 lower than toluene boiling point by tower 2 top extraction, loop back reactive system by the tower still extraction concentration expressed in percentage by weight of tower 2 greater than 99% ethylbenzene stream 105,105.Tower 2 has 50 theoretical stages, and reflux ratio is about 6.The tower still discharging 103 of tower 1 gets into the middle part of tower 3; And contain the vinylbenzene concentration expressed in percentage by weight greater than 99.7% styrene product 106 by the cat head extraction of tower 3; Contain by tower 3 tower still extraction in the logistics 107,107 of heavy components such as diethylbenzene, tar, stopper of styrene oligomer, reaction by-product and also contain a certain amount of vinylbenzene.Tower 3 also is the rectifying tower of a negative-pressure operation, and working pressure is close with tower 1, and 45 theoretical stages are arranged, reflux ratio about 0.8.For reducing cinnamic polymerization losses, in the trim the top of column of tower 1 and tower 3, add an amount of stopper, do not draw among the figure.
In accompanying drawing 2, form with accompanying drawing 1 in intermediate membrane one side of the identical liquid stocks 201 entering bulkhead rectifying tower 22 of logistics 101, the bulkhead rectifying tower has 90～150 theoretical stages, 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 the diethylbenzene, tar of styrene oligomer, reaction by-product, the heavy component logistics 204 that stopper geometric ratio vinylbenzene boiling point is high.Logistics 202 gets into the middle part of ethylbenzene regenerating column 33 and isolates light component such as benzene and toluene from 33 cat head, and the tower still Separation and Recovery from 33 gets ethylbenzene.
Through embodiment the present invention is done further elaboration below.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
| The component title | The C6 hydrocarbon | Benzene | Toluene | Ethylbenzene | Vinylbenzene | Tar | Many ethylbenzene | Water |
| Weight percentage, % | 0.2 | 0.3 | 1.5 | 36.3 | 58.9 | 1.3 | 1.4 | 0.1 |
Embodiment
[comparative example]
Adopting the flow process shown in the accompanying drawing 1, is that the annual device of 150,000 tons of vinylbenzene 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.Wherein the cat head thermal load is the heat exchange load of overhead condenser, and tower still thermal load is the heat exchange load of tower bottom reboiler, down together.
Table 2150Kt/a styrene device rectifying separation result
| Device number in the accompanying drawing 1 | 1 | 2 | 3 |
| The cat head working pressure, kPa | 12 | 156 | 12 |
| Stage number | 100 | 50 | 43 |
| Reflux ratio | 6.77 | 6 | 0.8 |
| The overhead benzene ethylene concentration, weight % | 0.011 | 0 | 0.9975 |
| Tower still concentration of styrene, weight % | 0.9550 | 0.0082 | 0.385 |
| The cat head ethylbenzene concentration, weight % | 0.9721 | 1ppm | 0.001 |
| Tower still ethylbenzene concentration, weight % | 0.0011 | 0.9758 | 0 |
| The cat head thermal load, kilowatt | -12771.26 | -663.95 | -4808.40 |
| Tower still thermal load, kilowatt | 13156.40 | 1815.00 | 4259.38 |
[embodiment 1]
Adopting the flow process shown in the accompanying drawing 2, is that the annual device of 150,000 tons of vinylbenzene 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 bulkhead section the lower partition segregation section has 10 theoretical stages, and working pressure is 12KPa, and the trim the top of column ratio is 6.5.The result lists in the table 3.
[embodiment 2]
Adopt the flow process shown in the accompanying drawing 2, other condition changes the total number of theoretical plate of bulkhead rectifying tower and number of theoretical plate and the working pressure and the reflux ratio of bulkhead section dividing plate both sides with embodiment 1.Total number of theoretical plate is increased to 150, and the number of theoretical plate of bulkhead section dividing plate both sides is increased to 70, and dividing plate segregation section up and down respectively has 40 theoretical stages, and working pressure is 13 for the 50KPa reflux ratio.For ease of comparing, the result also lists in the table 3.
[embodiment 3]
Adopt the flow process shown in the accompanying drawing 2, other condition changes the reflux ratio and the working pressure of bulkhead rectifying tower with embodiment 2.Reflux ratio is reduced to 6, and working pressure is reduced to 5KPa, and for ease of comparing, the result also lists in the table 3.
[embodiment 4]
Adopt the flow process shown in the accompanying drawing 2, feed conditions adopts the bulkhead rectifying tower of 90 theoretical stages with embodiment 2, and the number of theoretical plate of bulkhead section dividing plate both sides is 40, and reflux ratio is increased to 13, and working pressure is 5KPa.For ease of comparing, the result also lists in the table 3.
Table 3 adopts the vinylbenzene separating resulting of bulkhead distillation technology
| The embodiment sequence number | 1 | 2 | 3 | 4 |
| Main stage number | 120 | 150 | 150 | 90 |
| The baffle region number of theoretical plate | 65 | 70 | 70 | 40 |
| Working pressure, kPa | 12 | 50 | 5 | 5 |
| The king-tower reflux ratio | 6.5 | 13 | 6 | 13 |
| The overhead benzene ethylene concentration, weight % | 0.04％ | 0.07％ | 0.2％ | 0.24％ |
| Tower still concentration of styrene, weight % | 1.6％ | 1.2％ | 1.9％ | 3.4％ |
| Side is adopted vinylbenzene purity, weight % | 99.85％ | 99.95％ | 99.80％ | 99.71％ |
| The cat head thermal load, kilowatt | -12739.11 | -25478.97 | -12178.70 | -20017.50 |
| Tower still thermal load, kilowatt | 13065.39 | 25130.82 | 12287.92 | 20298.57 |
The energy consumption of bulkhead rectifying tower cat head and tower still should be compared with the cat head and the tower still total energy consumption of tower in the former technology 1 and tower 3 in the table 3, because bulkhead rectifying tower has played the effect of two common rectifying towers simultaneously.In former technology, tower 1 is-17579.66 kilowatts with the total heat exchange load of tower 3 cats head, and the total heat exchange load of tower still is 17415.78 kilowatts.Adopt technology of the present invention, under the processing condition of optimum, cat head can save energy 30%, and the tower still can save energy 29%.
Claims (9)
1. the power-economizing method of a phenyl ethylene rectification may further comprise the steps:
A) with contain ethylbenzene, cinnamic mixture is a raw material; Raw material at first gets into bulkhead section one side of a bulkhead rectifying tower; Through separating; Opposite side in the bulkhead section gets styrene stream I, gets the tar heavy component in the following segregation section of bulkhead rectifying tower bulkhead section bottom, must contain the stream I I of ethylbenzene at the above segregation section of bulkhead rectifying tower bulkhead section top;
B) stream I I gets into the middle part of ethylbenzene regenerating column, through separating, gets ethylbenzene in the bottom of ethylbenzene regenerating column, gets light component at the top of ethylbenzene regenerating column; Except that containing vinylbenzene, also contain the diethylbenzene and the tar heavy constituent of part ethylbenzene, toluene, benzene light constituent and small amounts of styrene oligopolymer, reaction by-product in the wherein said raw material.
2. the power-economizing method of phenyl ethylene rectification according to claim 1, it is characterized in that containing in the liquid stock cinnamic weight percentage is 20～93%, and the weight percentage of light component is 0.1～10%, and the weight percentage of heavy component is 1～20%.
3. the power-economizing method of phenyl ethylene rectification according to claim 2, it is characterized in that containing in the liquid stock cinnamic weight percentage is 40～70%, the weight percentage of heavy component is 1～10%.
4. the power-economizing method of phenyl ethylene rectification according to claim 1; It is characterized in that the bulkhead rectifying tower has 80～150 theoretical stages; The bulkhead section has 30～70 theoretical stages; The above segregation section of bulkhead rectifying tower bulkhead section has 20～60 theoretical stages, and the following segregation section of bulkhead rectifying tower bulkhead section has 5～30 theoretical stages.
5. the power-economizing method of phenyl ethylene rectification according to claim 4 is characterized in that the above segregation section of bulkhead rectifying tower bulkhead section has 35～55 theoretical stages, and the following segregation section of bulkhead rectifying tower bulkhead section has 5～20 theoretical stages.
6. the power-economizing method of phenyl ethylene rectification according to claim 1, the working pressure that it is characterized in that the bulkhead rectifying tower is 1.0～101KPa, bulkhead rectifying tower cat head reflux ratio by weight is 5～20.
7. the power-economizing method of phenyl ethylene rectification according to claim 6, the working pressure that it is characterized in that the bulkhead rectifying tower is 5～50KPa, bulkhead rectifying tower cat head reflux ratio by weight is 6.5～13.
8. the power-economizing method of phenyl ethylene rectification according to claim 1 is characterized in that the material feeding mouth is positioned at the middle part of bulkhead rectifying tower bulkhead section one side, and the extraction mouth of styrene product is positioned at the middle and lower part of the opposite side of bulkhead rectifying tower bulkhead section.
9. the power-economizing method of phenyl ethylene rectification according to claim 8 is characterized in that styrene product extracts mouth out and be positioned at several the 5th～20 theoretical stages that make progress from the dividing plate bottom.
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| CN102372614B (en) * | 2010-08-23 | 2014-01-22 | 中国石油化工股份有限公司 | Production method of polyoxymethylene dimethylether |
| 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 |
| 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 |
| KR102387476B1 (en) | 2017-11-17 | 2022-04-14 | 주식회사 엘지화학 | Process for Purification of Raffinate-2 streams |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2471134A (en) * | 1946-07-17 | 1949-05-24 | Standard Oil Dev Co | Fractionation apparatus |
| CN85102732A (en) * | 1984-04-26 | 1986-10-15 | 新日铁化学株式会社 | The distillating method of styrenic |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2471134A (en) * | 1946-07-17 | 1949-05-24 | Standard Oil Dev Co | Fractionation apparatus |
| CN85102732A (en) * | 1984-04-26 | 1986-10-15 | 新日铁化学株式会社 | The distillating method of styrenic |
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