CN101348412B - Energy-saving method for phenyl ethylene rectification - Google Patents
Energy-saving method for phenyl ethylene rectification Download PDFInfo
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- CN101348412B CN101348412B CN2007100439606A CN200710043960A CN101348412B CN 101348412 B CN101348412 B CN 101348412B CN 2007100439606 A CN2007100439606 A CN 2007100439606A CN 200710043960 A CN200710043960 A CN 200710043960A CN 101348412 B CN101348412 B CN 101348412B
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Abstract
The invention relates to an energy-saving method for the rectification of a material flow containing ethyl benzene and styrene, mainly solving the technical problems in the prior production process of styrene of long flow of a rectification separation process, large investment, high energy consumption and great loss of styrene. The energy-saving method solves the technical problems better throughadopting the technical proposal comprising the following steps that a mixture containing ethyl benzene and styrene is taken as a raw material; the raw material is fed into one side of a bulkhead section of a bulkhead rectification tower at first, and styrene is obtained through separation at the other side of the bulkhead section; meanwhile, heavy compositions such as tar are obtained at the bottom of a separation section under the bulkhead section of the bulkhead rectification tower, and contain a small amount of styrene; a vapor phase material flow I is obtained at the top of a separation section above the bulkhead section of the bulkhead rectification tower; moreover, the material flow I undergoes heat exchange with a mixture consisting of a material flow II, a material flow III and a material flow IV at first; then, a part of the material flow I is circulated to the top of the separation section above the bulkhead section of the bulkhead rectification tower, while the other part is fed into the middle part of an ethyl benzene recovery tower; and finally, toluene and a light composition with the boiling point lower than that of toluene are obtained at the top of the ethyl benzene recovery tower, and ethyl benzene is obtained at the bottom of the ethyl benzene recovery tower. In addition, the energy-saving method can be used in the industrial production of separation and refining of styrene during manufacturing styrene through ethyl benzene dehydrogenation.
Description
Technical field
The present invention relates to a kind of power-economizing method that is used for phenyl ethylene rectification, particularly about a kind of from contain ethylbenzene, styrene stream separation and purification ethylbenzene and vinylbenzene and save the rectificating method of investment and energy.
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 the light component lower than ethylbenzene boiling point again, ethylbenzene loops back reactor as charging, the crude styrene that the first rectifying tower still obtains rectifying again in the 3rd rectifying tower, and obtaining 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.Because the crude styrene tower is to operate under high vacuum, so the hot grade of cat head is lower, tower top temperature only is 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 to energy consumption and the increase economic benefit that reduces the production of styrene process if can fully utilize this part heat energy.In addition, although the crude styrene tower has adopted high efficiency packing and has operated under high vacuum, because the boiling-point difference between ethylbenzene and the vinylbenzene only is 9 ℃, volatilization is to very low relatively, and the overhead benzene ethylene loss of crude styrene tower is bigger in the existing rectification process, and state-of-the-art level is also about 1%, this part vinylbenzene will loop back reactor with ethylbenzene in the process that reclaims ethylbenzene, not only make the purity drop of ethylbenzene, and polymerization in reaction process, coking, catalyst deactivation is accelerated.The vinylbenzene loss of crude styrene tower still is also very big, and wherein cinnamic concentration expressed in percentage by weight is up to 40%, and the other unit of needs increase reclaims vinylbenzene wherein, has further increased the complicacy of investment and technology.
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, if will avoid the excessive polymerization losses of vinylbenzene, need to increase the consumption of stopper, this will partly offset energy-conservation economic benefit, and simultaneously, vinylbenzene still needs to be heated twice in rectifying in this technology, in the hot-zone residence time long, further increased cinnamic polymerization losses.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.In addition, it only is about 97.5% that this multitower flow process is separated the ethylbenzene purity that obtains, and wherein also contains a certain amount of vinylbenzene, and the inactivation of these vinylbenzene meeting accelerator activator after looping back reactor increases production cost.
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-, (US20030106786), C in the sepn process of (US20020183565), tetrahydrofuran (THF)/γ-butyrolactone/1,4-butyleneglycol in the production process of beta unsaturated alcohol
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, but Shang Weijian is used for the isolating report of vinylbenzene with the bulkhead rectifying tower, also do not see bulkhead distillation technology and low temperature heat energy are reclaimed the technical literature report of associating use.
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 the phenyl ethylene rectification flow process complexity that exists in the prior art, and investment is big, the energy consumption height, and ethylbenzene purity is low, and the problem that the vinylbenzene loss is big provides a kind of new power-economizing method that is used for phenyl ethylene rectification.It is simple that this method has flow process, less investment, and ethylbenzene purity height, the vinylbenzene loss is few, advantage of low 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 power-economizing method that is used for phenyl ethylene rectification may further comprise the steps:
A) with contain ethylbenzene, cinnamic mixture is a raw material, raw material at first enters bulkhead section one side of bulkhead rectifying tower, gets vinylbenzene through being separated in bulkhead section opposite side, must contain the heavy component of tar in the following segregation section of bulkhead rectifying tower bulkhead section bottom; The vapor phase stream I that must contain ethylbenzene at the above segregation section of bulkhead rectifying tower bulkhead section top;
B) stream I elder generation and the mixture heat exchange of forming by stream I I, stream I II and stream I V, part is circulated to the top of the above segregation section of bulkhead rectifying tower bulkhead section then, another part enters the middle part of ethylbenzene recovery tower, through separating, get toluene and the boiling point light component lower at the top of ethylbenzene recovery tower, at the bottom of the ethylbenzene recovery tower, get ethylbenzene than toluene;
Wherein stream I I is a liquid phase circulation ethylbenzene, and stream I II is fresh ethylbenzene, and stream I V is a water.
In the technique scheme, containing the ethylbenzene weight percentage in the stock liquid is 5～60%, cinnamic weight percentage is 20～93%, also contain in the raw material than low-boiling light component of vinylbenzene and the heavy component higher than vinylbenzene boiling point, wherein 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 the ethylbenzene weight percentage in the stock liquid be 20～50%, and cinnamic weight percentage is 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 the following segregation section of bulkhead rectifying tower bulkhead section has 5～30 theoretical stages; 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 5.0～101KPa, and bulkhead rectifying tower cat head reflux ratio by weight is 7～20; Preferred version is that the working pressure of bulkhead rectifying tower is 25～70KPa, and bulkhead rectifying tower cat head reflux ratio by weight is 7～13.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; Styrene product is extracted a mouthful preferred version out and is positioned at several the 5th～20 theoretical stages that make progress from bulkhead section 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 energy-conservation effect.Simultaneously, owing to the bulkhead rectifying tower only adopt a tower shell realize two conventional distillations function, the investment also can significantly reduce.The energy-saving principle that the azeotropic heat recovery technology is used for the vinylbenzene sepn process can be seen the theoretical declaratives of CN86108265.In technology disclosed in this invention, bulkhead distillation technology and azeotropic heat recovery technology are combined, obtained dual energy-conservation effect.
Adopt technology of the present invention, the concentration of styrene in the extraction of bulkhead rectifying tower top is less than 500ppm, and the concentration of styrene about 1% in the cat head extraction logistics even higher when adopting common rectification under vacuum; The vinylbenzene concentration expressed in percentage by weight is less than about 5% 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; Adopt bulkhead distillation technology of the present invention, ethylbenzene purity by weight percentage can reach 99% even higher, and the ethylbenzene purity that prior art obtains only is 97%～98%.This shows the loss of adopting the bulkhead distillation technology can significantly reduce the phenyl ethylene rectification process, improve the purity of ethylbenzene.Simultaneously, adopt the bulkhead distillation technology to compare with adopting common rectification under vacuum, the platform number of rectifying tower can reduce to one by three, auxiliary facilitys such as corresponding reboiler and condenser also can be kept to a cover by three covers, saved investment greatly, and compare with the isolating technical scheme of three towers, tower still thermal load and cat head refrigeration duty can reduce more than 15%.Combine by boiling hot recovery technology together, further reduced energy consumption.The purity of styrene product 〉=99.8%.Therefore, adopt technology disclosed by the invention can solve technical problem in the existing phenyl ethylene rectification technology preferably, received 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.
Pump and heat-exchange equipment have been omitted among attached 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 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 2 220 is bulkhead rectifying tower, and 221 is ethylbenzene tower, and 222 is overhead condensers of 220, and 223 is 220 cat head secondary coolers, and 224 is return tanks of 220, the 225th, and mixing tank.Logistics 201 is chargings of bulkhead rectifying tower, form with Fig. 1 in 101 identical, 202 is cat head vapour phase dischargings of 220, its form with accompanying drawing 1 in 102 identical, 203 is saturated liquid phases of 202 condensations, 204 is supercooled liquids of 203,215 is trim the top of column of 220, and 205 is cat head dischargings of 220, the 206th, and styrene product, 207 is tower still dischargings of 220, and composition is heavy components such as styrene oligomer, the diethylbenzene that reacts by-product, tar, stopper.209 is cat head dischargings of 221, and 210 is tower still dischargings of 221, for circulation ethylbenzene is stream I I, the 211st, fresh ethylbenzene is stream I II, the 212nd, and water is stream I V, 213 is 210,211 and 212 ethylbenzene-water azeotropic mixtures of forming, 214 is vaporization saturation steams of 213.
Below in conjunction with accompanying drawing the present invention is elaborated.
In accompanying drawing 1, contain cinnamic stock liquid 101 and enter tower 1 middle part.Tower 1 is a rectifying tower of operating under negative pressure, 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 enters 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 intermediate membrane one side that the stock liquid 201 identical with logistics 101 in the accompanying drawing 1 enters bulkhead rectifying tower 220, 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 5～101KPa, and preferred working pressure is 25～70KPa.The reflux ratio of bulkhead rectifying tower is 5～20, and preferred reflux ratio scope is 6.0～13.Containing ethylbenzene, toluene, benzene and the light component logistics 202 lower than ethylbenzene boiling point by the cat head extraction of bulkhead rectifying tower carries out heat exchange with the mixture of forming from the azeotropic that consists of ethylbenzene-water of mixing tank 225 213 and is condensed in interchanger 222, the latent heat of emitting is with 213 logistics heating and be vaporizated into 214,214 chargings that can be used as reactor behind further heat temperature raising; As 220 trim the top of column 215, a part is as 220 cat head extraction 205 and send into tower 221 and further isolate light component 209 and ethylbenzene 210 more than the toluene by the some of interchanger 223 further cooled logistics 204 for 202 saturated liquid 203.Differ from the middle part or the middle and lower part extraction styrene product 206 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 207 that stopper geometric ratio vinylbenzene boiling point is high.
The invention will be further elaborated below by embodiment.Raw material used in comparative example and embodiment is formed as shown in table 1.
Table 1 contains the weight of ethylbenzene, styrene stream and forms
Embodiment
[comparative example]
Adopting the flow process shown in the accompanying drawing 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.
Table 2150Kt/a styrene device rectifying part separating resulting
More than three towers to separate the total energy consumption cat head be-18243.61 kilowatts, wherein negative sign is represented condensing heat-exchange, three Tata still total energy consumptions are 19230.78 kilowatts.
[embodiment 1]
Adopting the flow process shown in the accompanying drawing 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 30KPa, and the trim the top of column ratio is 10.Separating resulting is listed in the table 3.Because the separation requirement and the segregational load of ethylbenzene tower (221 among 2 among Fig. 1 and Fig. 2) are all constant, so its cooling and heating load is all constant, can compare the total energy consumption of bulkhead rectifying tower and crude styrene tower and refining benzene ethylene column by the data in table 2 and the table 3, i.e. the energy consumption of divided wall column among 1 among Fig. 1 and 2 energy consumption summation and Fig. 2.
Table 3 adopts the vinylbenzene separating resulting of bulkhead distillation technology
Adopt technology of the present invention, the bulkhead distillation technology is combined with heat recovery technology, the total heat exchange load of separate part cat head is single still thermal load of tower 2, promptly-663.95 kilowatt, energy-conservation about 96%, reclaimed the heat of vaporization material ethylbenzene simultaneously, tower still part energy consumption is suitable with former technology, has only increased by 9.6%.
Claims (9)
1. power-economizing method that is used for phenyl ethylene rectification may further comprise the steps:
A) with contain ethylbenzene, cinnamic mixture is a raw material, raw material at first enters bulkhead section one side of bulkhead rectifying tower, gets vinylbenzene through being separated in bulkhead section opposite side, must contain the heavy component of tar in the following segregation section of bulkhead rectifying tower bulkhead section bottom; The vapor phase stream I that must contain ethylbenzene at the above segregation section of bulkhead rectifying tower bulkhead section top;
B) stream I elder generation and the mixture heat exchange of forming by stream I I, stream I II and stream I V, part is circulated to the top of the above segregation section of bulkhead rectifying tower bulkhead section then, another part enters the middle part of ethylbenzene recovery tower, through separating, get toluene and the boiling point light component lower at the top of ethylbenzene recovery tower, at the bottom of the ethylbenzene recovery tower, get logistics H than toluene;
Wherein stream I I is a liquid phase circulation ethylbenzene, and stream I II is fresh ethylbenzene, and stream I V is a water.
2. the power-economizing method that is used for phenyl ethylene rectification according to claim 1, it is characterized in that containing in the stock liquid ethylbenzene weight percentage is 5～60%, cinnamic weight percentage is 20～93%, also contain in the raw material than low-boiling light component of vinylbenzene and the heavy component higher than vinylbenzene boiling point, wherein 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 that is used for phenyl ethylene rectification according to claim 2, it is characterized in that containing in the stock liquid ethylbenzene weight percentage is 20～50%, and cinnamic weight percentage is 40～70%, and the weight percentage of heavy component is 1～10%.
4. the power-economizing method that is used for 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 that is used for 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 that is used for phenyl ethylene rectification according to claim 1, the working pressure that it is characterized in that the bulkhead rectifying tower is 5.0～101KPa, bulkhead rectifying tower cat head reflux ratio by weight is 7～20.
7. the power-economizing method that is used for phenyl ethylene rectification according to claim 6, the working pressure that it is characterized in that the bulkhead rectifying tower is 25～70KPa, bulkhead rectifying tower cat head reflux ratio by weight is 7～13.
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 bulkhead section bottom.
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