CN1006786B - Process for distillation of styrenes - Google Patents
Process for distillation of styrenesInfo
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- CN1006786B CN1006786B CN 85102732 CN85102732A CN1006786B CN 1006786 B CN1006786 B CN 1006786B CN 85102732 CN85102732 CN 85102732 CN 85102732 A CN85102732 A CN 85102732A CN 1006786 B CN1006786 B CN 1006786B
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Abstract
The present invention provides that part of or the whole of low boiling point component vapour which is extracted from the top of a tower is introduced into a compressor, and the vapour is taken as a heating source of a reboiler for use. Because a low boiling point component which is condensed by the reboiler and part of vapour which is not condensed are again returned to circulating lines of the distillation tower, the effect of saving energy is obtained, and a styrene distillation method which is stably operated is obtained.
Description
The present invention is the relevant method that adopts heat pump distillation styrenic.
In distillation, the heat that liquid is evaporated is necessary with making vaporized steam be able to condensing cooling.Common this evaporation and condensing calorific value are roughly the same basically, and particularly aspect the efficient that improves distillation procedure, it is very important reducing the required heat of evaporation.
In order to reduce the heat that is used for distillation tower, carrying out the distillatory method by heat pump is well-known (United States Patent (USP) the 4th, 056, No. 44 specification sheetss, open but unexamined Japanese patent application the 111st, No. 466/77, the open Japanese patent application of also having examined the 39th, No. 236/79 and the 39th, No. 375/79).This distillating method comprises that by compressor the steam of the low boiling component of discharging from the cat head of distillation tower being carried out adiabatic compression allows it heat up, and is used the latent heat of this steam as thermal source or heat reservoir.In this method, just can do the heat supply source to the overhead vapours utilization by supply with a spot of energy from the outside.Therefore, compare with common Distallation systm, to be said to be more useful distillating method to this distillating method from the viewpoint of thermo-economics.
The styrenic of vinylbenzene, Vinyl toluene class, alpha-methyl styrene etc. is by carrying out dehydrogenation manufacturing with ethylbenzene classes such as corresponding ethylbenzene, ethyltoluene class, isopropyl benzenes, this dehydrogenated oil (rough styrenic) mainly is by the styrenic and the unreacted ethylbenzene class that generate, and to contain that reorganization that the polymerization of the light constituent of a spot of benzene, toluene etc. and styrenic part obtains grades be that the mixture of so-called multicomponent type is formed.Thereby, when making styrenic, must from above-mentioned dehydrogenated oil, separate above-mentioned light constituent and heavy constituent and remove.Method like this is promptly used a plurality of distillation towers to distill with isolating method and is used.
But, their boiling point is very close for styrenic and ethylbenzene class, and for example under atmospheric pressure, cinnamic boiling point is 145.2 ℃, the boiling point of ethylbenzene class is 136.2 ℃, only 9.0 ℃ of the boiling-point differences between them.Thereby, when coming separating phenylethylene class and ethylbenzene class, just higher distillation efficiency must be arranged with distillation.Also just be necessary to enlarge the number of plies and the reflux ratio of distillation tower, so, be used to distill the distillation tower of styrenic, if this tower is the words of plate column, general all is tower tray about being equipped with from 60 layers to 100 layers, and the reflux ratio of this tower generally also will be set up the big ratio about 10, pressure difference between like this at the bottom of cat head one tower also becomes greatly, is 90～250mmHg.Thereby, in such distillation tower, just produced problem with the increase of the energy of thermal source form supply.
As this cinnamic distillating method, though require to adopt the distillating method of above-mentioned heat pump,, when the tower top temperature of distillation tower and the temperature head between the column bottom temperature become big, be necessary to increase the compression ratio of low boiling point component steam.Therefore aspect containing close boiling point composition and having the cinnamic distillation of polymerizability, it is generally acknowledged the distillating method that just can not adopt this heat pump.
The purpose of this invention is to provide the cinnamic method of a kind of distillation, this method is a kind ofly heat can be carried out the distillatory method by heat pump and be applied to many compositions type mixture one styrene mixture that obtains in the cinnamic process in preparation and can make the stable distillating method of operation process.
Distillating method that another object of the present invention provides a kind of using heat pump system has improved responsiveness that distillation tower changes for the composition of the liquid of sending into and for because system condition changes the responsiveness that makes the thermal equilibrium change in this system, so this distillation tower can fully adapt to the change that the one-tenth of sending into liquid is grouped into, and can be applied to the distillation of styrenic.
Another purpose of the present invention provides a kind of distillating method of eliminating when adopting the distillating method of this heat pump incident variety of problems when beginning to distill through being everlasting, these problems for example make problem that Distallation systm becomes to be needed before stable for a long time, during this period, problem by the purity decline of distilling the component that obtains, the problem of faults such as dirty dirty and obstruction, problem that the compressor of compressor breaks down or the like take place in machine.
That is to say the cinnamic a kind of method of distillation that the object of the present invention is to provide, this method comprises the distillation ethylbenzene dehydrogenation styrenic mixture of gained afterwards, and the separation styrenic next by ethylbenzene, the middle portion that this process is included in the distillation tower of the fill system of running under the depressurized system imports above-mentioned styrene mixture, in the low boiling point component steam of extracting out from the cat head of above-mentioned distillation tower based on the ethylbenzene class, extract high boiling point component liquids at the bottom of the tower out based on styrenic, part or all importing compressor of above-mentioned low boiling point component steam, allow after it heats up by carrying out adiabatic compression, again steam is imported in the reboiler of above-mentioned distillation tower, allow its part or all condensing, with heating source as above-mentioned reboiler, low boiling component after condensing or its mixture and the not condensing steam of a part are returned in the circulating line of above-mentioned distillation tower, and remaining just discharges from Distallation systm.
The styrenic mixture that the inventive method was suitable for is the mixture that the ethylbenzene class is obtained after dehydrogenation, and mainly form by the styrenic and the unreacted ethylbenzene class that generate, wherein can contain or not contain light constituent such as a spot of benzene, toluene and styrenic partially polymerized afterwards heavy constituent and the stopper that adds in order to prevent the polymerization in the fractionation by distillation process also have moisture, air, nitrogen etc.This styrenic mixture not only comprises the common dehydrogenated oil with steam dehydrogenation gained, also comprises the material by gas phase or liquid-phase oxidation dehydrogenation gained.Thereby above-mentioned styrenic typically refers to vinylbenzene, Vinyl toluene class, alpha-methyl styrene etc.And the ethylbenzene class is meant ethylbenzene, ethyltoluene class, isopropyl benzene etc.
As the constituted mode of distillation tower of the above-mentioned styrenic mixture of distillation, be for example in the 1st tower, to separate than the low-boiling light constituent of ethylbenzene class, next separate ethylbenzene class and styrenic and be higher than the heavy constituent of its boiling point, further styrenic and heavy constituent carried out isolating mode then at the 3rd tower at the 2nd tower; Also there is employing to extract the ethylbenzene class out and than its lower boiling light constituent from cat head at the 1st tower, at the bottom of tower, extract styrenic and the heavy constituent higher respectively out than its boiling point, next distillate at the bottom of overhead distillate and the tower is respectively charged in the 2nd tower, light constituent wherein is by separating in the ethylbenzene class that is related to above-mentioned cat head distillate, about distillate at the bottom of the tower then is from heavy component styrenic to be separated, or the like mode.The present invention goes for above-mentioned any mode.It is desirable to the applied distillation tower as the present invention, is the 2nd tower under the situation of preceding a kind of mode, is the 1st tower under the situation of a kind of mode in back.Therefore, as the applied styrenic mixture of the present invention, can be the mixture after the firm dehydrogenation of ethylbenzene class, also can be to derive to separate in advance and remove mixture than light constituents such as the low-boiling benzene of ethylbenzene class, toluene.
The applied distillation tower of the present invention is the distillation tower of the packed tower pattern that turns round under depressurized system.As the weighting material that is packed into this distillation tower, it would be desirable the weighting material of standard, the differential pressure of particularly calculating every number of plies theoretically will be below 1.5mm Hg, and optimal then is below 0.8mm Hg.Adopt such distillation tower that best distillation efficiency is not only arranged, but also can dwindle reflux ratio.Thereby the differential pressure of distillation tower can be decreased to below the 100mm Hg, it would be desirable to be reduced to below the 70mm Hg, so just can reduce column bottom temperature, the temperature head between also just can dwindling at the bottom of cat head and the tower.
In above-mentioned distillation tower, when extracting steam based on the low boiling point component of ethylbenzene class out, extract high boiling point component liquids at the bottom of its tower out based on styrenic from its cat head.And in part or all importing compressor of the above-mentioned low boiling point component steam of extracting out from the cat head of distillation tower, make its intensification by carrying out adiabatic compression with this compressor, again the steam through the low boiling point component after this intensification is imported in the reboiler of distillation tower, in this reboiler the not condensing steam of left part or all, major part makes it condensing, thus, this steam promptly is used as the heating source of reboiler.
Here be the performance of the composition of the composition according to the styrenic mixture of the distillation tower of packing into, the low boiling point component steam extracted out from the cat head of distillation tower and amount thereof, compressor about the ratio that imports the low boiling point component steam in the above-mentioned compressor and the condensing ratio of reboiler and consider to determine with required heat of the reboiler of the required energy of this compressor, use distillation tower or the like.About from cat head distilled low boiling point component steam, it would be desirable the pipeline that direct importing condensed device is set, at least a portion steam is directly imported in the condenser and is not imported in the compressor therein, so that keep thermal equilibrium to make Distallation systm stable.In addition, in reboiler, can allow whole steams condensing under the situation that does not contain light constituents such as low-boiling benzene than ethylbenzene class, toluene, to leave not condensing steam then better but be left in the situation that contains light constituent.Condensing ratio is to decide by the pressure of control reboiler, and the words of pressurize also just can make the steam of more ratios obtain condensing.But, will cause the excessive raising of pressure the increase of compressor load.In addition, the low boiling point component after this reboiler is condensing and not the part of condensing steam return the distillation tower circulating line, remainingly just discharge from distillation tower.And because this low boiling point component after condensing is still keeping high temperature, be favourable so the low boiling point component of condensation is used for the low boiling point component steam that preheating imports in the compressor.
Adopt method of the present invention preferably when beginning to carry out distillatory, will add distillating material or low boiling point component toward distillation tower in advance, use the auxiliary reboiler of external heat source that it is heated, state with total reflux begins to distill, as thermal source the cat head distilled low boiling point component steam from distillation tower is carried out preheating with liquid at the bottom of the tower, be used for making low boiling point component steam round-robin circulating line as the reboiler thermal source, preheater, compressor and solution-air separator tank must carry out preheating, then the temperature and pressure of each one is adjusted to after the state of the steady running condition that approaches distillation tower, the styrenic mixture of packing into, thereby emit from cat head distilled low boiling point component steam and just make it to change over to normal running.
In the time of the beginning distillatory, the material of the tower bottom of the distillation tower of packing in advance can be to carry out distillatory styrenic mixture, and but, best is to contain the low boiling point component liquid that its boiling point is similar to the boiling point that is contained in those low boiling components wherein.Under the situation that adds low boiling point component liquid in advance, be that the liquid with this low composition that boils of the material of not polymerizability of different boiling can be the mixture that one-tenth single component or two or more are grouped into regard to them.As this low boiling point component liquid, best being to use is included in the styrenic mixture and the low boiling point component of extracting out from the cat head of distillation tower when distillation, this low boiling point component in the styrenic mixture is the composition based on the ethylbenzene class, and optimal then is that the content of styrene monomer accounts for 5%(weight) below.
Adopt method of the present invention in the control distillation tower, need analyze continuously the composition of the styrenic mixture of supplying with distillation tower, carrying out the feed forward control calculation, regulate setting pressure in the solution-air separator tank that is arranged on the reboiler exit automatically as the key of running, also just can control the condensing pressure of reboiler by its output signal to the analytical results of this composition with the internal temperature of distillation tower.
The set-point of the thermometer that is provided with as detecting the temperature in the distillation tower is that basis will be carried out the kind of distillatory styrenic mixture and the characteristic of distillation tower decides.Moreover, to the amount of the low boiling component of prepare extracting out or be delivered to heat in the reboiler, preferably can to the two with above-mentioned distillation tower in temperature carry out cascade and control, like this, just the above-mentioned internal temperature of distillation tower can be controlled at the temperature of setting.In order to control the heat of biography to reboiler, this control can and be arranged on the combination of control valve of extracting the extraction pipeline of steam out from this solution-air separator tank by the tensimeter that is used to detect the pressure in the solution-air separator tank that is arranged on the reboiler exit and carry out.
Brief description of drawings:
Fig. 1 is a schema of representing to distill by heat pump according to one embodiment of present invention the method for styrenic.
The explanation of most preferred embodiment:
Under the situation that applies the present invention to styrene mixture (crude styrene class), quote in the accompanying drawings schema as embodiment, it is as follows that the present invention is described in detail in detail:
Fig. 1 packs the styrenic mixture with the stage casing of the distillation tower (2) of the packed tower system of depressurized system running into from charging hole (1).When extracting low boiling point component steam based on the ethylbenzene class out from the cat head pipeline (3) of distillation tower (2), the high boiling point that the pipeline (4) at the bottom of this tower is extracted out based on styrenic becomes separatory.
The low boiling point component steam of extracting out from above-mentioned pipeline (3) is distributed to condenser (5) distillation tower circulating line (6) and compressor (7) pipeline (8) on one side on one side, being assigned to above-mentioned pipeline (6) low boiling component steam on one side is with above-mentioned condenser (5) refrigerative, afterwards with regard in the reflux drum (9) of once all packing into, when a part was back to above-mentioned distillation tower (2) top from distillation tower circulating line (10), rest parts just was drawn out of the outside of total system.Be distributed to above-mentioned pipeline (8) other low boiling point component steams on one side by adiabatic compression being warmed up to more than the base product temperature, and then send into reboiler (13) from pipeline (12), at these these steams as just usefulness of thermal source.
It mainly is that the vapor volume of the low boiling component steam of importing compressor (7) is controlled at a set(ting)value that the steam of above-mentioned low boiling component is assigned to condenser (5) pipeline (6) and compressor (7) pipeline (8) on one side on one side, and prevent to supply with the too much heat of Distallation systm, the operating condition of Distallation systm and the change of raw material composition etc. are depended in the variation of heat, but be added to heat in the reboiler is not that superfluous amount just can be enough, generally be more than 0.5% to below 25%.As for adoptable control method, for example a kind of control method of the condensed liquid that comprises the low boiling point component steam that accumulates in condenser (5) the inside and utilize the method for controlling the fluid level of condensed liquid at the control valve and the fluid level meter in condensed liquid exit, thus increase or reduce the heat transfer area of condenser; Also can adopt at condenser (5) inlet side of pipeline (6) and establish the next directly actuated method of a control valve, and in this schema, then be at pipeline (6) valve that a control valve (14) is associated with the flow regulator (15) of the exit pipeline (12) that is located at compressor (7) by it to be set to open and close a vapor volume of the low boiling component steam of importing compressor (7) and maintain a definite value.
Also have, when the low boiling component steam that imports compressor (7) if during saturated vapo(u)r, steam can be condensing in compressor or condensing outlet conduit place with the compressor adiabatic compression time, drop can cause the polymerization of the fault of compressor or styrene monomer and usually bring very big damage in compressor, so it would be desirable that establishing one at above-mentioned pipeline (8) gives hot device (16), heat importing low boiling point component steam in the compressor in advance, to improve its temperature in advance.
Importing compressor (7) is used as heating source by pack into the low boiling component steam of reboiler (13) of pipeline (12) after heating up by adiabatic compression.In reboiler (13) lining, part or all lower boiling component is by condensing, and will mainly result from the latent heat utilization in this stage and make heating source.With the condensed liquid of the low boiling component of reboiler (13) heat supply or condensed liquid and steam is from pipeline (17) the solution-air separator tank (18) of packing into, and the low boiling component after condensing is separated with not condensing low boiling component steam.In this case, in order to reduce the pressure-losses at reboiler (13) inner heating surface, heat transfer efficiency is improved, and better is that the pipeline that leads to solution-air separator tank (18) from reboiler (13) is divided into the pipeline that makes condensed liquid flow into the pipeline of solution-air separator tank (18) and make not condensing low boiling point component steam inflow solution-air separator tank (18).In the condensing component of this reboiler (13) is to have high boiling relatively component in the low boiling component steam, and be component, be to have lower boiling relatively component in the low boiling component steam with the not condensing component of not condensing state by reboiler (13) in addition and be component based on benzene and toluene and moisture, air, nitrogen etc. based on the ethylbenzene class.
In this schema, from the bottom of above-mentioned gas-liquid separation groove (18) extract out condensing after low boiling component be when this component is controlled by liquidometer (19) and the control valve (21) that is arranged on pipeline (20), to be imported into preheater (16).After this component and the low boiling component steam that imports above-mentioned compressor (7) with preheater (16) carry out heat exchange, collaborate above-mentioned pipeline (6) by pipeline (22).Because this condensed liquid also keeping high temperature, thus preferably with condensed liquid by pipeline (32) delivery heat exchanger (33) and the phegma that is used for going back to distillation tower (2) maintain a constant temp.In addition, the low boiling component steam of extracting out from the top of above-mentioned solution-air separator tank (18) is to be extracted out while controlling by tensimeter that is arranged on above-mentioned solution-air separator tank (23) and the pressure controlled valve (25) that is arranged on pipeline (24), collaborate pipeline (6) by this pipeline (24), it can condensing fully by this way, just can not allowed in the low boiling point component steam, have high boiling relatively composition by being controlled at low boiling component steam in the reboiler (13), and improve the condensing temperature in reboiler (13) selectively by condensing.And can increase the heat transfer capacity of the condensing amount of per unit, moreover also can compresses machine (7) thus compression ratio and can reduce running expense and reduce cost of equipment.And the temperature that helps making low boiling component condensing in this reboiler (13) remains on and must and be enough to the temperature that in preheater (16) the low boiling component steam heated.The control of the condensing amount of the low boiling component steam in reboiler can by control reboiler pressure just the pressure of solution-air separator tank carry out.For example, there is pressure a large amount of steams also just to be increased once improving, when pressure one reduction, just heat transfer capacity can be reduced on the other hand, perhaps compression pressure can be reduced by condensing, heat transfer capacity.
The change that imports the low boiling point component steam of compressor (7) is that the change with the low boiling point component steam that imports reboiler (13) has direct contact, so in order to make this Distallation systm can stably carry out operation, at the pipeline that unrolls (26) that leads to condenser (5) from compressor (7) an accurate control valve (figure expression) is set, thereby can absorb can not be by the thermal capacity of the small variations of compressor (7) control.
For drive compression machine (7), available several different methods for example only with motor drive, with motor and gas-turbine combination or only with the gas-turbine driving etc.But in order to make Distallation systm reach stabilization, be preferably in the revolution control machinery that a precision is set in the driving machine of compressor (7).Can adopt VVVF machinery and VV machinery etc. as the machinery that is used to control revolution.Because power source voltage and the change of frequency or the change of vapor pressure can add feedback machinery with the i.e. control capacity change of control revolution.
In order to make this Distallation systm stably carry out operation, also further done following control in this embodiment.
Just locate to be provided with one and continuously styrenic the ingredients of a mixture of the distillation tower of packing into (2) is formed the successive analysis gc analysis device of analyzing (27) at above-mentioned charging line (1), the thermometer (28) that temperature is used in the mid-way of above-mentioned distillation tower (2) is provided with the detection tower is provided with one at the extraction pipeline (11) from above-mentioned reflux drum (9) and detects the under meter (29) of the flow of extracting low boiling component out and the control valve (30) of this flow of control.
And temperature and the extraction amount that detects with under meter (29) and detect the interior vapor pressure of solution-air separator tank (18) with pressure warning unit (23) and all carry out cascade respectively and control in the tower that detects with above-mentioned thermometer (28), simultaneously, the interior temperature of result who analyzes with above-mentioned gc analysis device (27) and the distillation tower (2) that detects with above-mentioned thermometer (28) is carried out the feed forward control calculation, is controlled the setting pressure of the low boiling component steam of solution-air separator tank (18) the inside by its output signal.The calculation formula of above-mentioned feedforward running is suitably to determine according to kind and the dynamic (dynamical) characteristic of distillation tower of sending into the styrenic mixture in the distillation tower (2) by pipeline (1).
In this embodiment, under the situation of forming change of the styrenic mixture of being sent into by charging line (1), the feedforward calculation process is so that the interior temperature of control distillation tower depends on the measurement result of temperature in analytical results and the distillation tower to this value of fixed value; By the output signal of computing, control valve is controlled, so that increase the amount of the low boiling component of extracting out.Simultaneously, control valve (25) is to be used for controlling the pressure that makes in the reboiler (13) to raise so that the condensing temperature of the low boiling point component steam in the reboiler (13) is improved and the heat transfer capacity increase.When low boiling point component reduces, just can adopt the antipodal control method of situation that increases with above-mentioned low boiling component conversely.
Moreover, only use above-mentioned reboiler (13) to supply with and under the insufficient situation or in order to supply with necessary heat of when starting, just require the auxiliary reboiler (31) that imports external heat sources such as steam to be set at the heating source of distillation tower (2) at distillation tower (2).In the time of the beginning distillatory, in distillation tower (2), add distillating material or low boiling component in advance, with above-mentioned auxiliary reboiler (31) it is heated with the total reflux state and begin distillation; And liquid is sent into preheater (16) so that cat head distilled low boiling point component steam is carried out preheating by pipeline (2) at the bottom of the tower, with the low boiling point component steam of this preheating to circulating line (3) (6) (8) (10) (12) (17) (20) (22) and (24), preheater (16), compressor (7), reboiler (13) and solution-air separator tank (18) carry out preheating, next the temperature and pressure of each one is adjusted to state near the steady running condition of distillation tower (2), charging feedstock then, Zhi Hou low boiling component steam flows to reboiler (13) and changes normal running over to by compression.
In addition, in this embodiment, when the Distallation systm entry into service or under the few situation of the low boiling component steam in solution-air separator tank (18), importing solution-air separator tanks (18) such as rare gas element such as nitrogen can be used for successfully controlling compression pressure.
Embodiment 1
Distallation systm according to embodiment shown in Figure 1, the dehydrogenated oil with the composition shown in the table 1 that obtains by ethylbenzene dehydrogenation is distilled, and the differential pressure between at the bottom of using the distillation tower filled standard weighting material (SULZER BROTHERS LTD produces, commodity MELLAPAK by name) and control cat head-Ta in this distillation is below 70mm Hg.In the running of this distillation tower, stably supply with dehydrogenated oil, extract 40 parts of lower boiling component liquid out and extract 60 parts of high boiling component liquid out from pipeline (4) from pipeline (11).Flow, the temperature and pressure of each measuring point A, B, C, D and E that the foregoing description is represented all are controlled to be the represented value of table 2.The composition of Extract is as shown in table 1 at the bottom of the low boiling component of distillation tower (2) and this tower.
Clearly illustrated that in this embodiment cinnamic distillation can carry out on quite stable ground, only use the situation of steam to compare, the energy decreased average that compressor (7) consumes about 30%, its result shows the consumption of having saved energy significantly.
Table 1
Extract at the bottom of the composition dehydrogenated oil overhead product tower
(weight %) (weight %) (weight %)
Benzene 0.67 1.67-
Toluene 2.25 5.61-
Non-aromatic hydrocarbon 0.16 0.34-
Ethylbenzene 34.45 90.50 0.04
Vinylbenzene 61.88 1.86 0.04
Heavy constituent 0.48-97.61
Water 0.11-2.31
Table 2
The flow temperature, pressure
Measuring point (A=100) (℃) (mm Hg)
A 100 73 105
B 95 83 90
C 95 124～126 425
D 90 120 -
E 5 120 110
Embodiment 2
Present embodiment uses the dehydrogenated oil as dehydrogenated oil replacement the foregoing description 1 of the represented composition of table 3 to distill.The composition of the low boiling point component of distillation tower (2) and the liquid extracted out at the bottom of this tower is as shown in table 3, flow, the temperature and pressure of each measuring point A, B, C, D and E all are controlled at the value shown in the table 4, in this embodiment 2 also equally quite stable ground carry out cinnamic distillation.
Table 3
Extract at the bottom of the component dehydrogenated oil overhead product tower
(weight %) (weight %) (weight %)
Benzene 0.10 0.21-
Toluene 0.16 0.42-
Non-aromatic hydrocarbon 0.10 0.22 0.40
Ethylbenzene 37.59 97.20 0.40
Vinylbenzene 61.50 2.31 97.63
Heavy constituent 0.45-2.30
Water 0.10--
Table 4
Measuring point flow temperature, pressure
（A＝100） （℃） （mm Hg）
A 100 75 105
B 88 83 90
C 88 125 425
D 86 120 -
E 2 120 110
Embodiment 3
In this embodiment except from pipeline (1) with 100 parts/hour speed pack into dehydrogenated oil, extract low boiling component liquid from pipeline (11) out with 36 parts/hour speed, extract out outside the high boiling component liquid from pipeline (4) with 64 parts/hour speed simultaneously, distill with the method identical with embodiment 1, the flow of measuring point A is 270 parts/hour.Flow, the temperature and pressure of each measuring point A, B, C, D and E all are controlled at the value shown in the table 5.Cinnamic distillation also can similarly be carried out highly stablely in embodiment 3.
Table 5
Measuring point flow temperature, pressure
（A＝100） （℃） （mm Hg）
A 100 70.2 95
B 99.1 75.8 319
C 97.3 121.3 392
D 93.7 91.9 -
E 3.7 91.9 385
Claims (4)
1, a kind of method of distilling styrenic, in the distillating method of this styrenic of separating phenylethylene class and ethylbenzene class, it is styrene mixture with ethylbenzene class gained after dehydrogenation, importing is with the stage casing of the packed tower of depressurized system running, distillate the lower boiling steam that ethylbenzene is main body from this distillation tower cat head, extract high boiling point liquid simultaneously at the bottom of the tower out based on vinylbenzene, the compressed machine of above-mentioned lower boiling steam carries out adiabatic compression, make it to heat up, the latent heat of this steam can utilize the thermal source as the distillation tower reboiler, to make the isolating distillation of vinylbenzene and ethylbenzene, the styrenic distillation method is characterised in that, make above-mentioned by a part of vapour condensation in the distillation tower cat head distilled lower boiling steam, and the circulation line of importing distillation tower, meanwhile, the steam of remainder is imported compressor, make it to heat up by adiabatic compression, send into then in the reboiler of distillation tower, make it part or all of condensation, can be utilized as the heating source of above-mentioned reboiler by this, then, in the gas-liquid separation groove, be separated into the low boilers and the uncooled lower boiling steam of condensation, with the low boilers of condensation, or the uncooled steam of it and a part sends back in the distillation tower circulation line, and resistates is then discharged from distillation column system.
2, according to the distillating method of the styrenic of claim 1, wherein the low boiling point component after reboiler is condensing is to go into the thermal source that gives hot device of the low boiling point component steam of compressor and use as giving thermal conductance.
3, according to the distillating method of the styrenic of claim 1, wherein make the interior temperature of distillation tower of operation point position reach design temperature, to the extraction amount of low boiling point component and/or when the heat transfer capacity of reboiler carries out cascade control, continuously to the composition of the styrenic mixture of supplying with above-mentioned distillation tower, analyze, again the temperature in the analytical results of this composition and the distillation tower is carried out the feed forward control calculation, the pressure in the reboiler is regulated automatically by its output signal.
4, according to the distillating method of the styrenic of claim 1, wherein at the auxiliary reboiler of distillation tower setting in order to the importing external heat source, give earlier and in distillation tower, add distillating material and low boiling point component, heating with above-mentioned auxiliary reboiler makes it begin to distill when the state of total reflux again, waste liquid is as the thermal source of preheater at the bottom of distillation proceeds to the distillation Tata that will heat in the stable process, and this preheater is to use do preheating for the steam of the low boiling point component that imports compressor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 85102732 CN1006786B (en) | 1984-04-26 | 1985-04-15 | Process for distillation of styrenes |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59082863A JPS60226836A (en) | 1984-04-26 | 1984-04-26 | Method for distilling styrene |
| CN 85102732 CN1006786B (en) | 1984-04-26 | 1985-04-15 | Process for distillation of styrenes |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN85102732A CN85102732A (en) | 1986-10-15 |
| CN1006786B true CN1006786B (en) | 1990-02-14 |
Family
ID=25741563
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 85102732 Expired CN1006786B (en) | 1984-04-26 | 1985-04-15 | Process for distillation of styrenes |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1006786B (en) |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100393831C (en) * | 2006-09-30 | 2008-06-11 | 陆让先 | Distillation process for energy-saving gum rosin |
| CN101429088B (en) * | 2007-11-07 | 2012-01-25 | 中国石油化工股份有限公司 | Distillation method for separating ethylbenzene and vinyl benzene-containing flow |
| CN101633597B (en) * | 2008-07-26 | 2012-10-10 | 中国石油化工股份有限公司 | Method for saving energy in rectification of styrene |
| US20100101273A1 (en) * | 2008-10-27 | 2010-04-29 | Sechrist Paul A | Heat Pump for High Purity Bottom Product |
| US9045697B2 (en) * | 2012-03-05 | 2015-06-02 | Uop Llc | Distillation column heat pump with compressor inlet superheater |
| JP5793157B2 (en) * | 2013-03-04 | 2015-10-14 | 日本リファイン株式会社 | Solution processing equipment |
| CN103495288A (en) * | 2013-10-17 | 2014-01-08 | 河南莱帕克化工设备制造有限公司 | Novel reflux ratio regulating device |
| CN105669353B (en) * | 2014-11-20 | 2018-04-06 | 中国石油化工股份有限公司 | Ethylbenzene styrene separation process |
| CN105669354B (en) * | 2014-11-20 | 2018-04-06 | 中国石油化工股份有限公司 | ethylbenzene dehydrogenation reaction product separation method |
| JP6566876B2 (en) * | 2016-01-26 | 2019-08-28 | 東洋エンジニアリング株式会社 | Heat exchange amount adjustment method for internal heat exchange distillation column |
| CN105588472B (en) * | 2016-03-08 | 2018-01-12 | 北京国电龙源环保工程有限公司 | The distribution method of the Load Distribution device of steam Direct Contact Heating method piece-rate system |
| CN109675333B (en) * | 2017-10-19 | 2021-09-14 | 中国石化工程建设有限公司 | Benzene tower fractionation device and method driven by heat pump |
| CN109675332B (en) * | 2017-10-19 | 2021-09-14 | 中国石化工程建设有限公司 | Toluene column fractionation device and method driven by heat pump |
-
1985
- 1985-04-15 CN CN 85102732 patent/CN1006786B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| CN85102732A (en) | 1986-10-15 |
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