CN85102732A - The distillating method of styrenic - Google Patents
The distillating method of styrenic Download PDFInfo
- Publication number
- CN85102732A CN85102732A CN85102732.6A CN85102732A CN85102732A CN 85102732 A CN85102732 A CN 85102732A CN 85102732 A CN85102732 A CN 85102732A CN 85102732 A CN85102732 A CN 85102732A
- Authority
- CN
- China
- Prior art keywords
- boiling point
- styrenic
- low boiling
- point component
- distillation tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Part or all importing compressor that is handle from the low boiling point component steam of cat head discharge provided by the present invention, this heating source as reboiler is used, because low boiling point component reboiler is condensing after and and this not the part of condensing steam go back to the distillation tower circulating line again, so just play the effect of the saving energy and can obtain the distillating method of the styrenic of runs steadily.
Description
The present invention is the relevant distillating method that adopts the styrenic of heat pump mode.
In distillation, the heat that liquid is evaporated is necessary with making vaporized steam be able to condensing cooling.Therefore, common this evaporation and condensing required heat are roughly the same basically, and particularly aspect the efficient that improves distillation procedure, it is very important reducing the required heat of evaporation.
Employing is to reduce the method for the heat that uses at these distillation towers, the distillating method that is heat pump mode has been well-known (United States Patent (USP) the 4th, 056, No. 444 specification sheets, spy open clear 52-111, No. 466 communiques, the clear 54-39 of patent gazette, No. 236 communiques and the clear 54-39 of patent gazette, No. 275 communiques).This distillating method is allowing its intensification after the steam adiabatic compression of the low boiling point component of discharging from the cat head of distillation tower by compressor, the latent heat of this steam is used as the thermal source of distillation tower reboiler, adds that supplying with a spot of energy again from the outside just can do the heat supply source to the overhead vapours utilization.Therefore, this distillating method can be described as than common distillation mode at distillating method more useful aspect the heat economy.
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) is based on the styrenic that generates and the material of unreacted ethylbenzene class, contain a spot of benzene, heavy constituent after the light constituent of toluene etc. and styrenic are partially polymerized, promptly so-called multicomponent is a mixture.Thereby, when making styrenic, above-mentioned light constituent and heavy constituent are separated from above-mentioned dehydrogenated oil to get rid of be necessary, as its method, the distillation and separation method that just is to use a plurality of distillation towers that is adopted.
But their boiling point is close concerning styrenic and ethylbenzene class, and for example under atmospheric pressure, cinnamic boiling point is that 145,2 ℃, the boiling point of ethylbenzene class are 136,2, only 90 ℃ and reach 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, it is that the occasion of layer tower generally all is the tower tray about being equipped with from 60 layers to 100 layers, the reflux ratio that also has it, generally also will expand to about 10, the pressure difference between at the bottom of cat head one tower also becomes greatly, is 90～250mmHg.Thereby, in suchlike distillation tower, just produce very big problem as the energy that thermal source is supplied.
As this cinnamic distillating method, though require to adopt the distillating method of above-mentioned heat pump mode, but, the tower top temperature of distillation tower and the temperature head between the column bottom temperature one become big, owing to must enlarge the compression ratio of low boiling point component steam, containing with close boiling point composition and having aspect the cinnamic distillation of polymerizability, it is generally acknowledged the distillating method that just can not adopt this heat pump mode.
The objective of the invention is distillating method with heat pump mode, the multicomponent that is applicable to styrenic manufacturing engineering gained is provided is that mixture is the distillation of styrene mixture and distillating method that can steady running.
Also have, other purpose of the present invention provides improves distillation tower for owing to supply with the change that the one-tenth of liquid is grouped into or measure intrasystem condition and change the responsiveness, the control distillation tower that produce thermally equilibrated change etc. and can fully adapt to the change that the one-tenth of supplying with liquid is grouped into, and can be applicable to the distillating method of the distillatory heat pump mode of styrenic.
In addition, caused variety of problems when another purpose of the present invention provides solution and begins to distill through being everlasting when adopting the distillating method of this heat pump mode, for example distillation is tied to needs the problem of long time, during this period before stable, distillation obtains problem that the purity of composition descends, problem that the compressor of problem, the compressor of faults such as the dirty dirty and obstruction of machine breaks down etc. takes place, and can be applicable to the distillating method of the distillatory heat pump mode of styrenic.
That is to say that the present invention is the styrenic mixture of distillation with gained after the ethylbenzene dehydrogenation, at separating phenylethylene class and ethylbenzene time-like, import above-mentioned styrene mixture at pars intermedia with the distillation tower of the packed tower pattern of depressurized system running, 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 of above-mentioned low boiling point component steam imported compressor by carrying out adiabatic compression, allow it heat up and import the device that to boil of distillation tower afterwards, allow part or all condensing heating source that makes as above-mentioned reboiler, next, low boiling point component after condensing also have with this not the part of condensing steam just go back to the distillation tower circulating line, remaining just from the distillating method of the styrenic of Distallation systm discharge.
The styrenic mixture that the inventive method was suitable for is the material that the ethylbenzene class is obtained after dehydrogenation, styrenic after the generation and unreacted ethylbenzene class are its main component, and difference according to circumstances contains light constituent such as a spot of benzene, toluene and styrenic heavy constituent and the stopper that adds for the polymerization that is controlled in the fractionation by distillation process etc. after partially polymerized and also has moisture, air, nitrogen etc.As this styrenic mixture, be not only dehydrogenated oil by the dehydrogenation gained of general steam, also contain material by the oxydehydrogenation gained of gas phase or liquid phase.Thereby above-mentioned so-called styrenic is exactly vinylbenzene, Vinyl toluene class, alpha-methyl styrene etc.Also have, so-called ethylbenzene class is exactly ethylbenzene, ethyltoluene class, isopropyl benzene etc.
Constituted mode as the distillation tower that distills above-mentioned styrenic mixture, just like separating than the low-boiling light constituent of ethylbenzene class at the 1st tower, next the heavy constituent that separate ethylbenzene class and styrenic and be higher than its boiling point at the 2nd tower, further styrenic and heavy constituent are carried out isolating mode then at the 3rd 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 separating phenylethylene class and the heavy constituent higher out than its boiling point, next distillate at the bottom of overhead distillate and the tower is respectively charged in the 2nd other tower, above-mentioned overhead distillate is carried out separating of light constituent and ethylbenzene class and distillate at the bottom of the above-mentioned tower is carried out isolating mode of styrenic and heavy constituent or the like.The present invention goes for above-mentioned any mode.Optimal is the 2nd tower as distillation tower that the present invention was suitable for, the former occasion, and the latter's occasion is the 1st tower.Therefore, as the styrenic mixture that the present invention was suitable for, can be the firm dehydrogenation of ethylbenzene class material afterwards, also can be to separate the material of removal in addition than light constituents such as the low-boiling benzene of ethylbenzene class, toluene in advance.
Also have, the distillation tower that the present invention was suitable for is the distillation tower with the packed tower pattern of depressurized system running.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 1.5mmHg, optimally then is below 0.8mmHg.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 also will it would be desirable to be reduced to below the 70mmHg below 100mmHg, so just can reduce column bottom temperature, the temperature head between also just can dwindling at the bottom of cat head-Ta.
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, this reboiler the not condensing steam of left part or all, major part allows its condensing employing make 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 low boiling point component steam in the above-mentioned compressor and the condensing ratio of reboiler and wait with the required heat of reboiler of the required energy of this compressor, use distillation tower and to consider to determine.Also have, about from cat head distilled low boiling point component steam, it would be desirable the pipeline that imports direct condensed device is set, like this for make Distallation systm must in steady running at least its a part do not import compressor and import direct condensed device and obtain thermal equilibrium with activation.In addition, in reboiler, can not allow it all condensing though do not contain the occasion of light constituents such as low-boiling benzene than ethylbenzene class, toluene, the occasion of light constituent is left to have not condensing steam then better but contain.Condensing ratio is to decide by the pressure of control reboiler, and it is condensing that the words of pressurize also just can make more ratio obtain.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 go back to distillation tower circulation series, remainingly just discharge from distillation tower.And because this low boiling point component after condensing is still keeping high temperature, be favourable so be used to import the heat of giving of low boiling point component steam 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, cat head distilled low boiling point component steam from distillation tower, liquid gives heat as thermal source at the bottom of the tower, give low boiling point component steam after the heat to the low boiling point component steam institute round-robin circulating line of the heating source that becomes reboiler with this, give hot device, compressor and gas-liquid separation groove give heat, 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 is emitted like this from cat head distilled low boiling point component steam and is just made 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 have to be similar to the wherein low boiling point component liquid of the boiling point of low boiling point component.Add the occasion of low boiling point component liquid, this low boiling point component liquid can be the material of the different not polymerizability of boiling point, also can be the mixture that is grouped into by single component or the one-tenth more than 2 kinds.As this low boiling point component liquid, best being to use is included in the styrenic mixture, the low boiling point component of extracting out from the cat head of distillation tower when distillation.Low boiling point component in this styrenic mixture is the material based on the ethylbenzene class, and optimal then is that styrene monomer content accounts for below 5% of weight.
Adopt method of the present invention in the control distillation tower, composition to the styrenic mixture of supplying with distillation tower is analyzed continuously, the analytical results of this composition with the setting is that temperature is carried out the feed forward control calculation, automatically regulated the setting pressure in the gas-liquid separation groove that is arranged on the reboiler exit by its output signal in the distillation tower, also just can control the condensing pressure of reboiler.
Here the measuring point that is provided with for the set thermometer of the interior temperature of detection distillation tower of indication is that basis will be carried out the kind of distillatory styrenic mixture and the characteristic of distillation tower determines.Also have, as the control that the temperature in the above-mentioned distillation tower is subjected to design temperature, the extraction amount of low boiling point component and to the heat transfer capacity of reboiler, preferably can to the two with above-mentioned distillation tower in temperature carry out cascade and control.And carry out as the combination that control passes the tensimeter of the pressure in the gas-liquid separation groove that means to the heat transfer capacity of reboiler can be arranged on the reboiler exit by detection and is arranged on the control valve in the extraction pipeline of extracting steam from this gas-liquid separation groove out.
Brief description of drawings:
Fig. 1 is the programchart that the relevant one embodiment of the present of invention of expression adopt the styrenic distillating method of heat pump mode.
The explanation of most preferred embodiment:
It below is the detailed description of representing that with reference to the accompanying drawings an example is done the programchart of the suitable embodiments of the invention of the styrenic mixture (crude benzole vinyl) that the dehydrogenation of ethylbenzene class is obtained.
Fig. 1, the styrenic mixture is to pack into the pars intermedia of the distillation tower (2) of the packed tower pattern of depressurized system running, in the low boiling point component steam of extracting out from the cat head pipeline (3) of this distillation tower (2) based on the ethylbenzene class from the pipeline of packing into (1), and 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 assigned 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 point component steam on one side is with the bucket (9) that refluxes of just once packing into after above-mentioned condenser (5) cooling, its part is when being back to above-mentioned distillation tower (2) top from distillation tower circulating line (10), and rest parts just is drawn out of the outside from pipeline (11).Be assigned to above-mentioned pipeline (8) low boiling point component steam on one side in addition and be by with above-mentioned compressor (7) adiabatic compression, more than being warmed up to the base product temperature after, from pipeline (12) reboiler (13) of packing into, the heating source that is used as it uses.
It mainly is that the vapor volume of the low boiling point component steam of importing compressor (7) is controlled in the set(ting)value that above-mentioned low boiling point component steam is assigned to condenser (5) pipeline (6) and compressor (7) pipeline (8) on one side on one side, to prevent to supply with the too much heat of Distallation systm.
So according to the operating condition of Distallation systm, the change that raw material is formed etc. changes, but is added to the heat in the reboiler if the words of not superfluous amount are just enough, generally be more than 0.5% to below 25%.As its control method, for example can adopt with the liquidometer of the liquid level of the condensed liquid that detects the low boiling point component steam that is trapped in condenser (5) the inside and the control valve of condensed liquid outlet and control the method that the heat-transfer surface that makes this condenser can do to increase and decrease control, 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 programchart, then be at pipeline (6) control valve (14) to be set to be associated with the flow regulator (15) of the exit pipeline (12) that is located at compressor (7) by it and to open and close a vapor volume of the low boiling point component steam of importing compressor (7) and maintain in the certain value.
Also have, the low boiling point component steam that imports compressor (7) is if the words of saturated vapo(u)r, since sometimes can be in compressor with after the compressor adiabatic compression time or its outlet conduit condensing, drop can cause the polymerization of the fault of compressor or styrene monomer and bring very big damage in compressor, so it would be desirable at above-mentioned pipeline (8) high and give hot device (16), heat in advance importing low boiling point component steam in the compressor, with its temperature of prior raising for well.
Import compressor (7), used as heating source by pack into the low boiling point component steam of reboiler (13) of pipeline (12) after heating up by adiabatic compression.In reboiler (13) lining, part or all of low boiling point component is condensing, mainly is exactly as heating source with at that time latent heat utilization.Reboiler give with the condensed liquid of the low boiling point component of heat or condensed liquid and steam be from pipeline (17) the gas-liquid separation groove (18) of packing into, the low boiling point component after condensing is separated with not condensing low boiling point component steam.At this moment, preferably for reboiler (13) the internal heating pressure-losses is on one side reduced, heat transfer efficiency is improved, the pipeline that leads to gas-liquid separation groove (18) from reboiler (13) is divided into the pipeline that makes condensed liquid flow into the pipeline of gas-liquid separation groove (18) and make not condensing low boiling point component steam inflow gas-liquid separation groove (18).At the condensing composition of this reboiler (13) is more high boiling composition in the low boiling point component steam, promptly be the material based on the ethylbenzene class, to be more lower boiling composition in the low boiling point component steam promptly be not condensing at reboiler (13) in addition and not condensing composition that in the same old way pass through based on the material of benzene and toluene and little branch, air, nitrogen etc.
In this programchart, from the bottom of above-mentioned gas-liquid separation groove (18) extract out condensing after low boiling point component be by liquidometer that is located at gas-liquid separation groove (18) (19) and the control valve (21) that is arranged on pipeline (20) control import give hot device (16), after this low boiling point component steam that gives hot device (16) and importing above-mentioned compressor (7) carries out heat exchange, collaborate above-mentioned pipeline (6) by pipeline (22).Also have, because this condensed liquid is also keeping high temperature, so preferably be used to keep from pipeline (32) guiding heat exchanger (33), go back to the certain temperature of phegma of distillation tower (2).In addition, the low boiling point component steam of extracting out from the top of above-mentioned gas-liquid separation groove (18) is extracted out while controlling by the tensimeter that is arranged on above-mentioned gas-liquid separation groove (23) and the pressure controlled valve (25) that is arranged on pipeline (24), collaborates pipeline (6) by this pipeline (24).Make the low boiling point component steam can condensing fully, just can not allow the more high boiling composition in the low boiling point component steam carry out condensing selectively by controlling like this at reboiler (13).Raising is in the condensing temperature of reboiler (13).Also have except the condensing amount of per unit also can obtain bigger heat transfer capacity, also can compresses machine (7) thus compression ratio control running expense make installation cost become cheap.And then after this reboiler (16) is condensing low boiling point component temperature with give hot device (16) to the low boiling point component steam heat aspect can keep necessary in addition and the advantage of temperature fully.The control of the condensing amount of the low boiling point component steam of reboiler be can be by the control reboiler pressure just the pressure of gas-liquid separation groove carry out.For example, can carry out condensing, also just increase of heat transfer capacity to pressure in large quantities once improving, and pressure one reduces, heat transfer capacity has just reduced, and just can reduce compression pressure.
The change that imports the low boiling point component steam of compressor 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, establish precision control valve (figure expression) accurately at the pipeline that unrolls (26) that leads to condenser (5) from compressor (7), the small change of the thermal capacity that compressor (7) can not control Wan is absorbed.
As the transmission amount of compressor (7) have motor separately, several different methods such as motor and gas-turbine combination or gas-turbine be independent.But in order to strive for the stabilization of Distallation systm, the drive motor that is preferably in compressor (7) is provided with the revolution controlling organization of a precision.As this revolution controlling organization is to adopt modes such as VVVF mechanism and VV mechanism.Pressure variation for power source voltage and variation of frequency and steam.The assembling feedback mechanism to revolution capacity change just control.
Stably carry out also further having done following control in this embodiment aspect the operation at Distallation systm.
Just be provided with one and continuously styrenic the ingredients of a mixture of the distillation tower of packing into (2) formed the gas chromatograph device that the successive analysis analyzed is used, be provided with in the mid-way of above-mentioned distillation tower (2) and detect temperature is used in the tower thermometer, a control valve (30) that detects the under meter (29) of the flow of extracting low boiling point component out and control this flow be set at extraction pipeline (11) from above-mentioned backflow bucket (9) at the above-mentioned pipeline of packing into (1).
And temperature and the extraction amount that detects with under meter (29) and all carry out cascade respectively with the pressure of pressure warning unit (23) detection gas-liquid separation groove (18) inner vapor and control in the tower that detects with above-mentioned thermometer (28), the analytical results of above-mentioned gas chromatograph device of while (27) and the temperature of heating up in a steamer in (2) with the distillation that above-mentioned thermometer (28) detects are carried out the feed forward control calculation, are controlled the setting pressure of the low boiling point component steam of gas-liquid separation groove (8) the inside by its output signal.In addition, the calculation formula of above-mentioned feed forward control is suitably to determine according to kind and the dynamic (dynamical) characteristic of distillation tower of being supplied with the styrenic mixture in the distillation tower (2) by the pipeline of packing into (1).
In this embodiment, the occasion of forming change by the styrenic mixture of the pipeline of packing into (1) supply, when increasing as this low boiling point component, according to its analytical results and distillation tower in the measurement result of temperature make temperature in the distillation tower be controlled at feedforward calculation in the set(ting)value, by its output signal, when the extraction amount of control valve (30) low boiling point component increases, because the condensing temperature of the low boiling point component steam in reboiler (13) improves, the heat transfer quantitative change is big, by control control valve (25) pressure in the reboiler (13) is risen.The occasion that reduces at low boiling point component just can adopt the antipodal control method of occasion that increases with above-mentioned low boiling point component conversely.
Also have, the heating source of distillation tower (2) has only above-mentioned reboiler (13) to supply with and insufficient occasion and in order to supply with heat required when starting, and just requires at distillation tower (2) the auxiliary reboiler (31) that imports external heat sources such as steam to be set.In the time of the beginning distillatory, in distillation tower (2), add distillating material and low boiling point component in advance, with above-mentioned auxiliary reboiler (31) to its heat with the total reflux state begin the distillation, and liquid flows to pipeline (20) from pipeline (34) at the bottom of the tower, pack into and give hot device (16) and afterwards cat head distilled low boiling point component steam is given heat, give the hot low boiling point component steam of crossing to circulating line (3) (6) (8) (10) (12) (17) (20) (22) and (24) with this, give hot device (16), compressor (7), reboiler (13) and gas-liquid separator tank (18) give heat, 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 point component steam flows to the gas that heavily boils (13) and changes normal running over to by compression.
And then in this embodiment, when the Distallation systm entry into service and resemble under the few occasion of low boiling point component steam in the gas-liquid separation groove (18), resemble the rare gas element that also can in gas-liquid separation groove (18), import nitrogen etc. can controlling condensing pressure satisfactorily.
Embodiment 1
Distallation systm according to embodiment shown in Figure 1, the dehydrogenated oil that ethylbenzene dehydrogenation is obtained composition as shown in table 1 is distilled, and the differential pressure between this time distillation is to use at the bottom of the distillation tower of having filled standard weighting material (SULzER BROTHERS LTD produces, commodity MELLAPAK by name), the cat head-Ta is controlled at below the 70mmHg.The running of this distillation tower is the stable supplying dehydrogenated oil, extracts 40 minutes low boiling point component liquid out and became separatory 60 minutes from pipeline (4) extraction high boiling point from pipeline (11) in proportion.Flow, the temperature and pressure of each measuring point A, B, C, D and E that the foregoing description is represented all are to be controlled to be the represented value of table 2.The composition of Extract is just as shown in table 1 at the bottom of the low boiling point component of distillation tower (2) and the tower.
This embodiment can quite stable ground carries out cinnamic distillation, also have the energy that compressor (7) consumed and the occasion of only using steam to compare has only it average about 30%, has tangible saving usefulness to obtain proving to the consumption of the energy.
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 0.04
Ethylbenzene 34.45 90.50 0.04
Vinylbenzene 61.88 1.86 97.61
Heavy constituent 0.48-2.31
Water 0.11--
Table 2
The flow temperature, pressure
Measuring point (A=100) (℃) (mmHg)
A 100 73 105
B 95 83 90
C 95 124～126 425
D 90 120 -
E 5 120 110
Embodiment 2
Embodiment 2
This enforcement uses the dehydrogenated oil as dehydrogenated oil replacement the foregoing description 1 of the represented composition of table 3 to distill.The low boiling point component of distillation tower (2) and at the bottom of the tower composition of Extract 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, adopt this embodiment 2 equally also can carry out cinnamic distillation in quite stable ground.
Table 3
Extract at the bottom of the composition dehydrogenated oil overhead product tower
(weight %) (weight %) (weight %)
Benzene 0.10 0.21-
Toluene 0.16 0.22-
Non-aromatic hydrocarbon 0.10 0.22 0.04
Ethylbenzene 37.59 97.20 0.04
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） （℃） （mmHg）
A 100 75 105
B 88 83 90
C 88 125 425
D 86 120 -
E 2 120 110
Embodiment 3
This embodiment except from pipeline (1) with 100 minutes/hour speed pack into dehydrogenated oil, extract high boiling point with 64 minutes/hour speed out from pipeline (4) when extracting low boiling point component liquid out with 36 minutes/hour speed and become the separatory difference all to adopt the method identical to distill with embodiment 1 with the outside from pipeline (11), the flow of measuring point A is 270 minutes/hour, and 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.Adopt this embodiment 3 equally also can carry out cinnamic distillation in quite stable ground.
Table 5
Measuring point flow temperature, pressure
（A＝100） （℃） （mmHg）
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
Errata
Errata
Claims (4)
1, the styrenic mixture that the dehydrogenation of ethylbenzene class is obtained distills, in separating phenylethylene class and ethylbenzene class, import above-mentioned styrenic from pars intermedia with the distillation tower of the packed tower pattern of depressurized system running, become separatory at the high boiling point of extracting out based on styrenic from the cat head of above-mentioned distillation tower, carry out adiabatic compression and make after it heats up by part or all of above-mentioned low boiling point component steam being imported compressor, import in the reboiler of distillation tower, by make its part or all carry out the condensing heating source that is used as above-mentioned reboiler and use.Next, the low boiling point component after condensing and with this not the part of condensing steam go back to the distillation tower circulating line again, remainingly discharge distillating method for the little styrenic of the present invention's spy from Distallation systm.
2, the distillating method of the styrenic of record in the 1st of patent claimed range, the low boiling point component reboiler is condensing after are to go into the distillating method of styrenic of the thermal source use of giving hot machine of the low boiling point component steam of compressor as giving thermal conductance.
3, the distillating method of the styrenic of record in the 1st of patent claimed range, as temperature in the measuring point with operation is the distillation tower of position becomes design temperature, to the extraction amount of low boiling point component and/, or when the heat transfer capacity of reboiler draws joint control system, 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 feed forward control calculation, the distillating method of the styrenic of the pressure in the reboiler being regulated automatically by its output signal.
4, in the 1st of patent claimed range, the record distillating method of the styrenic that carries, be provided with one to import the auxiliary reboiler of external heat source at distillation tower, give earlier and in distillation tower, add distillating material and low boiling point component, heat with above-mentioned auxiliary reboiler again and make its state begin to distill, proceed to liquid at the bottom of the distillation Tata that carried out heating between stable with distillation and use distillating method as styrenic as the thermal source that gives hot device of the low boiling point component steam that imports compressor with total reflux.
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 true CN85102732A (en) | 1986-10-15 |
| CN1006786B 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) |
Cited By (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 |
| 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 |
| CN102186546B (en) * | 2008-10-27 | 2014-03-19 | 环球油品公司 | Improved heat pump for high purity bottom product |
| CN104027997A (en) * | 2013-03-04 | 2014-09-10 | 日本瑞环株式会社 | Solution processing device |
| CN104159876A (en) * | 2012-03-05 | 2014-11-19 | 环球油品公司 | Distillation column heat pump with compressor inlet superheater |
| CN105588472A (en) * | 2016-03-08 | 2016-05-18 | 北京国电龙源环保工程有限公司 | Thermal load distribution device and method for separation system through steam direct-contact heating method |
| CN105669354A (en) * | 2014-11-20 | 2016-06-15 | 中国石油化工股份有限公司 | Ethylbenzene dehydrogenation reaction product separation method |
| CN105669353A (en) * | 2014-11-20 | 2016-06-15 | 中国石油化工股份有限公司 | Ethylbenzene and styrene separation method |
| CN106994260A (en) * | 2016-01-26 | 2017-08-01 | 东洋工程株式会社 | The method that the load exchanged heat to being thermally integrated in destilling tower is adjusted |
| CN109675332A (en) * | 2017-10-19 | 2019-04-26 | 中国石化工程建设有限公司 | Heat pump driven toluene tower fractionating device and method |
| CN109675333A (en) * | 2017-10-19 | 2019-04-26 | 中国石化工程建设有限公司 | Heat pump driven benzene column fractionating device and method |
-
1985
- 1985-04-15 CN CN 85102732 patent/CN1006786B/en not_active Expired
Cited By (20)
| 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 |
| CN102186546B (en) * | 2008-10-27 | 2014-03-19 | 环球油品公司 | Improved heat pump for high purity bottom product |
| CN104159876A (en) * | 2012-03-05 | 2014-11-19 | 环球油品公司 | Distillation column heat pump with compressor inlet superheater |
| CN104159876B (en) * | 2012-03-05 | 2017-11-24 | 环球油品公司 | Destilling tower heat pump with suction port of compressor superheater |
| CN104027997B (en) * | 2013-03-04 | 2016-08-17 | 日本瑞环株式会社 | Function Solution Handling Device Used |
| CN104027997A (en) * | 2013-03-04 | 2014-09-10 | 日本瑞环株式会社 | Solution processing device |
| 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 |
| CN105669354A (en) * | 2014-11-20 | 2016-06-15 | 中国石油化工股份有限公司 | Ethylbenzene dehydrogenation reaction product separation method |
| CN105669353A (en) * | 2014-11-20 | 2016-06-15 | 中国石油化工股份有限公司 | Ethylbenzene and styrene separation method |
| 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 |
| CN106994260A (en) * | 2016-01-26 | 2017-08-01 | 东洋工程株式会社 | The method that the load exchanged heat to being thermally integrated in destilling tower is adjusted |
| CN106994260B (en) * | 2016-01-26 | 2020-06-23 | 东洋工程株式会社 | Method for adjusting load of heat exchange in heat integration distillation tower |
| 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 |
| CN105588472A (en) * | 2016-03-08 | 2016-05-18 | 北京国电龙源环保工程有限公司 | Thermal load distribution device and method for separation system through steam direct-contact heating method |
| CN109675332A (en) * | 2017-10-19 | 2019-04-26 | 中国石化工程建设有限公司 | Heat pump driven toluene tower fractionating device and method |
| CN109675333A (en) * | 2017-10-19 | 2019-04-26 | 中国石化工程建设有限公司 | Heat pump driven benzene column fractionating device and method |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1006786B (en) | 1990-02-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR900008691B1 (en) | Distillation method of stirenes | |
| CN85102732A (en) | The distillating method of styrenic | |
| CN101980758B (en) | Batch process and system for the production of olefins | |
| RU2421264C2 (en) | Plant to produce alcohol by distillation, particularly, ethanol from fermented spent wort | |
| US4277268A (en) | Heat pump fractionation process | |
| CN1163289C (en) | Cascade reboiling of ethylbenzene/styrene columns | |
| KR100811971B1 (en) | Distillation system and distillating method thereof | |
| US8002952B2 (en) | Heat pump distillation | |
| CA2813892A1 (en) | Low energy distillation system and method | |
| JPH0256395B2 (en) | ||
| RU2672591C1 (en) | Improvements relating to propylene oxide purification | |
| Hernandez | Analysis of energy‐efficient complex distillation options to purify bioethanol | |
| US4645569A (en) | Process for producing anhydrous ethanol | |
| CN105829269A (en) | Energy efficient naphthene recycle via the use of a side draw fractionation tower and partial condensation | |
| CN102659508A (en) | Process method for vinyl chloride separation and refining | |
| CN107551586A (en) | A kind of device using next door tower combination multi-effect distillation production methanol | |
| US4230535A (en) | Heat-pumped fractionation process | |
| Horiuchi et al. | Energy-saving characteristics of heat integrated distillation column technology applied to multi-component petroleum distillation | |
| JPH11315051A (en) | Distiller for 2,2,4-trimethyl-1,3-pentanediol isobutyrates and their distillation | |
| JP4220345B2 (en) | Heat exchange apparatus using tower top vapor and tower bottom liquid and heat exchange method thereof | |
| JPH0568282B2 (en) | ||
| CN208151335U (en) | A kind of tower continuous distiller of full-automatic buffer pool | |
| RU2394064C2 (en) | Procedure for oil refining | |
| RU2802428C1 (en) | Method for styrene purification using combined action of falling film reboilers and heat pump technology to obtain a heat source for separating column | |
| CN208604042U (en) | Separate the device of sec-butyl alcohol and methyl ethyl ketone |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C13 | Decision | ||
| C14 | Grant of patent or utility model | ||
| C19 | Lapse of patent right due to non-payment of the annual fee |