CN107540508A - The method and its equipment of a kind of producing phenyl ethylene by ethyl benzene catalytic dehydrogenation - Google Patents
The method and its equipment of a kind of producing phenyl ethylene by ethyl benzene catalytic dehydrogenation Download PDFInfo
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Abstract
The invention provides a kind of method of producing phenyl ethylene by ethyl benzene catalytic dehydrogenation and its equipment, solves the problems, such as that a large amount of water vaporize repeatedly in the prior art and condensation causes high energy consumption.This method comprises the following steps：First supply low-pressure steam and main steam and mixed with ethylbenzene raw material, generate the gaseous mixture of ethylbenzene and water vapour, then carry out catalytic dehydrogenating reaction, be finally separating out styrene product；Wherein, low-pressure steam is 5% ~ 6% relative to percentage of the main steam with throughput with throughput, low-pressure steam and main steam and is recycled back into the gross mass of lime set and the mass ratio of ethylbenzene raw material and is reduced to 1.0~1.2.The present invention is reduced and the heat of reduction and the heat supplemented with throughput by increasing low-pressure steam to make up reduction water/ethylbenzene than caused overheat main steam flow, to keep 815~855 DEG C of main steam temperature of overheat constant, thus, the comprehensive energy consumption of the equipment of production styrene provided by the present invention declines 10.0~25.0 kilograms of mark oil/ton styrene products compared to prior art.
Description
Technical field
The invention belongs to chemical technology field, and in particular to a kind of method of producing phenyl ethylene by ethyl benzene catalytic dehydrogenation and adopt
With the equipment of this method production styrene.
Background technology
Styrene monomer is important basic organic chemical industry raw material, is widely used in production polystyrene PS, foam polyphenyl second
Alkene EPS and ABS synthetic resin etc., it additionally can be used for production ion exchange resin, agricultural emulsifier, pharmaceuticals, coating etc., because
This, styrene is the important basic organic chemical industry raw material of petrochemical industry, and polythene PE, polyvinyl chloride are only second to available for production
PVC, oxirane EO the fourth-largest ethylene derivative product, its yield are only second to polythene PE, polyvinyl chloride in synthetic resin
PVC, occupy the 3rd.
Ethylbenzene dehydrogenation technique is current main styrene industrial process, and in the method, material ethylbenzene steams in water
Vapour（As heat carrier）Gasify under the conditions of existing, and further provide the required heat of reaction with water vapour and carry out gas phase catalysis
Dehydrogenation reaction.At present, in the world the production capacity of Styrene Process tended to maximization and super-hugeization, and further to
Low energy consumption direction is developed.The styrene device that China is built is synchronous with world development trends, therefore, develops competing with low energy consumption
Striving the styrene Production of power has important significance of scientific research and economic benefit, and this is also the long-term research of Chemical R ＆ D personnel
One of focus.
In order to effectively reduce the energy consumption of styrene Production, prior art provides a variety of methods.
For example, Chinese patent CN 86108265A provide one kind uses benzene second under with the presence of water vapour and hot conditions
Alkane dehydrogenation produces the technique of styrene, wherein, including low temperature heat recovering process and vinylbenzene --- the improvement of water vapour charging,
Also, various dehydrogenation products are being separated, it is real to the condensation heat generally to be lost when vinylbenzene is separated particularly from styrene
The recovery of low-temperature heat quantity is showed, and has entered the vinylbenzene and water feeding liquid of dehydrogenation reactor with the heat vaporization of recovery, simultaneously should
Technique is also without using compressor.However, in this technique water vapour charging be improved to water vapour：Vinylbenzene=1.0~
Between 2.2, it is seen that the mass ratio of water vapour and ethylbenzene is higher, and therefore, integrated artistic energy consumption is still higher.
And for example, Chinese patent CN103664497 A disclose a kind of method of producing phenyl ethylene by ethyl benzene catalytic dehydrogenation, one
Determine solve the problems such as Styrene Process amount of steam is big, conversion ratio is low and equipment investment is big in degree.But, this side
The water vapour used in method：The mass ratio of ethylbenzene is 0.8 ~ 2.0:1, it is still higher, therefore, the energy of consumption needed for supply water vapour
Measure the space also further reduced.
Chinese patent CN1587242 A disclose a kind of improved method of producing phenyl ethylene by ethyl benzene catalytic dehydrogenation, wherein, water
Steam is divided into two strands in the first stage by heat exchanger come heating response effluent in second stage, its main body water vapour in
The porch of first dehydrogenation reactor mixes with ethylbenzene, and another strand of supplement water vapour is in the porch of the second dehydrogenation reactor with the
One dehydrogenation reactor outlet material mixes；However, the mass ratio of total water vapour therein and ethylbenzene is 1.2 ~ 1.8:1, water vapour
It is higher with the mass ratio of ethylbenzene；And for example Chinese patent CN102258877 A disclose a kind of evaporation side of ethylbenzene and water azeotropic mixture
Method and device, methods described include the flow of ethylbenzene and water evaporation, and the flow substantially increases driving force of heat transfer, and available
95-100 DEG C of low level energy steam, so as to reach the purpose of energy-conservation；But the water in the device：Ethylbenzene=0.5~2.0, and second
Benzene is not gasified totally.
It is well known that it is to reduce the matter of water vapour and ethylbenzene raw material to reduce one of key point of styrene Production energy consumption
Amount ratio（It may be simply referred to as water/ethylbenzene ratio）；However, above-mentioned prior art often employs higher water/ethylbenzene ratio, a large amount of water be present
The process that iterative cycles are vaporized and condensed, energy utilization is very unreasonable, therefore causes the high technical problem of energy consumption.
The content of the invention
In order to solve the technical problem of styrene Production high energy consumption, and overcome many disadvantages of the prior art, especially
It is to employ higher water/ethylbenzene ratio（The mass ratio of water vapour and ethylbenzene raw material）This major defect, inventor intend providing
A kind of new process of producing phenyl ethylene by ethyl benzene catalytic dehydrogenation.
As it is well known to the skilled in the art, because ethylbenzene dehydrogenation reaction is the endothermic reaction, the reactor of modern designs
For adiabatic reactor, therefore while water/ethylbenzene ratio is effectively reduced, it is necessary to which improving the temperature of overheat main steam could meet to take off
The heating demand of hydrogen reaction；And the overheat main steam temperature from water vapour superheater is by water vapour superheater furnace tube material
Limitation, generally can not further be improved.Therefore, how on the premise of furnace tube material is not changed without increasing cost of investment, both
It is the technological difficulties for reaching target of the present invention that it is more sufficiently high than the temperature for ensureing overheat main steam again, which effectively to reduce water/ethylbenzene,.
In order to further overcome above-mentioned technological difficulties, the first aspect of the present invention, there is provided a kind of ethylbenzene catalytic dehydrogenation life
The method for producing styrene, comprises the following steps：Low-pressure steam and main steam are supplied first and is mixed with ethylbenzene raw material, with generation
The gaseous mixture of ethylbenzene and water vapour, catalytic dehydrogenating reaction is then carried out, is finally separating out styrene product；Wherein, it is well known that
Low-pressure steam and main steam are water vapour；Wherein, low-pressure steam matches somebody with somebody the percentage of throughput with throughput relative to main steam
For 5% ~ 6%, low-pressure steam and main steam and to be recycled back into the gross mass of lime set with the mass ratio of ethylbenzene raw material be 1.0~1.2.
Wherein, the lime set that is recycled back into is from the separator for separating phenylethylene product and the ethylbenzene not reacted completely, wherein
It is main to include the condensate recycled.
Method provided by the present invention employs conventional ethylbenzene catalytic dehydrogenation technique and relevant apparatus, its key problem in technology point
It is that significantly improving low-pressure steam matches somebody with somebody throughput.Wherein, low-pressure steam and main steam and it is recycled back into the gross mass of lime set
Mass ratio with ethylbenzene raw material is generally described water/ethylbenzene ratio.
It can be seen that present invention employs technological means of the low-pressure steam with throughput is improved, so as to by increasing low-pressure steam
The heat supplemented with throughput is reduced and the heat of reduction to make up reduction water/ethylbenzene than caused overheat main steam flow
Amount, to keep overheat main steam temperature constant, to solve the water vapour superheater furnace tube material temperature caused by reducing water/ethylbenzene ratio
The problem of degree does not tolerate, reach the technical purpose for meeting ethylbenzene catalytic dehydrogenation reaction heating demand.
In addition, the second aspect of the present invention, there is provided a kind of method using described in first aspect present invention produces benzene second
The equipment of alkene, including：Gaseous mixture generating means, for providing the gaseous mixture of ethylbenzene and water vapour；It is connected to the gaseous mixture life
Into the catalytic dehydrogenating reaction device after device, generation styrene is reacted for ethylbenzene catalytic dehydrogenation；It is de- to be connected to the catalysis
Separator after hydrogen reaction unit, for separating phenylethylene product and the ethylbenzene not reacted completely；
Characterized in that, the gaseous mixture generating means include：Ethylbenzene evaporator, ethylbenzene/water/steam separator, azeotropic heat exchange
Device, water vapour superheater, ethylbenzene superheater；
Wherein, the ethylbenzene evaporator is heated using heating steam, and is provided with ethylbenzene feed(raw material)inlet and low-pressure steam enters
Mouth, and the mixed gas outlet of ethylbenzene and water vapour, the outlet are located at the ethylbenzene evaporator top；Ethylbenzene raw material is divided into two
Stock, wherein one ethylbenzene raw material enters the ethylbenzene evaporator through the ethylbenzene feed(raw material)inlet；
Wherein, the ethylbenzene/water/steam separator be provided with entry to mixed solution, gas phase ethylbenzene/steam entry, gas phase ethylbenzene/
Steam outlet, bottom water export and bottom ethylbenzene flow export；The bottom water export connects water-circulating pump by pipeline,
The output pipe of the water-circulating pump is connected to the azeotropic heat exchanger；The bottom ethylbenzene flow export connects ethylbenzene by pipeline
Circulating pump, the output pipe of the EB Circulation Pump are also connected to the azeotropic heat exchanger；The entry to mixed solution is used to receive
Another strand of ethylbenzene raw material, liquid phase ethylbenzene/water from the azeotropic heat exchanger and the mixed liquor for being recycled back into lime set；Wherein, institute
State and be recycled back into lime set and come from the separator, wherein including the condensate recycled；
Wherein, the azeotropic heat exchanger is provided with gas phase ethylbenzene/steam outlet, liquid phase ethylbenzene/water out, flow inlet and second
Benzene inflow entrance；
Wherein, the water vapour superheater is provided with main steam inlet and overheat main-steam outlet, the overheat main-steam outlet
Pass through pipeline connection to the ethylbenzene superheater；
Wherein, the ethylbenzene superheater is provided with overheat main steam inlet, gas phase ethylbenzene/water vapour mixing entrance and high temperature second
Benzene/steam outlet；Gas phase ethylbenzene/water vapour and the ethylbenzene/water of the upper outlet output of the ethylbenzene evaporator/
Gas phase ethylbenzene/water vapour of the gas phase ethylbenzene of steam separator/steam outlet output mixes into mixed pipe line, described
Mixed pipe line is communicated to the gas phase ethylbenzene/water vapour mixing entrance；The second of the high temperature ethylbenzene/steam outlet output generation
The gaseous mixture of benzene and water vapour.
The gaseous mixture of above-mentioned ethylbenzene and water vapour subsequently enters catalytic dehydrogenating reaction device and reacted, and produces styrene
Product；The separator, including destilling tower, with the ethylbenzene for being sufficiently separated styrene product and not reacting completely.
Preferably, in the said equipment, it is described overheat main-steam outlet output overheat main steam temperature be 815~
855℃。
Preferably, in the said equipment, the flow for being recycled back into lime set matches somebody with somebody the percentage of throughput relative to main steam
Than for 14% ~ 15%.
It is further preferred that in the said equipment, the low-pressure steam matches somebody with somebody air-flow with throughput relative to the main steam
The percentage of amount is 5.4% ~ 5.6%, and the flow for being recycled back into lime set matches somebody with somebody the percentage of throughput relative to the main steam
Than for 14.1% ~ 14.5%.
Preferably, in the said equipment, the flow of the heating steam matches somebody with somebody the percentage of throughput relative to the main steam
Than for 9.8% ~ 10.0%.
Preferably, in the said equipment, the catalytic dehydrogenating reaction device includes radial reactor or axial flow reactor.
It is further preferred that in the said equipment, the reaction pressure in the radial reactor or axial flow reactor is
0.05~0.1 MPa。
The method and use this method of producing phenyl ethylene by ethyl benzene catalytic dehydrogenation provided by the present invention produce styrene
Equipment, compared with prior art, have the following technical effect that：
（1）Due to using power-saving technology of the low water/ethylbenzene provided by the present invention than producing styrene, avoiding a large amount of water repeatedly
The process for being vaporized and condensing is circulated, the reasonable utilization of energy is realized, successfully solves styrene Production energy consumption
High technical problem；
（2）Method and its equipment provided by the present invention, improve low-pressure steam and match somebody with somebody throughput, so as to by increasing low-pressure steam
The heat supplemented with throughput is reduced and the heat of reduction to make up reduction water/ethylbenzene than caused overheat main steam flow
Amount, to keep overheat main steam temperature constant, while meeting that ethylbenzene catalytic dehydrogenation reacts heating demand, also efficiently solve
The technical problem that water vapour superheater furnace tube material temperature does not tolerate caused by reducing water/ethylbenzene ratio；
（3）Method and its equipment provided by the present invention, on the premise of water/ethylbenzene ratio is reduced, in order to keep overheating main steam
Temperature-resistant, increase low-pressure steam reduces main steam and matches somebody with somebody throughput with throughput, while reduces the stream for being recycled back into lime set
Amount, so as to effectively reduce water vapour superheater fuel gas consumption, and heat steam used by reducing ethylbenzene evaporator and disappear
Consumption, thus, the comprehensive energy consumption of the equipment of the final production styrene have dropped 10.0~25.0 kilograms of mark oil/ton styrene production
Product.
In summary, the method for producing phenyl ethylene by ethyl benzene catalytic dehydrogenation provided by the present invention and use this method produce
The equipment of styrene can significantly reduce the comprehensive energy consumption of production of styrene, therefore be with a wide range of applications and good city
Field prospect.
Brief description of the drawings
Fig. 1 is the mixing that ethylbenzene and water vapour are generated in the method for producing phenyl ethylene by ethyl benzene catalytic dehydrogenation of the present invention
The process flow diagram of steam.
Reference in Fig. 1 is respectively：1- ethylbenzene evaporators；2- ethylbenzene/water/steam separator；3- water-circulating pumps；4-
EB Circulation Pump；5- ethylbenzene raw materials；One ethylbenzene raw material of 5a-；Another strand of ethylbenzene raw material of 5b-；6- low-pressure steams；7- heating is steamed
Vapour；8- azeotropic heat exchangers；9- gas phases ethylbenzene/water vapour；10- is recycled back into lime set；11- liquid phase ethylbenzenes/water；12- ethylbenzene overheats
Device；13- overheats main steam；14- high temperature ethylbenzene/water vapour；15- gas phases ethylbenzene/water vapour；16- gas phases ethylbenzene/water vapour；17-
Water vapour superheater；18- main steams.
Embodiment
The present invention is described in more detail below by specific embodiment, to more fully understand the present invention,
But following embodiments are not intended to limit the scope of the invention.
In a preferred embodiment, method of the present invention according to technological process as shown in Figure 1 generate ethylbenzene and
The gaseous mixture of water vapour.Wherein, the fresh ethylbenzene raw material 5 from the external world is split as two strands first, one ethylbenzene therein
Raw material 5a enters ethylbenzene evaporator 1 under flow control；At the same time, low-pressure steam 6 also enters in the ethylbenzene evaporator 1, and two
Stock material is after heating steam 7 heats, and all gasification is gas phase ethylbenzene/water vapour 15, and from the top of the ethylbenzene evaporator 1
Outlet discharge.Another gang of ethylbenzene raw material 5b and liquid phase ethylbenzene/water 11 and it is recycled back into lime set 10 and merges, and blended liquid entrance enters
Enter ethylbenzene/water/steam separator 2, gas phase ethylbenzene/water vapour 9 also entered by gas phase ethylbenzene/steam entry the ethylbenzene/water/
In steam separator 2, the separation of ethylbenzene, water, steam is carried out together；
Arranged from gas phase ethylbenzene/water vapour 16 that the ethylbenzene/water/steam separator 2 is isolated by gas phase ethylbenzene/steam outlet
Go out；And the water isolated then flows out from bottom water export, after the supercharging of water-circulating pump 3, azeotropic heat exchanger 8 is conveyed into；
And the ethylbenzene isolated then flows out from bottom ethylbenzene flow export, after the supercharging of EB Circulation Pump 4, azeotropic heat exchange is also conveyed into
Device 8；In the azeotropic heat exchanger 8, a part of material steam raising is gas phase ethylbenzene/water vapour 9, and another part material then turns into
Unvaporized liquid phase ethylbenzene/water 11.
On the other hand, main steam 18 enters water vapour superheater 17 by jet chimney, is heated to be overheat main steam 13,
Exported from the water vapour superheater 17；The overheat main steam 13 and gas phase ethylbenzene/water vapour 15, gas phase ethylbenzene/water vapour 16
After merging, high temperature ethylbenzene/water vapour 14 is further superheated in ethylbenzene superheater 12；
After the high temperature ethylbenzene/water vapour 14 reaches dehydrogenation reaction temperature, the beds in dehydrogenation reaction device are immediately entered；
Under negative pressure adiabatic condition, catalytic dehydrogenating reaction generation styrene crude product occurs for ethylbenzene；Finally, benzene is isolated by separator
Ethylene product and the ethylbenzene not reacted completely（It is not shown in Fig. 1）.
Comparative example 1
Using 60,000 tons/year of styrene of prior art production scale：Wherein, it is 825 DEG C to overheat main steam temperature, main steam quality
It is 1.5 with ethylbenzene material quality ratio, main steam matches somebody with somebody the ton hour of throughput 8.79, is recycled back into the ton hour of condensate flow 2.68,
Heat the ton hour of steam flow 3.35, water vapour superheater fuel consumption 28.15GJ/ hours.
Embodiment 1
Using 60,000 tons/year of styrene of method production scale of the present invention：Wherein, it is 825 DEG C to overheat main steam temperature, low
It is 1.1 to press the gross mass of steam and main steam and the mass ratio of ethylbenzene raw material, and main steam matches somebody with somebody the ton hour of throughput 7.03, low pressure
Steam matches somebody with somebody the ton hour of throughput 0.38, is recycled back into the ton hour of condensate flow 0.99, heats the ton hour of steam flow 0.69,
Water vapour superheater fuel consumption 22.67GJ/hour.Compared with comparative example 1, comprehensive energy consumption reduces by 17.16 kilograms of mark oil/tons
Styrene product.
Comparative example 2
Using 800,000 tons/year of styrene of prior art production scale：Wherein, it is 825 DEG C to overheat main steam temperature, main steam quality
It is 1.5 with ethylbenzene material quality ratio, main steam matches somebody with somebody the ton hour of throughput 117.21, is recycled back into 35.67 tons of condensate flow/small
When, heat the ton hour of steam flow 44.69, water vapour superheater fuel consumption 375.39GJ/hour.
Embodiment 2
Using 800,000 tons/year of styrene of method production scale of the present invention：Wherein, it is 825 DEG C to overheat main steam temperature, low
It is 1.1 to press the gross mass of steam and main steam and the mass ratio of ethylbenzene raw material, and main steam matches somebody with somebody the ton hour of throughput 93.77, low pressure
Steam matches somebody with somebody the ton hour of throughput 5.10, is recycled back into the ton hour of condensate flow 13.25, heats the ton hour of steam flow 9.26,
302.22 GJ of water vapour superheater fuel consumption/hour.Compared with comparative example 2,19.87 kilograms of mark oil of comprehensive energy consumption reduction/
Ton styrene product.
Comparative example 3
Using 800,000 tons/year of styrene of prior art production scale：Wherein, it is 815 DEG C to overheat main steam temperature, main steam quality
It is 2.0 with ethylbenzene material quality ratio, main steam matches somebody with somebody the ton hour of throughput 156.28, is recycled back into 47.56 tons of condensate flow/small
When, heat the ton hour of steam flow 59.59, water vapour superheater fuel consumption 500.52GJ/hour.
Embodiment 3
Using 800,000 tons/year of styrene of method production scale of the present invention：Wherein, it is 815 DEG C to overheat main steam temperature, low
It is 1.2 to press the gross mass of steam and main steam and the mass ratio of ethylbenzene raw material, and main steam matches somebody with somebody the ton hour of throughput 102.29, low
Pressure steam matches somebody with somebody the ton hour of throughput 5.56, is recycled back into the ton hour of condensate flow 14.45,10.10 tons of steam flow of heating/small
When, 329.70 GJ of water vapour superheater fuel consumption/hour.Compared with comparative example 3, comprehensive energy consumption reduces by 10.02 kilograms of marks
Oil/ton styrene product.
Comparative example 4
Using 800,000 tons/year of styrene of prior art production scale：Wherein, it is 855 DEG C to overheat main steam temperature, main steam quality
It is 1.3 with ethylbenzene material quality ratio, main steam matches somebody with somebody the ton hour of throughput 101.58, is recycled back into 30.92 tons of condensate flow/small
When, heat the ton hour of steam flow 38.73,325.34 GJ of water vapour superheater fuel consumption/hour.
Embodiment 4
Using 800,000 tons/year of styrene of method production scale of the present invention：Wherein, it is 855 DEG C to overheat main steam temperature, low
It is 1.0 to press the gross mass of steam and main steam and the mass ratio of ethylbenzene raw material, and main steam matches somebody with somebody the ton hour of throughput 85.24, low pressure
Steam matches somebody with somebody the ton hour of throughput 4.63, is recycled back into the ton hour of condensate flow 12.05, heats the ton hour of steam flow 8.42,
274.75 GJ of water vapour superheater fuel consumption/hour.Compared with comparative example 4,24.97 kilograms of mark oil of comprehensive energy consumption reduction/
Ton styrene product.
The specific embodiment of the present invention is described in detail above, but is intended only as example, the present invention is not limited to
Particular embodiments described above.To those skilled in the art, any equivalent modifications and replacement carried out to the present invention
Also all among scope of the invention.Therefore, the impartial conversion made without departing from the spirit and scope of the invention and modification,
It all should be contained within the scope of the invention.
Claims (8)
1. a kind of method of producing phenyl ethylene by ethyl benzene catalytic dehydrogenation, comprises the following steps：Low-pressure steam and main steam are supplied first
And mixed with ethylbenzene raw material, the gaseous mixture of ethylbenzene and water vapour is generated, catalytic dehydrogenating reaction is then carried out, is finally separating out benzene second
Alkene product；Characterized in that, low-pressure steam is 5% ~ 6% relative to percentage of the main steam with throughput with throughput, low pressure is steamed
Vapour and main steam and to be recycled back into the gross mass of lime set and the mass ratio of ethylbenzene raw material be 1.0~1.2.
2. a kind of equipment that styrene is produced using the method as described in claim 1, including：Gaseous mixture generating means, are used for
The gaseous mixture of ethylbenzene and water vapour is provided；The catalytic dehydrogenating reaction device being connected to after the gaseous mixture generating means, is used for
Ethylbenzene catalytic dehydrogenation reaction generation styrene；The separator being connected to after the catalytic dehydrogenating reaction device, for separating
Styrene product and the ethylbenzene not reacted completely；
Characterized in that, the gaseous mixture generating means include：Ethylbenzene evaporator, ethylbenzene/water/steam separator, azeotropic heat exchange
Device, water vapour superheater, ethylbenzene superheater；
Wherein, the ethylbenzene evaporator is heated using heating steam, and is provided with ethylbenzene feed(raw material)inlet and low-pressure steam enters
Mouth, and the mixed gas outlet of ethylbenzene and water vapour, the outlet are located at the ethylbenzene evaporator top；Ethylbenzene raw material is divided into two
Stock, wherein one ethylbenzene raw material enters the ethylbenzene evaporator through the ethylbenzene feed(raw material)inlet；
Wherein, the ethylbenzene/water/steam separator be provided with entry to mixed solution, gas phase ethylbenzene/steam entry, gas phase ethylbenzene/
Steam outlet, bottom water export and bottom ethylbenzene flow export；The bottom water export connects water-circulating pump by pipeline,
The output pipe of the water-circulating pump is connected to the azeotropic heat exchanger；The bottom ethylbenzene flow export connects ethylbenzene by pipeline
Circulating pump, the output pipe of the EB Circulation Pump are also connected to the azeotropic heat exchanger；The entry to mixed solution is used to receive
Another strand of ethylbenzene raw material, liquid phase ethylbenzene/water from the azeotropic heat exchanger and the mixed liquor for being recycled back into lime set；Wherein, institute
State and be recycled back into lime set and come from the separator, wherein including the condensate recycled；
Wherein, the azeotropic heat exchanger is provided with gas phase ethylbenzene/steam outlet, liquid phase ethylbenzene/water out, flow inlet and second
Benzene inflow entrance；
Wherein, the water vapour superheater is provided with main steam inlet and overheat main-steam outlet, the overheat main-steam outlet
Pass through pipeline connection to the ethylbenzene superheater；
Wherein, the ethylbenzene superheater is provided with overheat main steam inlet, gas phase ethylbenzene/water vapour mixing entrance and high temperature second
Benzene/steam outlet；Gas phase ethylbenzene/water vapour and the ethylbenzene/water of the upper outlet output of the ethylbenzene evaporator/
Gas phase ethylbenzene/water vapour of the gas phase ethylbenzene of steam separator/steam outlet output mixes into mixed pipe line, described
Mixed pipe line is communicated to the gas phase ethylbenzene/water vapour mixing entrance；The second of the high temperature ethylbenzene/steam outlet output generation
The gaseous mixture of benzene and water vapour.
3. equipment according to claim 2, it is characterised in that the overheat main steam of the overheat main-steam outlet output
Temperature is 815~855 DEG C.
4. equipment according to claim 2, it is characterised in that the flow for being recycled back into lime set is matched somebody with somebody relative to main steam
The percentage of throughput is 14% ~ 15%.
5. equipment according to claim 4, it is characterised in that the low-pressure steam is with throughput relative to the main steam
Percentage with throughput is 5.4% ~ 5.6%, and the flow for being recycled back into lime set matches somebody with somebody throughput relative to the main steam
Percentage be 14.1% ~ 14.5%.
6. equipment according to claim 2, it is characterised in that the flow of the heating steam is matched somebody with somebody relative to the main steam
The percentage of throughput is 9.8% ~ 10.0%.
7. equipment according to claim 2, it is characterised in that the catalytic dehydrogenating reaction device include radial reactor or
Axial flow reactor.
8. equipment according to claim 7, it is characterised in that the reaction pressure in the radial reactor or axial flow reactor
Power is 0.05 ~ 0.1 MPa.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113941163A (en) * | 2021-09-28 | 2022-01-18 | 常州瑞华化工工程技术股份有限公司 | Low-pressure drop type ethylbenzene evaporator and energy-saving process for ethylbenzene vaporization in styrene dehydrogenation reaction system |
| CN114436744A (en) * | 2020-10-20 | 2022-05-06 | 中国石油化工股份有限公司 | Method and system for preparing styrene by ethylbenzene dehydrogenation |
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