KR101997814B1 - Method and apparatus for preparing of styrene and alphamethyl styrene concurrent - Google Patents

Abstract

A method and apparatus for simultaneous production of styrene and alpha methylstyrene that simultaneously produce styrene and alpha methylstyrene while reducing energy usage. The method for producing styrene and alpha methylstyrene at the same time comprises: (a) dehydrogenating ethylbenzene and cumene under a catalyst; (b) recovering heat from the reaction product by the reaction; (c) separating the gaseous phase from at least a portion of the reaction product obtained in the step (b) and sending it to the compression section, separating the condensed water containing water from the liquid phase, recovering the oil containing styrene and alphamethylstyrene step; (d) compressing and cooling at least a portion of the gas phase in the reaction product obtained in the step (c), separating the low boiling point component including hydrogen and carbon dioxide into a gaseous phase, To the step (c); (e) distilling at least a part of the oil containing styrene and alpha methyl styrene recovered in step (c) into an oil containing styrene and an unreacted cumene; (f) recovering styrene from at least a part of the oil containing styrene in step (e), and distilling and separating the oil containing unreacted ethylbenzene; (g) recovering ethylbenzene from at least a part of the unreacted ethylbenzene-containing oil in step (f) and returning it to the reaction part, distilling and separating the oil containing benzene and toluene; (h) recovering the cumene from at least a part of the oil containing the unreacted cumene of the step (e) and returning the cumene to the reaction part, distilling and separating the oil containing the alphamethylstyrene; And (i) recovering alpha methylstyrene from at least a part of the fraction containing alpha methyl styrene in step (h), and distilling and separating residual high boiling point components.

Description

TECHNICAL FIELD The present invention relates to a method and apparatus for simultaneously producing styrene and alphamethylstyrene,

The present invention relates to a method and an apparatus for simultaneously producing styrene and α-methylstyrene, and more particularly, to a method and apparatus for simultaneously producing styrene and α-methylstyrene, And to an apparatus and method for simultaneously manufacturing the same.

As shown in Reaction Scheme 1, the production of styrene monomer (SM) by catalytic dehydrogenation reaction of ethylbenzene (EB) in the presence of high temperature and steam is a well-known method for producing common styrene. Fig. 1 is a diagram showing a typical process for producing styrene. As shown in Fig. 1, styrene (SM) is obtained by dehydrogenating ethylbenzene (EB) and then subjecting the mixture to condensation and fractional distillation It can be seen that it is produced by the process. Benzene (BZ, boiling point: 80.09 ° C) and toluene (TOL, boiling point: 110.63 ° C), which have a relatively low boiling point, are discharged and transferred through the upper part of the distillation column, Styrene (SM, boiling point: 145.16 ℃), which has a relatively high boiling point, is discharged and transferred through the bottom of the distillation column and then separated in a similar manner.

[Reaction Scheme 1]

In addition, a-methylstyrene (AMS), which is used as a main raw material of heat resistant ABS (acrylonitrile butadiene styrene), is mostly obtained as a by-product of the phenol process at present, and its demand is increasing year by year. As shown in Scheme 2, alpha methyl styrene (AMS) can also be obtained by dehydrogenation of cumene (CM), which is similar in structure to ethylbenzene.

[Reaction Scheme 2]

Thus, although methods for producing styrene and alpha methyl styrene are widely known, there is no process capable of simultaneously producing styrene and alpha methyl styrene. When producing styrene and alpha methylstyrene at the same time, energy consumption may vary greatly depending on the configuration of the separation process. Therefore, it is required to develop a method capable of simultaneously producing styrene and alpha methylstyrene which reduce the amount of energy consumed excessively while reducing the inconvenience of separately preparing styrene and alpha methylstyrene .

Korean Patent Publication No. 10-2015-0088892

As described above, although methods for producing styrene and alpha methyl styrene are widely known, there is no process capable of simultaneously producing styrene and alpha methyl styrene. Depending on the composition of the process, . In order to overcome the difficulties of development due to such problems, it is necessary to find a way to make use of advantages such as low cost and high efficiency expected to be obtained by simultaneously producing styrene and alpha methylstyrene.

Accordingly, an object of the present invention is to provide a method and an apparatus for simultaneously producing styrene and alpha methylstyrene, which can improve the economical efficiency by reducing energy consumption while simultaneously producing styrene and alpha methylstyrene will be.

In order to accomplish the above object, the present invention provides a process for producing (a) dehydrogenating ethylbenzene and cumene under a catalyst; (b) recovering heat from the reaction product by the reaction; (c) separating the gaseous phase from at least a portion of the reaction product obtained in the step (b) and sending it to the compression section, separating the condensed water containing water from the liquid phase, recovering the oil containing styrene and alphamethylstyrene step; (d) compressing and cooling at least a portion of the gas phase in the reaction product obtained in the step (c), separating the low boiling point component including hydrogen and carbon dioxide into a gaseous phase, To the step (c); (e) distilling at least a part of the oil containing styrene and alpha methyl styrene recovered in step (c) into an oil containing styrene and an unreacted cumene; (f) recovering styrene from at least a part of the oil containing styrene in step (e), and distilling and separating the oil containing unreacted ethylbenzene; (g) recovering ethylbenzene from at least a part of the unreacted ethylbenzene-containing oil in step (f) and returning it to the reaction part, distilling and separating the oil containing benzene and toluene; (h) recovering the cumene from at least a part of the oil containing the unreacted cumene of the step (e) and returning the cumene to the reaction part, distilling and separating the oil containing the alphamethylstyrene; And (i) recovering alpha methylstyrene from at least part of the fraction containing alpha methyl styrene in step (h), and distilling and separating residual high boiling point components. Lt; / RTI >

The present invention also relates to a reactor comprising a reactor in which a dehydrogenation reaction of ethylbenzene and cumene is carried out under a catalyst; A heat exchanger for recovering heat from the reaction product by the reaction; A decanter separating the gaseous phase from at least a portion of the recovered reaction product and sending it to the compression section, separating the condensed water containing water from the liquid phase, and recovering the oil containing styrene and alpha methyl styrene; Compressing and cooling at least a part of the separated gas phase to separate the low boiling point components including hydrogen and carbon dioxide into a gaseous phase and recovering the liquid phase containing styrene, alphamethylstyrene, ethylbenzene and cumene, A compression unit comprising a heat exchanger and a drum; An SM / CM separation tower for distilling and separating at least a part of the oil containing styrene and alpha-methylstyrene supplied from the decanter, into oil containing the styrene-containing oil and unreacted cumene; An EB / SM separation tower for recovering styrene from at least a part of the styrene-containing oil separated from the SM / CM separation column and distilling and separating into stale oil containing unreacted ethylbenzene; A TOL / EB separation tower for recovering ethylbenzene from at least a part of the oil containing unreacted ethylbenzene separated from the EB / SM separation tower and returning the ethylbenzene to the reactor, distilling and separating the oil including benzene and toluene; A CM / AMS separation tower for recovering cumene from at least a part of the oil containing unreacted cumene separated from the SM / CM separation column and sending it back to the reactor, distilling and separating the oil containing alpha methyl styrene; And an AMS / Heavies separation tower for recovering alpha methyl styrene from at least part of the fraction containing alpha methyl styrene separated from the CM / AMS separation column and distilling off the oil containing residual high boiling point components And an alpha-methylstyrene monomer.

According to the method and apparatus for simultaneously producing styrene and alpha methylstyrene according to the present invention, energy consumption can be reduced while producing styrene and alpha methylstyrene at the same time, and styrene and alpha It is possible to improve the economical efficiency by changing the production ratio of methylstyrene. It is possible to produce styrene and α-methylstyrene at the same time with a low investment cost by modifying the existing process of producing styrene.

Fig. 1 is a diagram showing a typical process for producing styrene.
2 is a process diagram for explaining a method and an apparatus for simultaneously producing styrene and alpha methylstyrene according to an embodiment of the present invention.
3 is a diagram showing a process for producing styrene and alpha methylstyrene according to Comparative Example of the present invention.

Hereinafter, the present invention will be described in detail with reference to the accompanying drawings.

2 is a process diagram for explaining a method and an apparatus for simultaneously producing styrene and alpha methylstyrene according to an embodiment of the present invention. As shown in FIG. 2, the process for the simultaneous production of styrene and alpha methylstyrene according to the present invention comprises: (a) dehydrogenating ethyl benzene (EB) and cumene (CM) (B) recovering heat from the reaction product by the reaction; (c) separating the gaseous phase from at least a portion of the reaction product after the step (b) and sending it to the compression section, (Or condensate), recovering the oil containing styrene (SM) and alpha-methyl styrene (AMS), (d) Compressing and cooling at least a portion of the gas phase in the reaction product to separate the low boiling point component including hydrogen and carbon dioxide into a gaseous phase and the liquid phase comprising styrene, alpha methylstyrene, ethylbenzene and cumene, Back to (E) distilling at least a part of the oil containing styrene and alpha-methylstyrene recovered in the step (c) into an oil containing styrene and an oil containing unreacted cumene, ( f) recovering styrene from at least a part of the oil containing styrene in step (e) and distilling and separating into an oil fraction containing unreacted ethylbenzene, (g) separating the unreacted ethyl (B) recovering ethylbenzene from at least a portion of the oil containing benzene and returning it to the reaction portion, distilling and separating the oil containing benzene (BZ) and toluene (TOL) Recovering cumene from at least a portion of the unreacted cumene of the unreacted cumene and returning it to the reaction part, distilling and separating the oil containing alpha methylstyrene, and (i) recovering the oil containing alpha methylstyrene in step (h) Ha Recovering the alpha-methyl styrene from at least a portion of the oil, and a step of separating high boiling point components distilled off the residue.

In order to produce styrene and alpha methylstyrene simultaneously according to the present invention, first, ethylbenzene and cumene are dehydrogenated under a catalyst (a). That is, in the step (a), ethylbenzene and cumene, which have not existed in the past, are fed to a single reactor 100, so that ethylbenzene and cumene are simultaneously reacted with styrene and alpha methyl Styrene.

The catalyst to be added to the dehydrogenation reaction of ethylbenzene and cumene can be used without limitation as long as it can dehydrogenate ethylbenzene and cumene to obtain styrene and alpha methylstyrene. Examples thereof include iron oxide, Palladium, platinum, aluminum oxide, silicon oxide, ruthenium, rhenium, osmium, rhodium, iridium, cerium, molybdenum, tungsten, vanadium, bismuth, magnesium, potassium, calcium, copper, zinc, arsenic, antimony, And mixtures thereof. On the other hand, the ratio of ethylbenzene to cumene supplied to the reactor 100 (or used for the dehydrogenation reaction) is about 0.1 to 10: 1 by weight, and can be flexibly varied depending on the price of the market.

The dehydrogenation reaction is carried out at a temperature of 300 to 800 ° C, preferably 550 to 650 ° C. Also, as shown in FIG. 2, the steam supplied during the dehydrogenation reaction is a stable and selective reaction (Ethylbenzene and cumene) = 3 to 20: 1, preferably 6 to 12: 1, in terms of molar ratio.

Next, when the dehydrogenation product of step (a) is discharged from the reactor 100, (b) heat is recovered from the reaction product by the reaction, The reaction product is cooled to about 15 to 60 캜, preferably about 50 to 60 캜, in a heat exchanger (200). On the other hand, the heat recovered from the reaction product can be used as energy required in the process or used in an external process.

After the heat is recovered from the reaction product in the step (b), (c) the gas phase is separated from at least a part of the reaction product in which the heat is recovered and sent to a compression part (300) Separating the containing condensate, and recovering the oil containing styrene and alpha-methylstyrene. The process of step (c) is performed in a decanter (400), and the separated condensate may be recycled or discarded in the process.

Subsequently, (d) at least a part of the gas phase in the reaction product obtained in the step (c) is compressed and cooled to separate the low boiling point component including hydrogen and carbon dioxide into a gaseous phase (or vapor phase) That is, the active ingredient containing styrene, alpha-methylstyrene, ethylbenzene and cumene is recovered as a liquid phase and sent back to the decanter 400 of step (c). At this time, the compression unit 400 compresses the reaction product to a pressure of about 1.5 to 5.5 KCA (kgf / cm ² a), preferably about 1.5 to 2.5 KCA. On the other hand, the compression unit is composed of a compressor, a heat exchanger, and a drum.

Next, (e) at least a portion of the oil containing styrene and alpha methyl styrene recovered in step (c) (i.e., supplied from the decanter 400) Distillation is carried out with oil containing unreacted cumene. The process of step (e) is performed in the SM / CM separation tower 500 and includes a cumene having a boiling point relatively higher than that of styrene (SM, boiling point: 145.16 ° C) (CM, boiling point: 152.41 ° C) The oil is discharged to the lower part of the SM / CM separation tower 500, and the oil containing styrene is discharged through the upper part of the SM / CM separation tower 500. And the pressure of the SM / CM separation tower 500 is 0.01 to 5 KCA, preferably 0.1 to 1 KCA.

Next, (f) the styrene is recovered from at least a part of the oil containing the styrene in the step (e), and the distillate is separated from the oil containing unreacted ethylbenzene. The step (f) is carried out in the EB / SM separation tower 600. Styrene (SM, boiling point: 145.16 ° C) having a boiling point relatively higher than ethylbenzene (EB, boiling point: 136.2 ° C) The EB / SM separation tower 600 is discharged to the lower part of the separation tower 600, and the unreacted ethylbenzene is discharged through the upper part of the EB / SM separation tower 600. And the pressure of the EB / SM separation column 600 is 0.01 to 6 KCA, preferably 0.1 to 1 KCA.

Next, (g) ethylbenzene is recovered from at least a part of the unreacted ethylbenzene-containing oil in the step (f) and returned to the reaction part, and the oil including benzene and toluene is distilled off. The step (g) is performed in the TOL / EB separation column 620. Ethylbenzene (EB, boiling point: 136.2 ° C), which has a relatively high boiling point in comparison with toluene (boiling point: 110.63 ° C) EB separation tower 620 and the dehydrogenation reaction is carried out by the TOL / EB separation column 620. The oil containing the benzene and the toluene is returned to the reaction section (or the reactor 100) As shown in FIG. These benzenes and toluenes are by-products produced during the dehydrogenation and separation processes, but can be useful if they are recovered using additional equipment. And the pressure of the TOL / EB separation column 620 is 0.01 to 7 KCA, preferably 1 to 2 KCA.

(H) recovering the cumene from at least a part of the oil containing the unreacted cumene of the step (e) and returning it to the reaction part, and distilling off the oil containing the alphamethylstyrene. The step (h) is performed in the CM / AMS separation tower 520, and the cumene (boiling point: 152.41 ° C) having a boiling point that is relatively lower than the alphamethylstyrene (AMS, boiling point: 165.5 ° C) AMS separation tower 520 and returned to the reaction part (or the reactor 100), and the oil containing the alphamethylstyrene is returned to the lower part of the CM / AMS separation tower 520 ≪ / RTI > And the pressure of the CM / AMS separation column 520 is 0.01 to 8 KCA, preferably 0.1 to 1 KCA.

Finally, (i) the alphamethylstyrene is recovered from at least part of the oil containing alpha methyl styrene in step (h), and the oil containing the residual high boiling point component is separated by distillation. The process of step (i) is carried out in an AMS / Heavies separation tower 700, wherein the alphamethylstyrene (AMS, boiling point: 165.5 [deg.] C), whose boiling point is relatively lower than the residual high boiling point component (boiling point: The residual high boiling point component (boiling point: more than 165.5 ° C.) is discharged to the lower portion of the AMS / Heavies separation column 700. And the pressure of the AMS / Heavies separation tower 700 is 0.01 to 9 KCA, preferably 0.5 to 1.5 KCA.

On the other hand, the recovery of the styrene of step (f) and the recovery of the alpha methylstyrene of step (i) performed after step (e) are performed simultaneously. However, depending on the needs of the user, There is no particular restriction on the posterior relationship, such that any of the alpha methylstyrene recoveries of step (i) can be performed first.

As described above, the simultaneous production of styrene and α-methylstyrene according to the present invention can be carried out by supplying ethylbenzene and cumene to one reactor, Recovery) and alpha methylstyrene (recovered in step (i)) can be produced at the same time, and the production rate of styrene and alpha methylstyrene can be made different depending on the price of the market, thereby improving the economical efficiency. In addition, unreacted ethylbenzene or unreacted cumene, which may be discarded, can be recovered and reused as a raw material, so that productivity of the process can be increased and raw materials can be saved.

Next, with reference to FIG. 2, an apparatus for simultaneously producing styrene and alpha methylstyrene according to the present invention will be briefly described. The apparatus for simultaneously producing styrene and alpha methylstyrene according to the present invention comprises a reactor 100 in which a dehydrogenation reaction of ethylbenzene and cumene is carried out under a catalyst, a heat exchanger 200 for recovering heat from a reaction product by the reaction Separating the gaseous phase from at least a part of the recovered reaction product and sending it to the compression section, separating the condensed water containing water from the liquid phase, recovering the oil containing styrene and alphamethylstyrene, ), The low-boiling component including hydrogen and carbon dioxide is separated into a gas phase by compressing and cooling at least a part of the separated gas phase, and the liquid phase containing styrene, alphamethylstyrene, ethylbenzene and cumene is recovered A compression unit 300 composed of a compressor, a heat exchanger and a drum, a stencil unit 300 which is made of styrene and alpha methylstyrene supplied from the decanter 400, CM separation tower 500 for distilling and separating at least a part of the oil contained in the distillate into an oil containing styrene and an unreacted cumene, a styrene separated from the SM / CM separation tower 500, SM separator 600 for recovering styrene from at least a portion of the oil containing distillate and distilling the distillate into oil fractions containing unreacted ethylbenzene, an unreacted ethylbenzene separated from the EB / SM separator 600 , A TOL / EB separation tower 620 for recovering ethylbenzene from at least a part of the oil containing the benzene and toluene and returning it to the reactor 100, distilling and separating the oil including benzene and toluene, the SM / CM separation tower 500 A CM / AMS separation tower 520 for recovering cumene from at least a part of the oil fraction containing unreacted cumene separated from the CM / AMS separation tower and returning the cumene to the reactor, distilling and separating the oil containing alpha methyl styrene, Separated from the separation tower (520) Recovering the alpha-methyl styrene from at least a portion of the fraction comprising methyl styrene, and includes a residual high boiling point AMS / Heavies distillation to separate a fraction containing a component separating column (700).

The detailed description of the apparatus for producing styrene and alpha-methylstyrene in accordance with the present invention is based on the description of the method for producing the styrene and alpha methylstyrene simultaneously.

As described above, the simultaneous production of styrene and α-methylstyrene according to the present invention can reduce the amount of energy consumed while simultaneously producing styrene and α-methylstyrene. This reduction in energy usage is used in the in-process distillation columns, particularly in the reboilers of the SM / CM separation column 500, the CM / AMS separation column 520 and the EB / SM separation column 600 respectively (See Examples below). This is because the difference in boiling point between styrene, alpha methylstyrene, ethylbenzene and cumene is small and affects the relative volatility of each other, The difference in the amount of energy consumed occurs depending on whether or not it is separated by the method.

Also, by using the method and apparatus for simultaneously producing styrene and alpha methylstyrene according to the present invention, it is possible to simultaneously produce styrene and alpha methylstyrene while using less energy. In addition to improving the economical efficiency by changing the ratio of production of styrene and alpha methyl styrene according to the market prices of raw materials and products, Since simultaneous production of methylstyrene is possible, alpha methylstyrene can be produced at low investment cost.

The present invention relates to a method and an apparatus capable of simultaneously producing styrene and alpha methylstyrene which have not existed in the past, and it is difficult to easily deduce from existing known techniques, It is more a technology that requires special attention in the process composition and the like because there is a possibility that the economical efficiency may be lower than the technology in which the existing styrene and alpha methylstyrene are independently produced. The influence of the present invention can be said to be small. That is, the present invention can simultaneously reduce the amount of energy consumed excessively depending on the constitution of the separation process while controlling the production amount more flexibly, while simultaneously producing styrene and alpha methylstyrene. In addition, If the process of independently producing the existing styrene and alpha methyl styrene is modified, it can be constructed with a low investment cost.

It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the spirit or scope of the inventions. , And that such changes and modifications are within the scope of the appended claims.

[Example 1] Simultaneous production of styrene and alpha methylstyrene

As shown in FIG. 2, a styrofoam comprising a reactor, a heat exchanger, a compression section, a decanter, a SM / CM separation tower, a CM / AMS separation tower, an EB / SM separation tower, a TOL / EB separation tower, and an AMS / Heavies separation tower Ethylene benzene and cumene, which are raw materials, were fed to the reactor in the same amounts as shown in Table 1 below, and styrene and alpha methylstyrene were simultaneously produced using the apparatuses.

Input (kg / hr) Conversion Rate (%) Selectivity (%) Ethylbenzene Cumene Ethylbenzene Cumene Ethylbenzene Cumene Example 1 185,448 99,680 74.2 74.8 94.6 93.8 Comparative Example 1 185,440 99,680 74.2 74.8 95.7 94.5

[Comparative Example 1] Production of styrene and alpha methylstyrene

3 is a diagram showing a process for producing styrene and alpha methylstyrene according to Comparative Example of the present invention. 3, ethylbenzene and cumene as the amounts shown in Table 1 are supplied as raw materials to the reactor 10, and the substances discharged from the decanter 20 are transferred to the EB / SM separation tower 30 And the substances discharged therefrom are transferred to the next distillation column 40 to discharge and recover the styrene SM and the remaining substances such as cumene and alpha methyl styrene are discharged to the lower part to be separated from the CM / ), Styrene and alpha methylstyrene were sequentially produced in the same manner as in Example 1,

[Example 1, Comparative Example 1] Evaluation of the amount of energy used in the production of styrene and alpha methylstyrene

The amount of energy used in each step of Example 1 and Comparative Example 1 in which styrene and alpha-methylstyrene are produced, exactly, the amount of energy used in the reboiler of each distillation column, and the amount of styrene (SM) (AMS) are shown in Table 2 below.

Final production (kg / hr) Reboiler Energy Consumption (Gcal / hr) SM AMS EB / TOL separation tower EB / SM separation tower SM / CM separation tower CM / AMS Separator AMS / Heavies Separator system Example 1 130,120 699,52 0.63 7.44 10.84 3.07 1.31 23.29 Comparative Example 1 131,632 70,408 0.63 27.17 13.13 4.66 1.31 46.90

As shown in Table 2, when the same raw materials were added, the production amounts of the products (SM and AMS) of Example 1 and Comparative Example 1 were similar, but in the case of Example 1, the reboiler energy It can be seen that the amount of use is markedly reduced as compared with Comparative Example 1. [ This is because the difference in boiling point between styrene, alpha methyl styrene, ethyl benzene and cumene is small and affects the degree of volatilization among them, so that a difference in the amount of energy consumed occurs depending on the sequence and method of separating them And Example 1 by the method and apparatus for simultaneously producing styrene and alpha methyl styrene according to the present invention can be said to be optimized.

100: reactor
200: Heat exchanger
300:
400: decanter
500: SM / CM separation tower
520: CM / AMS Separator
600: EB / SM separation tower
620: TOL / EB separation tower
700: AMS / Heavies Separator

Claims (13)

(a) dehydrogenating ethylbenzene and cumene under a catalyst;
(b) recovering heat from the reaction product by the reaction;
(c) separating the gaseous phase from at least a portion of the reaction product obtained in the step (b) and sending it to the compression section, separating the condensed water containing water from the liquid phase, recovering the oil containing styrene and alphamethylstyrene step;
(d) compressing and cooling at least a portion of the gas phase in the reaction product obtained in the step (c), separating the low boiling point component including hydrogen and carbon dioxide into a gaseous phase, To the step (c);
(e) distilling at least a part of the oil containing styrene and alpha methyl styrene recovered in step (c) into an oil containing styrene and an unreacted cumene;
(f) recovering styrene from at least a part of the oil containing styrene in step (e), and distilling and separating the oil containing unreacted ethylbenzene;
(g) recovering ethylbenzene from at least a part of the unreacted ethylbenzene-containing oil in step (f) and returning it to the reaction part, distilling and separating the oil containing benzene and toluene;
(h) recovering the cumene from at least a part of the oil containing the unreacted cumene of the step (e) and returning the cumene to the reaction part, distilling and separating the oil containing the alphamethylstyrene; And
(i) recovering alpha methylstyrene from at least part of the oil containing alpha methyl styrene in step (h), and distilling and separating residual high boiling point components, Simultaneous manufacturing method. The method according to claim 1, wherein the step (f) of recovering the styrene and the step (i) of recovering the alpha-methylstyrene are simultaneously carried out. The process according to claim 1, wherein the ratio of ethylbenzene to cumene used in the dehydrogenation reaction is 0.1 to 10: 1 by weight. The method according to claim 1, wherein the dehydrogenation reaction is carried out at a temperature of 300 to 800 ° C. The method of claim 1, wherein the catalyst is selected from the group consisting of iron oxide, palladium, platinum, aluminum oxide, silicon oxide, ruthenium, rhenium, osmium, rhodium, iridium, cerium, molybdenum, tungsten, vanadium, bismuth, magnesium, , Zinc, arsenic, antimony, chromium iron, cobalt, and mixtures thereof. The method according to claim 1, wherein the reaction product of step (b) is cooled to 15 to 60 占 폚. The process according to claim 1, wherein the reaction product after step (c) is compressed to a pressure of 1.5 to 5.5 KCA. A reactor in which a dehydrogenation reaction of ethylbenzene and cumene is carried out under a catalyst;
A heat exchanger for recovering heat from the reaction product by the reaction;
A decanter separating the gaseous phase from at least a portion of the recovered reaction product and sending it to the compression section, separating the condensed water containing water from the liquid phase, and recovering the oil containing styrene and alpha methyl styrene;
Compressing and cooling at least a part of the separated gas phase to separate the low boiling point components including hydrogen and carbon dioxide into a gaseous phase and recovering the liquid phase containing styrene, alphamethylstyrene, ethylbenzene and cumene, A compression unit comprising a heat exchanger and a drum;
An SM / CM separation tower for distilling and separating at least a part of the oil containing styrene and alpha-methylstyrene supplied from the decanter, into oil containing the styrene-containing oil and unreacted cumene;
An EB / SM separation tower for recovering styrene from at least a part of the styrene-containing oil separated from the SM / CM separation column and distilling and separating into stale oil containing unreacted ethylbenzene;
A TOL / EB separation tower for recovering ethylbenzene from at least a part of the oil containing unreacted ethylbenzene separated from the EB / SM separation tower and returning the ethylbenzene to the reactor, distilling and separating the oil including benzene and toluene;
A CM / AMS separation tower for recovering cumene from at least a part of the oil containing unreacted cumene separated from the SM / CM separation column and sending it back to the reactor, distilling and separating the oil containing alpha methyl styrene; And
And an AMS / Heavies separation tower for recovering alpha methyl styrene from at least a part of the fraction containing alpha methyl styrene separated from the CM / AMS separation column and distilling and separating the oil containing the residual high boiling point component An apparatus for simultaneous production of styrene and alpha methylstyrene. The apparatus of claim 8, wherein the pressure of the SM / CM separation column is 0.01 to 5 KCA. The apparatus of claim 8, wherein the pressure of the EB / SM separation column is 0.01 to 6 KCA. The apparatus of claim 8, wherein the TOL / EB separation column has a pressure of 0.01 to 7 KCA. The apparatus of claim 8, wherein the pressure of the AMS / Heavies separation column is between 0.01 and 9 KCA. The apparatus of claim 8, wherein the pressure of the CM / AMS separator is between 0.01 and 8 KCA.

Images