KR20190086944A - Method of purification for polymerization solvent of preparing process for petroleum resin using dividing wall column - Google Patents

Abstract

An object of the present invention is to provide a method of purifying a polymerization solvent used in a preparing process for a petroleum resin using a dividing wall distillation column, configured to increase energy efficiency of the distillation column, resolving pressure unbalance occurring in the distillation column, and reducing investment costs. According to one embodiment of the present invention, the method of purifying a polymerization solvent used in a preparing process for a petroleum resin using a dividing wall distillation column includes a step of injecting a mixture of the polymerization solvent used in the preparing process for a petroleum resin, into the dividing wall distillation column and fractionally distilling the mixture. The dividing wall distillation column comprises: a main tower having a dividing wall and divided into a top section, a supply section, an outflow section, and a bottom section; a condenser; and a reboiler, wherein the mixture of the polymerization solvent is introduced to the supply section of the main tower, and a purified polymerization solvent is discharged to the outflow section of the main tower.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for purifying a polymer solvent in a petroleum resin manufacturing process using a separation wall type distillation column,

The present invention relates to a purification method using a separation wall type distillation column, and more particularly, to a purification method using a separation wall type distillation column in which a polymerization solvent used in a petroleum resin production process is purified with high purity and recovered for reuse, And a purification method.

It is known that distillation is a representative separation technique that accounts for more than 90% of all separation means in the chemical industry and has the advantage of being able to effectively process large amounts of the mixture.

As shown in FIG. 1, the process for separating three components is mostly a continuous two-stage distillation column (1, 2) structure. The distillation columns 1 and 2 respectively include condensers 1a and 1a, reboilers 1b and 2b and main columns 1c and 2c. The mixture 11 supplied to the first distillation column 1 is separated into the low boiling point component 12 and the primary high boiling point component 13 first. The first high boiling point component 13 discharged to the lower portion of the first distillation column 1 is continuously introduced into the second distillation column 2 continuously. The primary high boiling point component 13 supplied to the second distillation column 2 is finally separated and discharged into the middle boiling point component 14 and the high boiling point component 15.

However, when the continuous two-stage distillation towers 1 and 2 are used, there arises a problem that the thermodynamic efficiency is lowered due to the remixing of the middle boiling point components in the first distillation tower 1, and thus a method for improving the energy efficiency is steadily proposed .

There are many studies on new distillation structures such as control system improvement, external heat integration, process improvement, internal improvement, etc. In particular, new distillation technologies have been developed that dramatically improve energy efficiency through thermal integration. As a representative example thereof, there are a separation wall type distillation column and an internal heat exchange type distillation column. As a representative example of this, there is a Petlyuk distillation column structure of FIG.

The Petlyuk distillation column is composed of a preliminary separator 3 and a main separator 4 and a condenser 4a and a reboiler 4b provided in the main separator 4. The mixture 21 supplied to the preliminary split device 3 is separated into the primary low boiling point component 22 and the primary high boiling point component 23 in the primary separator 3. Subsequently, the primary low boiling point component 22 and the primary high boiling point component 23 introduced into the main separator 4 are introduced into the main separator 4 through the low boiling point component 23, the middle boiling point component 25 and the high boiling point component 25 ).

This has the advantage of fundamentally eliminating the problem of energy efficiency deterioration due to the re-mixing of the intermediate boiling point material which may occur when the two distillation towers (1, 2) are used. However, it is difficult to operate and it is difficult to balance the pressure.

It is an object of the present invention to provide a method for purifying a polymerization solvent in a petroleum resin manufacturing process using a separation wall type distillation column which improves energy efficiency in a distillation column, eliminates pressure imbalance in a distillation column, and reduces investment cost.

The method for purifying a polymerization solvent in a petroleum resin manufacturing process using a separating wall type distillation tower according to an embodiment of the present invention includes a step of introducing a mixture containing a polymerization solvent used in a petroleum resin manufacturing process into a separating wall type distillation column to perform fractional distillation Wherein the separation wall-type distillation column has a separation wall and is divided into a tower zone, a feed zone, an outlet zone, and a bottom zone; Condenser; Wherein the mixture of polymerization solvents is introduced into the feed zone of the main tower and the purified polymerization solvent is flowed out to the effluent zone of the main tower wherein the weight ratio of the first A high boiling point component comprising purified xylene having a second range weight percent lower than the first range is passed through the outlet end of the outflow zone, And flows out to the outlet lower end of the outlet zone.

In the mixture comprising the polymerization solvent, the xylene content may be at least 60% by weight based on the weight of the total mixture.

The first range wt% may be 80 wt%. More specifically, the middle boiling point component may contain at least 80 wt.%, Or at least 85 wt.%, Or at least 90 wt.% Of purified xylene and may flow out to the outflow midway in the outflow zone of the main tower.

The second range weight percentage may be 10 to 20 wt%. More specifically, the high boiling point component may contain 10 to 20% by weight of xylene and may flow out to the outflow lower end of the outflow zone of the main tower.

Also, the temperature of the bottom zone can be maintained between 170 캜 and 190 캜.

Wherein the pressure of the intermediate outlet is 0.12 to 0.18 barg and the temperature of the intermediate outlet is 142 to 144 g / hr when the amount of xylene flowing out through the outlet middle portion is 10,000 to 12,000 kg / hr, Lt; 0 > C.

The mixture comprising the polymerization solvent may comprise at least one of xylene, toluene, cyclohexane and ethylbenzene.

The number of stages of the top zone may be one to twenty, or five to fifteen, and the number of stages of the bottom zone may be one to fifteen, or five to ten, singles.

The number of the dividing walls may be one to thirty or one to twenty-five stages, which may be equal to or less than 60% of the total number of stages of the main tower, independently of the number of stages of the top zone or each stage of the top zone. .

The number of stages of the top zone is from 7 to 12 stages, the stage of the bottom stage is from 7 stages to 9 stages, the number of stages of the separation walls is from 1 stage to 20 stages, and may be less than 60% of the total number of stages of the main tower .

In the feed tower and outflow zone within the main tower, the vapor split ratio of the gas phase flow can be 40:60 to 60:40.

In the feed tower and outflow zone within the main tower, the liquid split ratio of the liquid stream may be 40:60 to 60:40.

The purification purity of the polymerization solvent may be 90% or more.

Thus, one embodiment of the present invention is to improve the disadvantages of the Feltreich distillation column by separating the top zone, the feed zone, the outlet zone and the bottom zone using the separate wall type distillation column and integrating the two distillation columns into one distillation column can do.

That is, one embodiment can increase the energy efficiency in the distillation column because it forms a thermally integrated structure such as the Felt-Yüque distillation column, the topping zone, the feed zone, the outflow zone, and the bottom zone.

One embodiment also eliminates pressure imbalance in the distillation column because the top zone, feed zone, outlet zone, and bottom zone form an integrated structure, and it is possible to reduce the investment cost by installing only one distillation column, have.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic view showing a structure of a continuous two-stage distillation column in a polymerization solvent purification apparatus of a petroleum resin manufacturing process according to the prior art; FIG.
2 is a view showing a structure of a Petlyuk distillation column in a polymerization solvent purification apparatus of a petroleum resin manufacturing process according to the prior art.
FIG. 3 is a view illustrating a polymerization solvent purification apparatus for a petroleum resin production process using a separation wall type distillation tower according to an embodiment of the present invention.
4 is a configuration diagram showing the flow of the mixture in the polymerization solvent purification apparatus of the petroleum resin manufacturing process according to the first comparative example.
5 is a configuration diagram showing the flow of the mixture in the polymerization solvent purification apparatus of the petroleum resin manufacturing process according to the second comparative example.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings so that those skilled in the art can easily carry out the present invention. The present invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. In order to clearly illustrate the present invention, parts not related to the description are omitted, and the same or similar components are denoted by the same reference numerals throughout the specification.

FIG. 3 is a view illustrating a polymerization solvent purification apparatus for a petroleum resin production process using a separation wall type distillation tower according to an embodiment of the present invention. Referring to FIG. 3, an embodiment provides a method of purifying a polymerization solvent comprising a step of introducing a mixture of a polymerization solvent used in a petroleum resin manufacturing process into a separating wall-type distillation column and subjecting to fractional distillation.

The separating wall type distillation tower used in one embodiment includes a main tower 100 having a separation wall 10, a condenser 200 and a reboiler 300. The main tower 100 has a top zone 20, A zone 30, a feed zone 40, and an outlet zone 50.

The feed zone 40 can be further divided into an upper feed zone 40a and a lower feed zone 40b and the outflow zone 50 can be divided into an upper outflow zone 50a and a lower outflow zone 50b .

The top zone 20 refers to the upper area of the separation wall 10 and the upper area of the main tower 100 without the separation wall 10. The bottom section 30 is the lower section of the separating wall 10 and the lower section of the tower 100 without the separating wall 10.

The supply zone 40 is a region where one side of the main tower 100 is partitioned by the separation wall 10 and is a region of the mixture A containing a polymerization solvent (for example, xylene) It is the area where the flow enters.

The upper supply region 40a is an upper region of the supply region 40 and is a sub region located above the flow of the mixture A supplied to the main tower 100. [ The lower supply zone 40b is a lower region of the supply zone 40 and is a sub region located below the flow of the mixture A supplied to the main tower 100. [

The outflow zone 50 is a region where one side of the main tower 100 is partitioned by the separation wall 10 and the flow of the low boiling point component C containing purified polymerization solvent of high purity (for example, xylene) Area.

The upper outlet area 50a is an upper area of the outlet area 50 and is a sub area located above the flow of the low boiling point component C discharged from the main tower 100. [ The lower outflow area 50b is a lower area of the outflow area 50 and is a sub area located below the flow of the low boiling point component C discharged from the main tower 100. [

For convenience, the column in the main tower 100 is not shown, and the term " length " in the following refers to the length determined by the number of columns. It is also contemplated that one or more of the above embodiments may be used in one independent zone, for example, top zone 20, bottom zone 30, top feed zone 40a, bottom feed zone 40b, top runout zone 50a, ), The ends of the columns are located at regular intervals, and the intervals of the column ends in the regions that are distinguished from each other may be independently the same or different.

In the pylon (100) of the separating wall type distillation column, the mixture (A) of polymerization solvents used in the petroleum resin manufacturing process flows into the feed zone (40). More specifically, the mixture (A) containing a polymerization solvent (e.g., xylene) as a main component is fed to the middle region of the feed zone 40, that is, the feed middle zone in which the upper feed zone 40a and the lower feed zone 40b contact (Fig. 3).

The low boiling point component C is separated from the upper portion of the separation wall 10 and the high boiling point component D is separated from the lower portion of the separation wall 10. The middle boiling point component (B) is separated into the outflow zone (50). More specifically, the middle boiling point component B can flow out into the middle region of the outflow zone 50, i.e., the outflow middle end where the upper outflow zone 50a and the lower outflow zone 50b contact. The middle boiling point component (B) is characterized by being a polymerization solvent of high purity (for example, xylene).

The separating wall type distillation tower used in one embodiment further includes a condenser 200 and a reboiler 300. The condenser 200 is an apparatus for depriving and condensing the vaporization heat of a mixture containing a gaseous polymerization solvent, and the condenser used in the conventional chemical engineering apparatus can be used without limitation. The reboiler 300 is a device for vaporizing and vaporizing a mixture containing a polymerization solvent in a liquid state. The reboiler used in the conventional chemical engineering apparatus can be used without limitation.

Since the space divided by the separating wall 10 serves as a preliminary separator (3 in FIG. 2) in the pillar 100 of the separating wall type distillation column, the liquid composition becomes almost equal to the equilibrium distillation curve due to the separation of the high boiling component and the low boiling component And the remixing effect is suppressed, thereby improving the thermodynamic efficiency for separation.

The upper feed zone 40a and the lower feed zone 40b play a similar role as the preliminary separator of the conventional process (3 in Fig. 2). That is, the supply zone 40 including the upper supply zone 40a and the lower supply zone 40b may be referred to as a kind of pre-separation zone. The mixture (A) containing the polymerization solvent flowing into the preliminary separation region is largely divided into the low boiling point component and the high boiling point component. A portion of the low boiling point component and the high boiling point component separated in the preliminary separation region flows into the top region 20 and the bottom region 30 and part of them flows into the top flow region 50a and the bottom flow region 50b again, Distillation.

The upper outlet region 50a and the lower outlet region 50b serve as the main separator (4 in FIG. 3) of the conventional process. That is, the outflow zone 50 including the upper outflow zone 50a and the lower outflow zone 50b may be referred to as a main separation zone. In the upper portion of the separation wall 10 of the main separation region, mainly the low boiling point component and the middle boiling point component are separated, and in the lower portion, mainly the high boiling point component and the high boiling point component are separated.

The low boiling point component is separated into the low boiling point component C after passing through the top portion 20 and the condenser 200 of the main tower 100 and partly separated into the top portion 20 ). The separating wall type distillation column of one embodiment may further include a condenser drum 400. The condenser drum 400 is a device for giving a buffer for stable reflux supply.

The high boiling point component is separated into a high boiling point component D after passing through the bottom portion 30 and the reboiler 300 of the main tower 100 and the remaining portion is separated into the high boiling point component D by the vapor flow rate VB, Is refluxed to the zone (30).

In a separating wall type distillation column of one embodiment, the factors affecting the purity and energy efficiency of the polymerization solvent (e.g., xylene) flowing out to the middle boiling point component (B) are very diverse. For example, the total column number of the main tower 100, the top zone 20, the top feed zone 40a, the top flow zone 50a, the bottom feed zone 40b, the bottom flow zone 50b, The length of the separation wall 10, the amount of reflux in the condenser 200, the amount of heat supplied in the reboiler 300, the vapor split ratio, (Xylene), and the energy consumption of the distillation tower. Therefore, by adjusting these parameters, it is possible to control the concentration of the polymerization solvent , Xylene) is not easy to refine.

According to an embodiment, there is provided a method for purifying a polymerization solvent in a petroleum resin manufacturing process using a separating wall type distillation column capable of purifying a polymerization solvent (for example, xylene) at a high purity of 90% or more at a low energy consumption rate .

For example, the mixture (A) comprising the polymerization solvent fed to the feed zone 40 may be selected from the group consisting of xylene (boiling point 138.5 캜), toluene (boiling point 110.6 캜), cyclohexane (boiling point 80.7 캜) Lt; 0 > C). The polymerization solvent may include an unreacted material after the polymerization reaction, a polymer generated during the reaction, an inactive material, and the like.

As an example, the mixture (A) comprising the polymerization solvent supplied to the feed zone 40 is based on xylene, and has a xylene content of 60 wt% or more based on the weight of the total mixture.

When the polymerization solvent containing xylene is purified using a separate wall-type distillation column, the polymerization solvent may contain a first range weight percentage, for example, 80 weight% or more, or 85 weight% or more, or 90 weight% The purified xylene is separated and flows out through the outflow zone 50. In this case, when only the high-boiling-point component is to be separated from the bottom portion 30, the temperature of the bottom portion 30 must be 200 ° C or higher. At such a temperature, the polymerization reaction may occur. Therefore, it is important to maintain the temperature of the bottom portion 30 at 190 DEG C or lower and 170 DEG C or higher in order to prevent unnecessary polymerization reaction in the bottom portion zone 30 while purifying xylene with high efficiency. When the temperature of the bottom zone 30 is below 190 ° C, the purified high boiling point materials may have a second range weight percentage lower than the first range, for example, about 10-20% by weight To the bottom section 30.

On the other hand, when the amount of xylene which is separated from the intermediate boiling point and flows out through the outflow middle stage is 10,000 to 12,000 kg / hr, the pressure of the outlet middle stage is 0.12 to 0.18 barg, the temperature of the outlet middle stage is 142 to 144 Lt; / RTI >

At this time, the number of stages of the top zone 20 may be 1 to 20 stages, or 5 to 15 stages, preferably 7 to 12 stages. And the number of stages of the bottom zone 30 can be from 1 to 15, or from 5 to 10, and preferably from 7 to 9. The number of stages of separating walls 10 may be independently from 1 to 30, or from 1 to 25, and preferably from 1 to 20, singlets, . At this time, the number of stages of the separation wall 10 should be 60% or less of the total number of stages of the main tower 100.

When the number of stages of the separating wall 10 exceeds 60% of the total number of stages of the main tower 100, the liquid / vapor phase and medium / intermediate boiling point components of the low boiling / It may be difficult to produce the column.

The vapor split ratio of the gaseous stream in the feed zone 40 and the outlet zone 50 in the main tower 100 is in the range of 40:60 to 60:40, preferably 50:50 And the liquid split ratio of the liquid stream in the feed zone 40 and the outflow zone 50 is operable in the range of 40:60 to 60:40.

There may be a problem that the separation efficiency is lowered in the supply zone 40 and the outflow zone 50 when the gas phase split ratio and liquid phase split ratio are out of the above range.

The number of stages of the column, the length of the separating wall 1, the condenser 200 and the reboiler 300, and the gas phase split ratio and the split split ratio are collectively referred to as the refining purity of the polymerization solvent (for example, xylene) , These parameters are adjusted so that the polymerization solvent (for example, xylene) can be purified at a high purity while consuming the lowest energy.

According to the polymerization solvent purification method using the separating wall type distillation column of the present invention as described above, the purity of the polymerization solvent can be purified to a high purity of 90% or more or 95% or more.

A partition wall column (DWC) was designed to verify the performance of the polymerization solvent purification apparatus in the petroleum resin manufacturing process according to one embodiment, and was simulated using a usable chemical process simulator (eg, ASPEN). The DWC is designed so that the composition of the required product is obtained in comparison with the current operating conditions. In the comparative example, two conventional distillation columns without separation walls were used.

4 is a configuration diagram showing the flow of the mixture in the polymerization solvent purification apparatus of the petroleum resin manufacturing process according to the first comparative example. 4, in the first comparative example, the low boiling point component 12 and the primary high boiling point component 13 are first separated from the mixture 11 in the first distillation column 1 and the primary high boiling point component 13 is separated from the mixture 11, (14) and the high boiling point component (15) in the second distillation column (2).

5 is a configuration diagram showing the flow of the mixture in the polymerization solvent purification apparatus of the petroleum resin manufacturing process according to the second comparative example. 5, in the second comparative example, the high boiling point component 15 and the primary low boiling point component 13 are first separated from the mixture 11 in the first distillation column 1, and the high boiling point component 15 and the low- And to separate the low boiling point component (12) and the middle boiling point component (14) from the second distillation column (2).

As shown in Fig. 3, the embodiment uses one pylon 100 with a separation wall 10. Referring to Figure 3, in the pylon 100 of an embodiment, a mixture (A; A1, A2) comprising a polymerization solvent (e.g., xylene) is introduced into the feed midrange of the feed zone 40, The low boiling point component C and the middle boiling point component are separated from each other by the separating wall 20 and the middle boiling point component B and the high boiling point component D are separated from each other in the head bottom section 30, The low boiling point component C is separated and the high boiling point material D is separated from the lower part of the separation wall 10 and the middle boiling point component B flows out to the outflow middle end. The middle boiling point component (B) is a polymerization solvent of high purity (e.g., xylene).

The examples and the first and first comparative examples had column numbers as shown in Table 1.

Item Column number Example The top zone (20) 9 In the bottom zone 30, 7 The separation wall (10) 18 The supply intermediate stage 40 (liquid phase) 11 Supply intermediate stage 40 (meteorological) 16 The outflow mid- 12 Comparative Examples 1 and 2 The first distillation tower (1) 20 The second distillation column (2) 34

(A1, A2) which is a polymerization solvent having a xylene content of not less than 60% by weight based on the weight of the entire mixture in the first and second comparative examples and the examples so as to have the number of columns as shown in Table 1 The purification process was simulated.

The results of the refining process simulations of the first and second comparative examples and the examples were as shown in Tables 2 and 3 below.

division unit A1 A2 C B D Comparative Example 1 Condition Temperature ℃ 125.0 202.2 60.0 141.2 181.2 pressure Barg 3.0 1.0 0.1 0.1 0.2 flux Kg / hr 4972 11960.4 900 11022.2 5010.2 Xylene composition wt% 38.6 74.8 10.7 90.0 16.8 Comparative Example 2 Condition Temperature ℃ 125.0 202.2 60.0 144.6 179.4 pressure Barg 3.0 1.0 0.1 0.2 0.15 flux Kg / hr 4972 11960.4 900 11022.2 5010.2 Xylene composition wt% 38.6 74.8 10.7 90.0 16.8 Example Condition Temperature ℃ 125.0 202.2 60.0 143.4 181.6 pressure barg 3.0 1.0 0.1 0.16 0.21 flux Kg / hr 4972 11960.4 900 11022.2 5010.2 Xylene composition wt% 38.6 74.8 10.7 90.0 16.8

Energy Consumption [Gcal / hr] Example Rebid (300) 0.71 The condenser (200) 1.85 Comparative Example 1 Total Rebid 2.03 Condenser 3.18 The first distillation tower (1) Rebid 0.73 Condenser 1.91 The second distillation column (2) Rebid 1.3 Condenser 1.27 Reduction rate Rebid 65.0% Condenser 41.8% Comparative Example 2 Total Rebid 1.57 Condenser 2.71 The first distillation tower (1) Rebid 0.94 Condenser 2.18 The second distillation column (2) Rebid 0.63 Condenser 0.53 Reduction rate Rebid 54.8% Condenser 31.7%

Since mixtures of various materials (A1 and A2) are used in the process of the present invention, only the composition of the xylene mixture (B) is described in Table 2 below, and the flow of the mixture and the low, middle, and high boiling point components (C, D) 4, 5 and 3. Depending on the kind of the polymerization solvent, the results of the above embodiments may be varied.

As has been described in the embodiment, when the column 100 having a separation wall type distillation column, that is, the separation wall 10, is used, the xylene having a purity of 90% or more is more efficiently .

As compared with the first and second comparative example distillation towers 1 and 2 and the four heat exchangers (two condensers 2 and two reboilers 2) in terms of investment cost, the first tower 100 of the embodiment and the heat exchanger (the condenser and the re- 2) are much cheaper, and energy consumption is greatly reduced.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the invention is not limited to the disclosed exemplary embodiments, but, on the contrary, And it goes without saying that the invention belongs to the scope of the invention.

10: separating wall 20: top zone
30: head bottom section 40: supply section
40a: upper feed zone 40b: lower feed zone
50: outflow zone 50a: upper outflow zone
50b: lower outflow zone 100: pylon
200: condenser 300: re-boiling
A: mixture C: low boiling point component
D: high boiling point component B: middle boiling point component

Claims (13)

A method for purifying a polymerization solvent comprising a step of introducing a mixture containing a polymerization solvent used in a petroleum resin manufacturing process into a separating wall type distillation column and subjecting to fractional distillation,
The separation wall-
A main tower having a separation wall and divided into a top zone, a feed zone, an outflow zone, and a bottom zone; Condenser; And re-
The mixture of polymerization solvents is introduced into the feed zone of the main tower,
The purified polymerization solvent flows into the effluent zone of the main tower,
With respect to the weight of total xylene contained in the mixture,
A first boiling point component comprising purified xylene in a first range of weight percent flows out to the outflow middle end of the outflow zone,
Wherein a high boiling point component containing purified xylene at a second range weight percent lower than the first range flows out to a lower outlet end of the outlet zone,
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).
The method according to claim 1,
In the mixture comprising the polymerization solvent, the xylene content is at least 60% by weight, based on the weight of the total mixture,
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).
The method according to claim 1,
Wherein the first range weight percent is at least 80 wt%
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).
The method according to claim 1,
Wherein the second range wt% is 10 to 20 wt%
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).
The method according to claim 1,
Maintaining the temperature of the bottom zone between < RTI ID = 0.0 > 170 C < / RTI &
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).
The method according to claim 1,
And flows out through the outflow middle stage
When the amount of xylene is 10,000 to 12,000 kg / hr,
Wherein the pressure at the outgoing intermediate stage is between 0.12 and 0.18 barg,
Lt; RTI ID = 0.0 > 144 C, < / RTI >
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).
The method according to claim 1,
The mixture comprising the polymerization solvent
Xylene, toluene, cyclohexane, and ethylbenzene.
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).
The method according to claim 1,
Wherein the number of stages of the top zone is from 1 stage to 20 stages, or from 5 stages to 15 stages,
Wherein the number of stages of the bottom zone is from 1 to 15, or from 5 to 10,
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).
9. The method of claim 8,
The number of divisions of the separating wall
The number of the stages of the top zone and the number of stages of the bottom zone may be the same or different from each other,
Or less than 60% of the total number of stages of the main tower,
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).
The method according to claim 1,
The number of stages of the top zone is from 7 to 12,
The number of stages of the bottom zone is 7 to 9 stages,
Wherein the number of the separation walls is one to twenty,
Or less than 60% of the total number of stages of the main tower,
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).
The method according to claim 1,
In the feed tower and outflow zone in the main tower, the vapor split ratio of the gaseous stream is 40:60 to 60:40,
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).
The method according to claim 1,
In the feed tower and outflow zone in the main tower, the liquid split ratio of the liquid stream is 40:60 to 60:40,
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).
The method according to claim 1,
Wherein the purity of the polymerization solvent is at least 90%
(Method for Purifying Polymeric Solvent in Petroleum Resin Manufacturing Process Using Separated Wall Type Distillation Column).

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