KR102668568B1 - Apparatus for producing polyester and method for producing polyester - Google Patents

Abstract

The present invention relates to polyester production equipment and methods for producing polyester. Specifically, according to one embodiment of the present invention, an ester reactor for esterifying a given raw material; a condensation polymerization reactor that performs a condensation polymerization reaction on the reactants produced in the ester reactor to produce a polyester compound and by-products in at least one of gaseous state and liquid state; A receiver unit including a receiver tank that collects some of the incoming by-products; And a receiver including a first flow pipe that guides the by-product to the receiver tank and a second flow pipe that guides the flow of the by-product upward so that another part of the by-product flowing into the receiver tank is discharged from the receiver tank. A polyester manufacturing apparatus comprising a pipe may be provided.

Description

Polyester manufacturing apparatus and method for manufacturing polyester {APPARATUS FOR PRODUCING POLYESTER AND METHOD FOR PRODUCING POLYESTER}

The present invention relates to an apparatus for producing polyester and a method for producing polyester.

Polyester is a material with excellent mechanical strength, heat resistance, durability, and chemical resistance, and is used in household goods, biodegradable products, and parts for various machines. Such polyester can be produced by subjecting certain raw materials to an esterification reaction and subjecting the reactant produced by the esterification reaction to a condensation polymerization reaction. for example,

The polyester production apparatus may be equipped with an esterification reactor necessary for the production of polyester and a condensation polymerization reactor that receives the reactant generated in the esterification reactor and performs a condensation polymerization reaction. For example, in the esterification reactor, an esterification reaction between an aromatic dicarboxylic acid and an aliphatic dihydroxy compound and an esterification reaction between an aliphatic dicarboxylic acid and an aliphatic dihydroxy compound may proceed.

In the condensation polymerization reactor, the condensation polymerization reaction of the esterified reactant may proceed. In order to increase the degree of polymerization of the condensation polymerization reaction in such a condensation polymerization reactor, unreacted products and reaction by-products generated in the condensation polymerization reactor must be removed, and the interior of the condensation polymerization reactor must be maintained in a vacuum state. In order to remove these by-products and maintain the interior of the polycondensation reactor in a vacuum state, the polyester manufacturing apparatus is further equipped with a vacuum pump and one or more pipes provided between the polycondensation reactor and the vacuum pump.

Conventional polyester manufacturing equipment had a problem in that by-products solidified inside the pipe while flowing along the vacuum pipe in either a gaseous state or a liquid state. For example, if by-products solidify and accumulate in the vacuum pipe, there is a problem in that it becomes difficult to maintain the target vacuum level inside the condensation polymerization reactor. Additionally, there is a problem that if solidified by-products flow into the vacuum pump, the vacuum pump may be damaged.

Accordingly, the need for polyester manufacturing equipment that prevents by-products from solidifying and accumulating in one or more pipes and from entering the vacuum pump is increasing.

One embodiment of the present invention was invented with the above background in mind, and aims to provide a polyester manufacturing apparatus that prevents by-products from solidifying and accumulating in one or more pipes.

In addition, it is intended to provide a polyester manufacturing device that prevents damage to the vacuum pump by preventing by-products from entering the vacuum pump.

According to one embodiment of the present invention, a receiver unit including a receiver tank that collects some of the by-products flowing from the polyester condensation polymerization reactor; And a receiver pipe including a first flow pipe that guides the by-products to the receiver tank and a second flow pipe that guides the by-products so that some of the by-products flowing into the receiver tank are discharged from the receiver tank, The receiver unit includes a heating jacket for heating the first flow pipe to prevent the by-product flowing through the first flow pipe in the receiver tank from solidifying; And a polyester manufacturing apparatus including a cooling unit that cools the by-product discharged from the receiver tank through the first flow pipe.

In addition, the cooling unit includes a cooling coil disposed inside the receiver tank, and in the vertical direction, the cooling coil is disposed between the lower end of the first flow pipe and the lower end of the second flow pipe. A device may be provided.

In addition, a polyester manufacturing apparatus may be provided in which the cooling coil is supplied with a refrigerant at a temperature of 5°C to 10°C.

In addition, the cooling unit may surround an outer peripheral surface of the receiver tank and further includes a cooling jacket disposed on the upper portion of the receiver tank to cool the upper portion of the receiver tank.

Additionally, a polyester manufacturing device may be provided in which a refrigerant with a temperature of 5°C to 10°C flows inside the cooling jacket.

Additionally, a vacuum pump for removing air from the receiver tank so that the receiver tank is placed in a vacuum state; And a trap communicating with the second flow pipe and the vacuum pump, and further comprising a trap for cooling the by-product passing through the second flow pipe, may be provided.

Additionally, a polyester manufacturing apparatus may be provided in which the temperature of the trap is -70°C to -30°C.

In addition, the heating jacket is disposed to surround the outer peripheral surface of a portion of the first flow pipe, a portion of the first fluid pipe is disposed within the receiver tank, and the inside of the heating jacket has a temperature of 220°C to 250°C. A polyester manufacturing apparatus in which the fruit flows may be provided.

Additionally, a polyester manufacturing apparatus may be provided in which the temperature of another part of the first flow pipe is 100°C to 170°C.

In addition, the other part of the first flow pipe is disposed above any part of the first flow pipe, and extends between the condensation polymerization reactor and any part of the first flow pipe. A polyester manufacturing apparatus is provided. It can be.

In addition, a by-product introduction step in which by-products generated during the condensation polymerization reaction of the reactants generated in the esterification reaction step are introduced into the receiver tank through the first flow pipe, and the by-products flowing into the receiver tank are collected in the receiver tank. A by-product collection step, and a by-product discharge step in which the remaining by-products collected in the by-product collection step are discharged from the receiver tank through a second flow pipe, and the by-product collection step is to collect the by-products flowing into the receiver tank. A method of producing polyester, comprising a heating step of heating a portion of the first flow pipe to prevent solidification, and a cooling step of cooling the by-product flowing through the first flow pipe through a cooling unit. This can be provided.

In addition, the cooling step includes a coil cooling step of cooling the by-product through a cooling coil disposed inside the receiver tank, and in the vertical direction, the cooling coil is connected to the lower end of the first flow pipe and the first flow pipe. A method of manufacturing polyester disposed between the lower ends of two flow pipes may be provided.

In addition, the cooling step further includes a jacket cooling step of cooling the by-product through a cooling jacket disposed on the upper part of the receiver tank to cool the upper part of the receiver tank, and the cooling jacket is located on the outer peripheral surface of the receiver tank. Surrounding, a method for producing polyester can be provided.

In addition, manufacturing polyester further includes an air removal step of removing air in the receiver tank so that the receiver tank is placed in a vacuum state, and a trap step of cooling and removing the by-product that has passed through the second flow pipe. A method may be provided.

Additionally, a method for producing polyester may be provided in which a refrigerant with a temperature of 5°C to 10°C flows in the cooling unit.

The polyester manufacturing apparatus according to an embodiment of the present invention has the effect of preventing by-products from solidifying and accumulating in the pipe and increasing the efficiency of the condensation polymerization reaction by maintaining the vacuum level required for the condensation polymerization reactor by the vacuum pump.

In addition, the polyester manufacturing device has the effect of preventing damage to the vacuum pump by preventing by-products from entering the vacuum pump.

1 is a conceptual diagram of a polyester manufacturing apparatus according to an embodiment of the present invention.
Figure 2 is a longitudinal cross-sectional view of the receiver unit taken along line A-A' of Figure 1.
Figure 3 is a longitudinal cross-sectional view showing the flow of by-products flowing in the receiver unit and receiver pipe.
Figure 4 is a block diagram conceptually showing a polyester manufacturing apparatus according to an embodiment of the present invention.
Figure 5 is a flow chart schematically showing a method for producing polyester according to an embodiment of the present invention.
Figure 6 is a flow chart schematically showing the by-product removal steps according to an embodiment of the present invention.

Hereinafter, specific embodiments for implementing the technical idea of the present invention will be described in detail with reference to the drawings.

In addition, when describing the present invention, if it is determined that a detailed description of a related known configuration or function may obscure the gist of the present invention, the detailed description will be omitted.

Additionally, when a component is mentioned as being 'connected', 'flowing', or 'supplied' to another component, it is understood that it may be directly connected, flowing, or supplied to the other component, but that other components may exist in between. It should be.

The terms used in this specification are merely used to describe specific embodiments and are not intended to limit the invention. Singular expressions include plural expressions unless the context clearly dictates otherwise.

Additionally, terms including ordinal numbers, such as first, second, etc., may be used to describe various components, but the components are not limited by these terms. These terms are used only to distinguish one component from another.

As used in the specification, the meaning of "comprising" is to specify a specific characteristic, area, integer, step, operation, element, and/or component, and to specify another specific property, area, integer, step, operation, element, component, and/or group. It does not exclude the existence or addition of .

In addition, it should be noted in advance that in this specification, expressions such as upper part, lower part, upper surface, etc. are explained based on the illustrations in the drawings, and may be expressed differently if the direction of the object in question is changed.

Hereinafter, the specific configuration of the polyester manufacturing apparatus 1 according to an embodiment of the present invention will be described with reference to the drawings.

Referring to FIG. 1, the polyester production apparatus 1 according to an embodiment of the present invention produces polyester by esterifying a given raw material and performing a condensation polymerization reaction of the reactant produced by the esterification reaction. You can. Predetermined raw materials may include aromatic dicarboxylic acid, aliphatic dicarboxylic acid, and aliphatic dihydroxy compound. This polyester manufacturing device (1) includes a slurry tank (100), a reactor (200), a receiver unit (300), a trap (400), a vacuum pump (500), a pipe module (600), a refrigerant supply unit (700), and a refrigerant supply unit (700). It may include a supply unit 800 and a controller 900.

The slurry tank 100 can produce a first slurry containing an aromatic dicarboxylic acid and an aliphatic dihydroxy compound and a second slurry containing an aliphatic dicarboxylic acid and an aliphatic dihydroxy compound. For example, the temperature at which the first slurry is produced in the slurry tank 100 may be 30°C to 100°C. Additionally, the temperature at which the second slurry is produced in the slurry tank 100 may be, for example, 30°C to 70°C. The first slurry and second slurry produced in this slurry tank 100 may be supplied to the reactor 200.

The reactor 200 may include an ester reactor 210 and a condensation polymerization reactor 220. The ester reactor 210 may receive the first slurry and the second slurry from the slurry tank 100. This ester reactor 210 can esterify the first slurry and the second slurry. For example, the ester reactor 210 may esterify the first slurry at a temperature of 200°C to 230°C. Additionally, as an example, the ester reactor 210 may perform an esterification reaction of the second slurry at a temperature of 200°C to 220°C.

This ester reactor 210 can esterify the first slurry and then esterify the second slurry. However, the spirit of the present invention is not limited thereto, and the ester reactor 210 performs an esterification reaction on the first slurry after esterifying the second slurry, or performs an esterification reaction on the first slurry and the second slurry simultaneously. You can also do it.

Additionally, one or more of a polyhydric alcohol and a polyhydric acid branching agent may be added to the ester reactor 210. As one or more of these polyhydric alcohols and polyhydric acid branching agents are added, the reaction rate of the esterification reaction of the first slurry and the second slurry is improved.

The condensation polymerization reactor 220 can receive the ester reaction product generated in the ester reactor 210 and perform a condensation polymerization reaction. This condensation polymerization reactor 220 can produce polyester compounds and by-products by performing a condensation polymerization reaction on ester reactants. By-products refer to reaction by-products produced through a condensation polymerization reaction, and these by-products may be in one or more of a gaseous state and a liquid state.

The interior of the condensation polymerization reactor 220 may be placed in a vacuum state by the vacuum pump 500 while the condensation polymerization reaction is performed. The vacuum state can be understood in a comprehensive sense that includes not only a state of extremely low pressure where air is completely absent, but also a state of negative pressure lower than atmospheric pressure. For example, the vacuum state in this specification can be understood as a concept that includes all states with a pressure of less than 760 torr.

This condensation polymerization reactor 220 can perform a first condensation polymerization reaction of the ester reactant in a first vacuum condition. For example, the first vacuum state may be defined as a state in which the pressure inside the condensation polymerization reactor 220 is 760 torr to 1 torr. For example, this first condensation polymerization reaction may be performed for 30 to 40 minutes. Additionally, the temperature at which the first condensation polymerization reaction is performed may be, for example, 220°C to 240°C.

Additionally, the condensation polymerization reactor 220 may subject the first condensation polymerization reactant to a second condensation polymerization reaction in a second vacuum state. For example, the second vacuum state may be defined as a state in which the pressure inside the condensation polymerization reactor 220 is 0 to 1 torr. For example, this second condensation polymerization reaction may be performed for 120 to 240 minutes. Additionally, the temperature at which the second condensation polymerization reaction is performed may be, for example, 230°C to 250°C.

Referring further to FIGS. 2 and 3, the receiver unit 300 may collect by-products generated in the condensation polymerization reactor 220. This receiver unit 300 may include a receiver tank 310, a cooling unit 320, and a heating jacket 330. The receiver tank 310 can collect by-products. A receiver chamber 310a may be formed in this receiver tank 310. This receiver chamber 310a may include a flow space for gaseous and liquid state by-products to flow and a stacking space where solidified by-products are stacked. Additionally, the stacking space may be placed lower than the flow space.

The receiver tank 310 may include an inlet 311, an outlet 312, a drain 313, and a by-product stack 314. The inlet 311 may be connected to the first flow pipe 640, which will be described later. The outlet 312 may be connected to a second flow pipe 650, which will be described later. The inlet 311 and outlet 312 may be disposed above the receiver chamber 310a.

The drain unit 313 can selectively discharge by-products collected in the collection space to the outside of the receiver unit 300. For example, the drain unit 313 is provided with an on-off valve, and the collected by-products can be selectively discharged to the outside of the receiver unit 300 by opening and closing the on-off valve. This drain portion 313 may be disposed lower than the byproduct stack portion 314.

The by-product stacking unit 314 may stack solidified by-products. This by-product stacked portion 314 can form a stacked space. This by-product stack 314 may be disposed lower than the first flow pipe 640. For example, this by-product stack 314 may have a hopper shape whose width in the horizontal direction narrows downward.

The cooling unit 320 may solidify by-products in one or more of gaseous state and liquid state. For example, the cooling unit 320 may cool the by-product flowing upward through the first flow pipe 640. Refrigerant may flow inside the cooling unit 320. This cooling unit 320 can receive refrigerant from the refrigerant supply unit 700. Additionally, the cooling unit 320 may be disposed lower than the second flow pipe 650. This cooling unit 320 may include a cooling jacket 321 and a cooling coil 322.

The cooling jacket 321 may be disposed outside the receiver tank 310. This cooling jacket 321 may be arranged to surround the upper outer peripheral surface of the receiver tank 310. Additionally, refrigerant (C) may flow inside the cooling jacket 321. For example, the temperature of the refrigerant flowing inside the cooling jacket 321 may be 5°C to 10°C. The top of the cooling jacket 321 may be disposed above the top of the cooling coil 322. Additionally, in the vertical direction, the lower end of the cooling jacket 321 may be disposed between the upper and lower ends of the cooling coil 322.

The cooling coil 322 may be a coil-shaped heat exchange pipe through which the refrigerant (C) supplied from the cooling jacket 321 flows. This cooling coil 322 can cool the by-product discharged from the receiver tank 310. Additionally, the cooling coil 322 may be disposed between the bottom of the heating jacket 330 and the top of the receiver tank 310 in the vertical direction. This cooling coil 322 may be placed inside the receiver tank 310. This cooling coil 322 may extend in the vertical direction.

The heating jacket 330 can heat the by-product flowing in the first flow pipe 631. For example, the heating jacket 330 can heat the by-product and prevent the by-product from solidifying. This heating jacket 330 can heat the lower part of the first flow pipe 631. For example, the heating jacket 330 may be arranged to surround the lower outer peripheral surface of the first flow pipe 631. The lower part of the first flow pipe 631 may be referred to as a ‘warmth pipe’ in this specification.

This heating jacket 330 may extend along the vertical direction. This heating jacket 330 may be placed inside the receiver tank 310. However, the spirit of the present invention is not necessarily limited to this, and the upper part of the heating jacket 330 is disposed outside the receiver tank 310, and the central and lower parts of the heating jacket 330 are located inside the receiver tank 310. can be placed in The fruit H may flow inside the heating jacket 330. For example, the temperature of the fruit H may be 220°C to 250°C. This heating jacket 330 can receive fruit H from the fruit supply unit 800. The lower end of the heating jacket 330 may be disposed lower than the cooling coil 322.

The trap 400 can collect remaining by-products that are not captured in the receiver unit 300. For example, the trap 400 can collect the remaining by-products by cooling them. For example, the temperature of the trap 400 may be -70°C to -30°C. This trap 400 may be placed between the vacuum pump 500 and the receiver unit 300. For example, the trap 400 may connect the vacuum pump 500 and the receiver unit 300. This trap 400 can be placed in a vacuum state by the vacuum pump 500.

The vacuum pump 500 can maintain the polycondensation reactor 220, receiver tank 310, and trap 400 in a vacuum state. For example, the vacuum pump 500 can suck air from the polycondensation reactor 220, the receiver tank 310, and the trap 400 and discharge it to the outside.

The pipe module 600 may include a plurality of pipes. These plural pipes may communicate with each other. Additionally, each of the plurality of pipes may be independently heated by a predetermined heating device (not shown). For example, the temperatures at which a plurality of pipes are heated may be the same or different. These plural pipes include an inlet pipe 610, a first connection pipe 620, a second connection pipe 630, a first flow pipe 640, a second flow pipe 650, and an discharge pipe 660. can do.

The inlet pipe 610 can guide the flow of a certain raw material flowing into the slurry tank 100. The inlet pipe 610 may guide the flow of one or more of the first slurry and the second slurry. One end of this inlet pipe 610 may be connected to the slurry tank 100.

The first connection pipe 620 may guide the slurry discharged from the slurry tank 100 to the ester reactor 210. One end of the first connection pipe 620 may be connected to the slurry tank 100, and the other end may be connected to the ester reactor 210. For example, the temperature of the first connection pipe 620 may be 30°C to 100°C.

The second connection pipe 630 may guide the flow of the ester reactant discharged from the ester reactor 210 to the condensation polymerization reactor 220. One end of the second connection pipe 630 may be connected to the ester reactor 210, and the other end may be connected to the condensation polymerization reactor 220. For example, the temperature of the second connection pipe 630 may be 210°C to 240°C.

The first flow pipe 640 may guide the by-product discharged from the polycondensation reactor 220 to the receiver tank 310. One end of the first flow pipe 640 may be connected to the polycondensation reactor 220, and the other end may be placed inside the receiver tank 310. This first flow pipe 640 may be connected to the inlet 311. For example, a part of the first flow pipe 640 may be disposed inside the receiver tank 310, and another part may be connected to the inlet 311. A part of the first flow pipe 640 may be referred to as the 'lower part of the first flow pipe 640,' and another part of the first flow pipe 640 may be referred to as the 'upper part of the first flow pipe 640.' It can be named '. The lower part of the first flow pipe 640 may be heated by the heating jacket 330.

The lower part of the first flow pipe 640 may extend in the vertical direction. Additionally, at least a portion of the lower part of the first flow pipe 640 may be disposed inside the receiver tank 310. For example, the height of the upper end of the lower part of the first flow pipe 640 may be lower than or equal to the height of the upper end of the inlet 311. As another example, the height of the upper end of the lower part of the first flow pipe 640 may be higher than the height of the upper end of the inlet 311. Additionally, the upper part of the first flow pipe 640 may be connected to the condensation polymerization reactor 220. For example, the upper part of the first flow pipe 640 may be formed integrally with the lower part of the first flow pipe 640. Additionally, the temperature of the first flow pipe 640 may be, for example, 100°C to 170°C. Additionally, in the vertical direction, the lower end of the first flow pipe 640 may be disposed between the cooling coil 322 and the by-product stack 314. By-products that pass through the first flow pipe 640 may flow upward.

The second flow pipe 650 may guide the flow of the by-product cooled in the cooling unit 320 upward. One end of the second flow pipe 650 may be connected to the outlet portion 312, and the other end may be connected to the trap 400. The second flow pipe 650 may guide the remaining by-products discharged from the receiver tank 310 to the trap 400. Such

The discharge pipe 660 may guide the air discharged from the trap 400 to the vacuum pump 500. One end of the discharge pipe 660 may be connected to the trap 400, and the other end may be connected to the vacuum pump 500.

The refrigerant supply unit 700 may supply refrigerant (C) to the cooling unit 320. For example, the refrigerant supply unit 700 may supply the refrigerant (C) condensed in the reactor 200 to the cooling unit 320. This refrigerant supply unit 700 can supply refrigerant (C), whose temperature has been lowered by condensing in the reactor 200, to the cooling jacket 321 and the cooling coil 322.

The fruit supply unit 800 may supply fruit H to the condensation polymerization reactor 220 and the heating jacket 330. For example, the fruit supply unit 800 may share the fruit (H) supplied to the condensation polymerization reactor 220 with the heating jacket 330.

In this way, the refrigerant supply unit 700 shares the refrigerant (C) used in the reactor 200 with the cooling unit 320, and the heat supply unit 800 heats the heat (H) used in the condensation polymerization reactor 200. By sharing it with the jacket 330, the structure of the facility can be simplified and the energy used for heating and cooling by-products can be minimized.

Referring further to FIG. 4, the controller 900 includes a slurry tank 100, a reactor 200, a receiver unit 300, a trap 400, a vacuum pump 500, a refrigerant supply unit 700, and a fruit supply unit 800. ) can be controlled. This controller 900 can control the temperatures of the slurry tank 100, reactor 200, trap 400, cooling unit 320, heating jacket 330, and pipe module 600.

The controller 900 may be implemented by an arithmetic device including a microprocessor, and since the implementation method is obvious to those skilled in the art, further detailed description will be omitted.

Hereinafter, the operation and effects of the polyester manufacturing apparatus 1 according to an embodiment of the present invention will be described.

A certain raw material may be introduced into the slurry tank 100 of the polyester manufacturing apparatus 1 through the inlet pipe 610. In this slurry tank 100, a first slurry and a second slurry may be produced. The first slurry and the second slurry may pass through the first connection pipe 620 and flow into the ester reactor 210. The ester reactor 210 may generate an ester reaction product by esterifying the first slurry and the second slurry. These ester reactants may pass through the second connection pipe 630 and flow into the condensation polymerization reactor 210.

This condensation polymerization reactor 210 can perform a condensation polymerization reaction of ester reactants to produce polyester and by-products. By-products in one or more of the gaseous state and the liquid state may pass through the first flow pipe 640 and flow into the receiver tank 310. While these by-products flow along the lower part of the first flow pipe 640, the by-products may be heated by the heating jacket 330.

By-products heated by the heating jacket 330 can be prevented from solidifying in the lower part of the first flow pipe 640. This heating jacket 330 has the effect of preventing the lower part of the first flow pipe 640 from being clogged due to solidification of by-products, thereby placing the interior of the polycondensation reactor 220 in a target vacuum state.

Additionally, the lower portion of the first flow pipe 640 extends in the vertical direction and at least a portion of it may be disposed inside the receiver tank 310. By-products that have passed through the first flow pipe 640 may flow upward from the bottom of the receiver chamber 310a together with air. While these by-products and air flow upward, they may pass through the cooling space surrounded by the cooling coil 322. Additionally, by-products and air can be cooled by the cooling jacket 321 while passing through the cooling space. In other words, by-products and air can be double cooled by the cooling jacket 321 and the cooling coil 322.

These cooled by-products may solidify and fall downward. By-products that fall downward may be stacked on the by-product stacking portion 314. Byproducts stacked on the byproduct stacking unit 314 may be discharged to the outside of the receiver unit 300 through the drain unit 313.

In this way, the polyester manufacturing device 1 has the effect of maximizing cooling of the by-product through the cooling jacket 321 and the cooling coil 322, thereby increasing the by-product removal rate.

Additionally, the remaining by-products remaining after passing through the cooling jacket 321 and the cooling coil 322 may pass through the second flow pipe 650 together with air and flow into the trap 400. The trap 400 can cool the remaining by-products introduced with air and solidify the remaining by-products that have not been solidified in the cooling unit 320. By-products are completely removed through this trap 400, so that only air can exist inside the trap 400. This air may pass through the discharge pipe 660 and flow into the vacuum pump 500. Air introduced into the vacuum pump 500 may be discharged to the outside. As the vacuum pump 500 discharges air to the outside, the polycondensation reactor 220, the first flow pipe 640, the receiver tank 310, the second flow pipe 650, the trap 400, and The discharge pipe 660 may be placed in a vacuum state.

In this way, the polyester manufacturing device 1 removes most of the by-products through the cooling jacket 321 and the cooling coil 322, and completely removes the remaining by-products through the trap 400, preventing the pipe module 600 from clogging. This has the effect of preventing any damage to the vacuum pump 500.

Hereinafter, with reference to FIGS. 5 and 6, a method (S10) for producing polyester according to an embodiment of the present invention will be described. In explaining the method (S10) for producing polyester, the differences compared to the polyester production apparatus (1) described above are mainly explained, and the same description and reference numerals refer to the above-described embodiments.

The method for producing polyester (S10) may include a slurry preparation step (S100), an esterification reaction step (S200), a condensation polymerization reaction step (S300), a by-product removal step (S400), and an air removal step (S500). there is.

In the slurry production step (S100), one or more of the first slurry and the second slurry may be produced. This slurry preparation step (S100) may include a first slurry preparation step and a second slurry preparation step. In the first slurry production step, an aromatic dicarboxylic acid and an aliphatic dihydroxy compound may be slurried to produce a first slurry. For example, this first slurry preparation step may be performed at a temperature of 30°C to 100°C. In the second slurry production step, an aliphatic dicarboxylic acid and an aliphatic dihydroxy compound may be slurried to produce a second slurry. For example, this second slurry preparation step may be performed at a temperature of 30°C to 70°C.

In the esterification reaction step (S200), the first slurry and the second slurry may be esterified to produce an ester reaction product. This ester reaction step (S200) may include a first ester reaction step and a second ester reaction step. In the first ester reaction step, for example, the first slurry may be esterified. As another example, in the first ester reaction step, an aromatic dicarboxylic acid and an aliphatic dihydroxy compound may be added simultaneously to esterify. For example, this first ester reaction step may be performed at a temperature of 200°C to 230°C.

In the second ester reaction step, for example, the second slurry may be esterified. As another example, in the second ester reaction step, an aliphatic dicarboxylic acid and an aliphatic dihydroxy compound may be added simultaneously to esterify. For example, this second ester reaction step may be performed at a temperature of 200°C to 220°C.

These first and second ester reaction steps may be performed sequentially or in reverse order, respectively. Furthermore, the first ester reaction step and the second ester reaction step may be performed simultaneously. Additionally, the temperature at which the ester reaction step (S200) is performed may be, for example, increased at a rate of 1°C/min to 3°C/min. In other words, the temperature may be gradually increased until it reaches the temperature at which the ester reaction step (S200) is performed.

In the condensation polymerization reaction step (S300), the ester reaction product may be condensation polymerized. In this condensation polymerization reaction step (S300), polyester and by-products may be produced. This condensation polymerization reaction step (S300) may include a pre-condensation reaction step and a polycondensation reaction step. In the precondensation reaction step, the ester reactant introduced into the condensation polymerization reactor may be stabilized for, for example, 10 to 20 minutes. In this precondensation reaction step, the stabilized ester reactant may be precondensed for a predetermined time. For example, in the precondensation reaction step, the ester reactant may be precondensed for 30 to 40 minutes. While this precondensation is in progress, the degree of vacuum inside the polycondensation reactor 210 may be gradually increased from 760 torr to 1 torr. For example, this precondensation reaction step may be performed at a temperature of 220°C to 240°C.

In the polycondensation reaction step, the pre-condensed condensation polymer may be polycondensed for, for example, 120 to 240 minutes. While polycondensation is in progress, the degree of vacuum inside the polycondensation reactor 220 may be gradually increased until the vacuum is less than 1 torr. For example, this polycondensation reaction step may be performed at a temperature of 230°C to 250°C. Once this polycondensation reaction step is completed, polyester with the molecular weight desired by the user can be produced.

Referring again to FIG. 6, in the by-product removal step (S400), the by-products generated in the condensation polymerization reaction step (S300) may be removed. This by-product removal step (S400) may include a by-product inflow step (S410), a by-product collection step (S420), a by-product outflow step (S430), and a trap step (S440).

In the by-product introduction step (S410), by-products in either a gaseous state or a liquid state and air may be introduced into the receiver chamber (310a). In the by-product collection step (S420), the by-products flowing into the receiver chamber 310a may be collected and stacked in the by-product stacking unit 314. This by-product collection step (S420) may include a heating step (S421) and a cooling step (S422). In the heating step (S421), the by-products flowing in the receiver inlet pipe 630 may be heated by the heating jacket 330 to prevent them from solidifying.

In the cooling step (S422), the by-product flowing upward through the first flow pipe 640 may be cooled and solidified. In this cooling step (S422), the solidified by-product may fall due to a load and be stacked on the by-product stacking portion 314. This cooling step (S422) may include a coil cooling step (S422a) and a jacket cooling step (S422b).

In the coil cooling step (S422a), the by-product flowing upward may be cooled by the cooling coil 322 disposed inside the receiver tank 310. In the jacket cooling step (S422b), by-products flowing upward may be cooled by the cooling jacket 321 disposed outside the receiver tank 310. In the by-product discharge step (S430), the remaining by-products collected in the by-product collection step (S420) may flow into the second flow pipe (650).

In the trap step (S440), the remaining by-products that have passed through the second flow pipe 650 may be cooled and collected in the trap 400. After this trap step (S440) is performed, only air may remain as the gas inside the trap (400).

In the air removal step (S500), the vacuum pump 500 is driven so that the remaining air inside the trap 400 can be discharged to the outside. This air removal step (S500) may be continuously performed while polyester is manufactured.

Although embodiments of the present invention have been described above as specific embodiments, this is merely an example, and the present invention is not limited thereto, and should be construed as having the widest scope following the technical idea disclosed in this specification. A person skilled in the art may implement a pattern of a shape not specified by combining/substituting the disclosed embodiments, but this also does not depart from the scope of the present invention. In addition, a person skilled in the art can easily change or modify the embodiments disclosed based on the present specification, and it is clear that such changes or modifications also fall within the scope of the present invention.

1: Polyester manufacturing equipment
100: slurry tank 200: reactor
210: Ester reactor 220: Condensation polymerization reactor
300: Receiver unit 310: Receiver tank
310a: Receiver chamber 311: Inlet
312: outlet 313: drain part
314: By-product layering section 320: Cooling section
321: cooling jacket 322: cooling coil
330: Heating jacket 400: Trap
500: Vacuum pump 600: Pipe module
610: Inlet pipe 620: First connection pipe
630: second connection pipe 640: first flow pipe
650: second flow pipe 660: discharge pipe
700: Refrigerant supply unit 800: Fruit supply unit
900: Controller C: Refrigerant
H: fruit

Claims (15)

A receiver unit including a receiver tank that collects some of the by-products flowing from the polyester condensation reactor; and
It includes a receiver pipe including a first flow pipe that guides the by-products to the receiver tank and a second flow pipe that guides the by-products so that some of the by-products flowing into the receiver tank are discharged from the receiver tank,
The receiver unit is,
a heating jacket for heating the first flow pipe to prevent the by-product flowing through the first flow pipe in the receiver tank from solidifying; and
Comprising a cooling unit that cools the by-product discharged from the receiver tank through the first flow pipe,
Polyester manufacturing equipment. According to claim 1,
The cooling unit includes a cooling coil disposed inside the receiver tank,
In the vertical direction, the cooling coil is disposed between the lower end of the first flow pipe and the lower end of the second flow pipe,
Polyester manufacturing equipment. According to claim 2,
The cooling coil is supplied with refrigerant at a temperature of 5℃ to 10℃,
Polyester manufacturing equipment. According to claim 2,
The cooling unit,
Surrounding the outer peripheral surface of the receiver tank, further comprising a cooling jacket disposed on the upper part of the receiver tank to cool the upper portion of the receiver tank,
Polyester manufacturing equipment. According to claim 4,
A refrigerant with a temperature of 5°C to 10°C flows inside the cooling jacket.
Polyester manufacturing equipment. According to claim 1,
A vacuum pump that removes air from the receiver tank so that the receiver tank is placed in a vacuum state; and
Further comprising a trap that communicates with the second flow pipe and the vacuum pump and cools the by-product that has passed through the second flow pipe,
Polyester manufacturing equipment. According to claim 6,
The temperature of the trap is -70°C to -30°C,
Polyester manufacturing equipment. According to claim 1,
The heating jacket is arranged to surround an outer peripheral surface of a portion of the first flow pipe,
A portion of the first flow pipe is disposed in the receiver tank,
Inside the heating jacket, fruit with a temperature of 220 ℃ to 250 ℃ flows,
Polyester manufacturing equipment. According to claim 1,
The temperature of the other part of the first flow pipe is 100°C to 170°C,
Polyester manufacturing equipment. According to clause 9,
Another part of the first flow pipe,
It is disposed above any part of the first flow pipe and extends between the condensation polymerization reactor and any part of the first flow pipe,
Polyester manufacturing equipment. A by-product inflow step in which by-products generated during the condensation polymerization reaction of the reactants generated in the esterification reaction step are introduced into the receiver tank through the first flow pipe, and the by-products that have flowed into the receiver tank are collected in the receiver tank. A collection step, and a by-product discharge step in which the remaining by-products collected in the by-product collection step are discharged from the receiver tank through a second flow pipe,
The by-product collection step is,
A heating step of heating a portion of the first flow pipe to prevent the by-product flowing into the receiver tank from solidifying, and a cooling step of cooling the by-product flowing through the first flow pipe through a cooling unit. doing,
How to make polyester. According to claim 11,
The cooling step includes a coil cooling step of cooling the by-product through a cooling coil disposed inside the receiver tank,
In the vertical direction, the cooling coil is disposed between the lower end of the first flow pipe and the lower end of the second flow pipe,
How to make polyester. According to claim 12,
The cooling step further includes a jacket cooling step of cooling the by-product through a cooling jacket disposed on the top of the receiver tank to cool the top of the receiver tank,
The cooling jacket surrounds the outer peripheral surface of the receiver tank,
How to make polyester. According to claim 11,
Further comprising an air removal step of removing air in the receiver tank so that the receiver tank is placed in a vacuum state, and a trap step of cooling and removing the by-product that has passed through the second flow pipe,
How to make polyester. According to claim 11,
A refrigerant with a temperature of 5°C to 10°C flows in the cooling unit,
How to make polyester.

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