Apparatus and method of use thereof

Abstract

To provide an apparatus and a process for heating or cooling a high-viscosity solution containing a polymer.SOLUTION: There is disclosed herein an apparatus comprising a shell, the shell having an inlet port for introducing a polymer solution into the shell and an outlet port for removing the polymer solution from the shell; wherein the polymer solution comprises a polymer and a solvent that is operative to dissolve the polymer; a plurality of plates in the shell; where the plurality of plates are stacked one atop the other to define a central passage that is in fluid communication with the inlet port of the shell; where the plurality of plates further define a plurality of conduits, each conduit extending radially outwards from the central passage, where the plurality of conduits are in fluid communication with the central passage; and where the apparatus is operated at a pressure and a temperature effective to maintain the polymer solution in a single phase during its travel through the apparatus.SELECTED DRAWING: Figure 1A

Description

[Technical field]

[0001] The present disclosure relates to an apparatus and process for heating or cooling high viscosity solutions containing polymers. Regarding s. [Background technology]

[0002] Polymers and polymer products (hereinafter referred to as "polymers") are often prepared in the presence of solvents and and other volatile components (e.g., monomers and by-products) (solvents and The combination of the polymer and the solubilizing solvent is During the production of polymers, the polymer solution is heated or It may be necessary to remove heat from the polymer solution.

[0003] Solution polymerization can be accomplished in adiabatic or non-adiabatic reactors, where part of the heat of reaction is One advantage of the latter is that it is possible to reduce the amount of heat generated by the process without the presence of a heat exchanger. The advantage of this method is that it allows for a higher production rate compared to conventional methods. It is desirable to remove volatiles from the polymer. The process of removing volatile substances from a polymer solution is generally called "devolatilization." This is achieved by heating the polymer solution to a temperature above the boiling point of the volatile substances, and at the same time (heating Volatile substances evolved during the heating process (in parallel with the heating process) or consecutively (after heating) were extracted from the polymer solution. can be.

[0004] The heat exchanger used for this purpose is the shell-and-tube heat exchanger, The tubes are placed in a vessel where heat is removed by circulating cooling water on the shell side of the vessel. One potential problem with these heat exchangers is the amount of heat that needs to be removed from the process. The high pressure drop used for the amount of reaction is required to remove the heat of reaction while minimizing the pressure drop. It is advisable to remove

[0005] In addition, shell-and-tube heat exchangers suffer from high pressure drop and reduced heat transfer coefficient. This allows for the processing of high viscosity polymer solutions of 10,000 to 1,000,000 centipoise. Therefore, it is not possible to maintain the polymer and solvent in a single phase at temperatures above 150°C. It would be desirable to have a heat exchanger capable of handling the aforementioned high viscosity polymer solutions. Summary of the Invention

[0006] As used herein, an inlet port for introducing a polymer solution into the shell, and a polymer a shell having an outlet port for removing the polymer solution from the shell; The shell contains the polymer and a solvent that acts to dissolve the polymer; The conduits are stacked to define a central passageway in fluid communication with the inlet port of the shell, and each of the conduits extends from the central passageway. a plurality of plates within the shell further defining a plurality of conduits extending radially outward from the and a plurality of plates, the plurality of conduits being in fluid communication with a central passage. and while the device moves through the device from the inlet port of the shell to the outlet port of the shell, It is operated at a pressure and temperature effective to maintain the polymer solution in a single phase.

[0007] Also referred to herein is an inlet port for introducing a polymer solution into the shell, and a shell having an outlet port for removing the polymer solution from the shell; The conduits are joined together to define a central passageway in fluid communication with the inlet port of the shell, and each of the conduits extends from the central passageway. A plurality of plates disposed within the shell further defining a plurality of conduits extending radially outward. and a plurality of plates, the plurality of conduits being in fluid communication with a central passage. and discharging the single-phase polymer solution from the inlet port of the shell to the outlet port of the device. The apparatus is operated at a pressure and temperature effective to maintain the polymer solution in a single phase during movement through the and removing the single-phase polymer solution from an outlet port of the apparatus, The polymer solution is at a higher temperature than the inlet port. or the polymer solution maintains the same temperature at the inlet and outlet ports. However, a method is also disclosed in which the heat of reaction is removed from the polymer solution. . [Brief description of the drawings]

[0008] [Figure 1A] 1 is a schematic diagram of an exemplary apparatus. [Figure 1B] 1A and 1B are side and top views of a support tube. [Diagram 2] FIG. 2 is another schematic diagram of an exemplary apparatus. [Figure 3A] FIG. 2 is a top view of an exemplary plate in the apparatus. [Figure 3B] 1 is a top view of another exemplary plate within the apparatus. [Figure 4A] FIG. 3B is an enlarged schematic top view of cross section XYY′X′ seen in FIG. 3A. [Figure 4B] FIG. 3C is another enlarged schematic top view of a cross section of the plate from FIG. 3B. [Diagram 5] FIG. 4B is an enlarged schematic side view of section AA' seen in FIG. 4A. [Figure 6] FIG. 1 is a schematic diagram of an exemplary devolatilizer involving top-to-bottom (inside-to-outside) flow of polymer solution. [Figure 7] FIG. 1 is a schematic diagram of an exemplary devolatilizer involving bottom-to-top (outside-to-inside) flow of polymer solution. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0009] In the present specification, the temperature of a high-viscosity solution containing a polymer is increased or decreased, or An apparatus and process for removing heat of reaction or reaction heat passing through the apparatus is disclosed. While maintaining the polymer solution in a single phase during transportation, its temperature is increased to its initial temperature (e.g., or alternatively, by increasing or decreasing the temperature by an amount of more than 10°C from the inlet port temperature. Maintaining the polymer at a constant temperature (in a reactive polymer solution system) The pressure drop is effectively designed to reduce as little as possible.

[0010] In short, it is the process of increasing, decreasing or keeping the temperature of the polymer solution constant. While facilitating the process, the pressure of the polymer solution is reduced as little as possible. The device facilitates changes in pressure of the polymer solution while allowing the polymer to be transported through the device. To heat, cool, or maintain a constant temperature (from the inlet port to the outlet port) of a solution can be used for.

[0011] In one embodiment, the device is a shell and plate heat exchanger. In the method, the apparatus comprises a shell in which a plurality of plates are disposed, stacked on top of each other. , when a pair of adjacent plates (with their associated walls) contact each other, multiple radial The conduits are arranged to pass the polymer solution from the center of the shell to the outside of the shell, or Alternatively, it can facilitate the transport of the gas from the outside to the center of the shell while increasing its temperature. Alternatively, the device may be a cylindrical shell in which the plate is The heat exchanger may be described as a flat plate heat exchanger suspended within a fin.

[0012] Therefore, the device includes a pressure controllable system and is entirely solvent and single-phase polymer. While maintaining the temperature of the polymer solution at 120°C to 300°C, preferably 180°C to The temperature rises from 0°C to 260°C, and the pressure drops from the inlet pressure to 70 kilograms per square centimeter (kg f / cm 2 ) and preferably less than 35kgf / cm 2 In one embodiment, Inlet pressure is 35 to 250 kgf / cm 2 and the outlet pressure is 20 to 200k. gf / cm 2 The single phase is a liquid phase. The polymer solution is hereinafter referred to as 100 to 2,000,000 centipoise, preferably 50, as measured as described in detail below. ,000 to 1,000,000 centipoise, more preferably 100,000 to 600, It is a highly viscous solution having a solution viscosity of 0.000 centipoise.

[0013] In another embodiment, the apparatus includes a pressure-controllable reactive exothermic system, such as a polymerization system. The polymer solution is heated to a temperature between 120°C and 300°C, preferably while maintaining all the solvent and the polymer in a single phase. The desired temperature is preferably kept in the range of 150°C to 230°C, and the pressure is kept within 50 K from the inlet pressure. log per square centimeter (kgf / cm 2 ) less than 25kgf / c m 2 In one embodiment, the inlet pressure is reduced by less than 35 to 250 kgf / cm 2 The outlet pressure is 20 to 200 kgf / cm 2The single phase is the liquid phase. The solution is measured as detailed below until the end of this disclosure, 500 to 20,000 0 centipoise, preferably 1,000 to 10,000 centipoise. High viscosity solutions. One or more of these devices are part of a polymerization reactor system. may be also possible.

[0014] Also provided herein is a method for producing a polymer solution from a device in fluid communication with a pressure control device. Allows volatilization of volatile materials (e.g., solvents, volatile by-products, volatile reactants, etc.) from the A degassing apparatus is also detailed, comprising a pressure control vessel and a separate low pressure flash vessel. The control device is variably adapted to control the pressure within the apparatus to keep the polymer solution in a single phase. In one embodiment, the devolatilizer is equipped with a high viscosity polymer solution. The device may further include a pump to facilitate filling the device.

[0015] 1A and 2 show schematic diagrams of an exemplary device, and FIGS. 3A and 3B show the configuration of the device. 1A, 2, 3A and 3B are top views of one exemplary embodiment of a plate placed on the 3B, the device 100 dispenses the polymer solution from the center of the device to its outer periphery. A plurality of plates 104 (also referred to herein as a plate stack) to be transported are arranged. In one embodiment, each plate 104 comprises a shell 102 that is formed by bonding the inner periphery of the plate. 107 to the outer periphery 109, and extends radially outward from the center of the device to its outer periphery ( 1A) to deliver a polymer solution from its outer periphery to its interior. In the center, a plurality of channels 106 (see FIG. 3A) transport the polymer solution in opposite directions (see FIG. 2). 3B) and / or 406 (see FIG. 3B). The floor may have channels 106 formed therein (e.g., machined into the floor), or alternatively may have channels 106 formed therein (e.g., machined into the floor). Note that the channel 106 may be formed when combined with the wall 108. Plates and walls with multiple channels (one plate bottom to adjacent plate The combination of the wall (measured to the bottom of the wall) is also called a "layer." 108 may be an integral part of the plate 104 or may be in contact with the plate 104. It may be a separate unit that creates the channel 106. The device 100 is assembled The channel between the floor and wall of the plate also serves as the upper adjacent plate (which acts as the roof). ) and the polymer solution is distributed from the center of the shell to the outer periphery and Alternatively, they form a "conduit" leading from the outer periphery to the center of the shell.

[0016] 1A and 2, the shell 102 is formed by dissolving a polymer solution 200 (see FIG. 1A) and and / or 500 (see FIG. 2) into the device via an inlet port 120; and an outlet port 130 through which the polymer solution is removed. 0 and outlet port 130 are not in direct fluid communication with each other. Plate 152 (without a central hole) is placed in the middle of the device to allow the polymer solution to pass through the inlet port of the device. 120 directly to the outlet port 130. The shell 102 is provided with a Other than the inlet port 120 located at the bottom of the shell and the outlet port 130 located at the bottom of the shell, The polymer solution is introduced at a first temperature (T1) and a first pressure (P1). The second temperature (T2) and the second pressure (P2) are supplied to the inlet port 120 and the outlet port 130, 130. In one embodiment, T1 is lower than T2 and P1 is lower than P2. In another embodiment, T1 is higher than T2 and P1 is higher than P2. In this embodiment, T1 is the same as T2, but P1 is higher than P2.

[0017] The flow of the polymer solution is depicted and described in this application as either top to bottom or bottom to top. Although the device is described as being horizontal (as shown in Figs. 1A, 2, 6, and 7, but not vertically), The flow can be described as left to right or right to left. Therefore, the top-to-bottom or bottom-to-top flow description is subject to change without notice. It is simply a way to enable a user to understand how a device functions.

[0018] In another embodiment, the polymer solution is introduced into the device at the inlet port 120 in a single phase. , exiting the device at outlet port 130 in a single phase. During movement of the polymer solution through the device, the polymer The solution is 20 kgf / cm 2 More than 40kgf / cm 2 More than 60kg, preferably f / cm 2 More than 70kgf / cm 2 More preferably, 80kgf / cm 2 Super The reaction is always single phase due to the pressure in the reactor being maintained at 1000 K. The pressure in the reactor is maintained at 1000 K. The solvent, unreacted The monomers, and by-products of the reaction are kept from vaporizing within the apparatus.

[0019] In FIG. 2, the shell 102 is a shell through which the polymer solution 500 fills the device. An inlet port 120 is located at the bottom of the well and a shell through which the polymer solution is removed. and an outlet port 130 located at the top of the tube. 30 are not in direct fluid communication with each other, and fluid passes through conduits (104) along the periphery of the device. The plate 152 (middle) located at the bottom of the stack of plates must be moved. The absence of a central hole prevents the polymer solution from flowing directly from the bottom to the top of the device. 02 has an inlet port 120 located at the bottom of the shell and an outlet port 122 located at the top of the shell. The polymer solution is heated to a first temperature (T1) and a second temperature (T2). The inlet port 120 is filled with the first pressure (P1) and the second temperature (T2) and the second pressure (P3) are (P2) through the exit port 130. In one embodiment, T1 is lower than T2. In another embodiment, T1 is greater than T2 and P1 is greater than P2. In yet another embodiment, T1 is the same as T2, but P1 is higher than P2. is also expensive.

[0020] In the configuration shown in FIG. 2, the polymer solution is introduced into the device at inlet port 120 in a single phase. The polymer solution is then mixed with the polymer solution and exits the device at outlet port 130 in a single phase. -The solution is 20kgf / cm 2 More than 40kgf / cm 2 Above 60k, preferably gf / cm 2 More than 70kgf / cm 2 More preferably, 80kgf / cm 2 Due to the pressure in the apparatus being maintained above 1000 K, it is always single phase. The solvent, unreacted monomer, and The by-products of the reaction are not vaporized within the device.

[0021] In the configuration shown in FIG. 1A, the plates in the plate stack are aligned with the tubes in the tube bundle. By the tube 140 and the support slot tube 158 (hereinafter, support tube 158) The support tubes 158 provide structural support to the plate stack. , which holds the plate in place and prevents damage to the plate during operation of the device. This enables the plate stack to withstand the high pressures used in the device during operation. In the configuration shown in FIG. 2, the support tube 158 is not present.

[0022] As described in more detail below, when the plates are stacked vertically, they are heated by a polymer solvent. The support tube 158 forms a passageway 300 through which fluid is transported. It sits in passage 300 and contacts end plate 152 to provide structural support thereto.

[0023] The support tube 158 comprises a tubular shell 157 having an opening 156 disposed therein. The opening 156 allows the polymer solution to flow into the ring 159. The polymer solution is filled and delivered through the passage 300 to the conduit (see FIG. 1B) or through the conduit. 2. The ring plate assembly 10 4 is held in place by a lock nut (162) located on the end of the support tube 158. Can be held together.

[0024] The following paragraphs detail the top-down flow of the polymer solution as seen in Figure 1A. The configuration in which the polymer solution flows from bottom to top as shown in FIG. 2 will be described in detail later.

[0025] Top to bottom flow The term "top-to-bottom" flow refers to the flow in Figure 1A (when the device is mounted vertically). This is used to describe the flow of the polymer solution inside the device. It is sometimes called inside-out flow because the flow occurs from the inside to the outside periphery of the device. The terms "top-down" flow or "inside-out" flow refer to how the device functions. This is just one way of explaining to the reader how the device is mounted horizontally rather than vertically. If the flow is centered on the left, the flow can occur from left to right or right to left.

[0026] In FIG. 1A and FIG. 3A, each plate 104 of the plurality of plates (the bottom plate 1 52) are openings that allow the polymer solution to move from the top to the bottom of the device. When the plates 104 are stacked vertically, the openings 112 from each plate are 12 are vertically aligned to form a passageway 300 through which the polymer solution is transported within the device. In an embodiment, the opening 112 is located at the center of each plate 104. The connector 104 is ring-shaped as can be seen in Figures 3A and 3B.

[0027] The shell 102 may have any cross-sectional shape, but its cross-sectional area when viewed from above is generally circular. In an exemplary embodiment, the shell 102 is preferably shaped like a 00 to 700 centimeters, preferably 250 to 400 centimeters, The inner diameter d1 is 120 to 400 cm, preferably 150 to 180 cm. The inner diameter d1 referred to in this specification is the diameter measured on the inner surface of the shell. An exemplary material of construction for the shell 102 is metal. An example of a suitable metal is carbon steel. , stainless steel or other metal alloy.

[0028] Each plate 104 (see FIGS. 3A and 3B) has a diameter slightly smaller than the inner diameter d1 of the shell. The space between the inner surface of the shell and the outer periphery of the plate 104 is This allows for the passage of the polymer solution during migration through the station 100, as will be described later. The average difference between the inner diameter d1 of the shell (see above) and the outer diameter d3 of the plate is 1 to 1 50 centimeters, preferably 10 to 50 centimeters.

[0029] The opening 112 in the plate 104 has a diameter of 10 to 150 centimeters, preferably 40 to 50 centimeters. The annular space 159 has a diameter d2 of 100 centimeters. The support tube 158 has a width of 5 to 50 centimeters. 0 cm, preferably 5 to 20 cm thick. 58 has between 2 and 40 openings 156, preferably between 6 and 36 openings along its length and surface. It's fine.

[0030] An exemplary material of construction for the plate 104 is metal. Examples of suitable metals are aluminum, carbon steel, stainless steel or other metal alloys. In an embodiment, the inner periphery 107 and the outer periphery 109 of the plate 104 are both flush with each other. 102 and is concentric with the inner surface of the shell 102.

[0031] 1A, 3A and 4A, each plate is A plurality of radii having increasing widths over at least a portion of a radius extending from 107 to the outer periphery 109. 4A is an enlarged schematic top view of the cross section XYY'X' shown in FIG. which represents one possible design of the channel 106. In one embodiment, each plate has 1, the plate 104 has a plurality of channels 106 whose width increases from the inner periphery 107 to the outer periphery 109. In one embodiment, each channel extends from the inner periphery 107 to the outer periphery 109 of the plate 104. It may have a certain width up to

[0032] The polymer solution 200 enters the device through the inlet port 120 and travels along a passageway 300. 104 and contacts a plurality of plates 104 where it flows radially outward along a plurality of channels 106 Between each successive pair of channels 106 in the plate 104, a heat transfer fluid 1 50 includes a bore 110 for accommodating a bank of tubes 140 to be transported therethrough. A wall 108 is placed (see FIG. 1A).

[0033] The heat transfer fluid 150 transfers heat to the polymer solution as it is transported through the device 100. - facilitating heating or cooling of the solution (see FIG. 1A). The heat transfer fluid 150 is placed in the tube Through the tubes of the bundle 140 from the bottom to the top of the device, or alternatively from the top of the device In yet another embodiment, the tube 140 may be configured to allow the fluid to pass through the device 10. Some tubes can be arranged to transport fluid back and forth through the and then connected to a common header, which can then transport fluid from bottom to top. .

[0034] As can be seen in FIG. 4A, the channel 106 has a width that gradually increases in the radial direction. The inner periphery 107 of the plate 104 is bounded by a pair of walls 108A and 108B. In this embodiment, the channel 106 extends from the inner periphery 107 to the outer periphery 109. The width does not decrease from the outer periphery 109 to the outer periphery 109.

[0035] In the embodiment shown in FIG. 4A, the walls 108A and 108B are The walls 108A and 108B extend radially outwardly in a straight line from the inner periphery 107 to the outer periphery 109. 108B are closer to each other at the inner periphery 107 and farther apart at the outer periphery 109. The channel 106 has a width that gradually increases from the inner periphery 107 to the outer periphery 109 of the plate. As noted above, walls 108A and 108B are integral with plate 104. (i.e., the wall 108 and the plate 104 are a monolithic part) , or alternatively, a separate, independent part that is assembled with the flat plate 104 and the channel 106 may be formed.

[0036] The channel width "d5" at the inner circumference is less than the channel width "d6" at the outer circumference. The ratio of d6 to d5 is 2:1 to 6:1, preferably 2.2:1 to 3.5:1. In this embodiment, the distance d6 is 4 to 8 centimeters, preferably 5 to 7 centimeters. The distance d5 is 1 to 4 centimeters, preferably 2 to 3 centimeters. The channel 106 is located 0.10 to 0.75 centimeters from the top of the wall 108, preferably 0. It has a floor with a depth of 0.2 to 0.4 centimeters.

[0037] Thus, the polymer solution migrates from the opening 112 (see FIG. 1A) to the periphery 109. As the fluid moves through the slot, it contacts the ever-expanding channel. This reduces the pressure drop when the heat exchanger moves and increases the heat transfer area, allowing optimal heat transfer. This is advantageous in that

[0038] Walls 108 are positioned between the channels 106 to separate successive channels on a particular plate. The walls 108 and channels 106 extend across the surface of the plate 104 and separate the panels from one another. As described above, each wall 108 is uniformly distributed with respect to the fluid 1 50 includes a plurality of holes 110 that accommodate tubes 140 flowing therethrough (see FIG. 1A). see).

[0039] In one embodiment, the single plate 104 has a thickness of 30 to 90 mm, preferably 55 to 65 mm. The channel has 30 to 90, preferably 55 to 65 walls 108, and the walls and the channel The panels alternate evenly with each other around the plate 104. Each wall 108 is connected to a tube 14. Each wall 108 contains between 8 and 40 tubes, preferably between 10 and 35 tubes. In one embodiment, the tube is a metal tube and may include carbon steel.

[0040] The wall 108 has a thickness of 1.5 to 3 centimeters, preferably 2 to 2.5 centimeters. In one embodiment, the wall thickness of the tube 140 in the tube bundle is The outer diameter of each tube in the tube bundle is 2 to 10% larger than the outer diameter, preferably 3 to 5% larger. 40 has an inner diameter of 1 to 3 centimeters and an outer diameter of 1.5 to 4.0 centimeters The preferred inner diameter of the tube is 1.5 to 2 centimeters, and the preferred outer diameter is 2 .0 to 2.2 centimeters.

[0041] 3B and 4B show that the width "w" of the channel 106 decreases over a portion of the plate radius. Another exemplary wall 108 having a small diameter and then increasing over a portion of the plate radius. In this embodiment, the wall 108 is connected to the plate 104 (e.g., a monolithic It may be integral with the plate 104 (contact unit) or may be separate from the plate 104. 1A, 3B and 4B, each plate is formed by inserting an inner periphery 107 of plate 104 into the inner periphery 107 of plate 104. A plurality of channels having a decreasing width over at least a portion of a radius extending from the After decreasing over a portion of the plate radius, the channel advances to the outer periphery 109. The width increases as the

[0042] FIG. 4B shows a first generally converging zone 402 that is wider at its entrance than at its exit; The minimum width of the panel is sufficient to provide a pressure effect across the restricted zone, thereby maximizing a second restriction zone 404 to prevent substantial flashing of volatile components while in the first zone; ; A small reduction in pressure in the polymer solution is applied while the polymer solution is continuously kept in a single phase. a third generally expanding zone 406 designed to enable The shape of the channel 106 is shown. The inner periphery 107 and the outer periphery 108 of the plate 104 in FIG. 9 (representing the length of the channel 106) is detailed above and shown in FIGS. Same as detailed in A.

[0043] Now referring to FIG. 4B, distance d9 is greater than d7, which in turn is greater than d8. The first zone 402 has an opening 418 through which the polymer solution enters the channel 106. The length of the first zone is 5 to 20% of the total length of the channel, and the width of the inner periphery 107 is 1.0 to 5.0 centimeters (cm) relative to the width of the first zone at its narrowest point The ratio of widths at the widest points of the zones varies from 1.5:1 to 10:1.

[0044] The second zone 404 begins at the end of the first zone and extends in length to the inlet of the third zone. The width of the second zone varies from about 1.0% to 40% of the total length of the channel that connects to the Remains constant over its entire length, decreases to a minimum, then remains constant, or reaches a maximum Preferably, at its narrowest point, the second zone is 0.25 to 4.00 centimeters in width, more preferably 1 to 2 centimeters in width The ratio of the width of the zone at its widest point to the width of the zone at its narrowest point is preferably 1. Preferably, the ratio of the first width to the narrowest width of the second zone is 0:1 to 1.5:1. The ratio of the widest width of one zone is greater than 2:1, preferably greater than 3:1.

[0045] The third zone 406 begins at the end of the second zone and is used for the discharge of the polymer solution. It terminates at an outlet 420. The length of the third zone is approximately 40-85% of the total length of the channel. The ratio of the width of the third zone at its inlet to its end is preferably 1.75:1. ~10:1. The width of the zone does not need to increase continuously from the entrance to the end, but should be sinusoidal. It may follow a curve or other curved shape. Also preferably, the minimum width of the restriction zone is The third zone has a maximum width ratio greater than 2:1.

[0046] As can be seen in Figure 1A, the plate transfers heat to the polymer solution filled in the device. For ease of use, they are stacked together in a shell. A', which shows six plates 104 (104A, 104B, 104C, 104D, 104E and 104F). FIG. 5 shows a stack of plates 1 1 shows a side partial cross-sectional view of a portion of the outer periphery of a stack of 04. The stacked and heated members are arranged to define the walls, floor and ceiling of each conduit 114. 1A. The polymer solution is then passed through the opening 300 of the opening 300. The polymer solution is then passed through the opening 300. The plate 104E includes a plurality of plates 104 in the shape of a fixed disk. The plate 104F contacts the upper surface of the wall of the adjacent plate 104F so that the polymer solution flows through it. The conduit 114 includes the floor 160, the roof 150, and the walls 108 to be transported.

[0047] Each conduit may have a constant width along its length or may have a width that varies along its length. As discussed above for each channel, the width may vary depending on the interior of the plate. The length may gradually increase from the circumference to the outer circumference. The width may increase over a portion of the length of the conduit and decrease over the remaining length of the conduit. In an embodiment, it has a reduced width over a portion of its length and a widened width over the remaining length of the conduit. The width may increase accordingly.

[0048] A tube 140 (not shown) passes through a hole 110 in the wall 108 and heats the channel 106. In one embodiment, the tube 140 is configured to transmit 10 are fastened together to form a stack (where the walls 108 and plates 104 form a single integral structure). In another embodiment, the tube 140 is formed by the wall 108 and the plate. The plates 104 are fastened together to form a stack (although the walls 108 are separate structures from the plates 104). The heat is transferred to the wall 108 by the fluid 150 in the tube 140. , is transmitted from the wall to the floor 160 of the channel 106 and to the roof of the channel 150.

[0049] As mentioned above, the plates 104 are stacked vertically within the shell 102. Each plate has a thickness of 0.1 to 1.0 centimeters, preferably 0.2 to 0.3 centimeters. The plates are spaced apart from each other by a distance of 100 mm. The total number of plates (in the stack) is 50-1000, preferably 700-800. In one embodiment, the total number of channels in the shell is between 1,000 and 100,000. and the total number of walls in the shell is between 1,000 and 100,000.

[0050] Now referring to Figures 1A, 3A, 3B, 4A and 4B, one embodiment of the device for operating the device is shown in Figure 1. In this manner, the polymer solution 200 entering the inlet port 120 is The route indicated by A~200B~200C~200D~200E is installed at the outlet port 130. The polymer solution 200 enters the inlet port 120 and moves through the inlet port 120 until it exits the inlet port 120 (see FIG. 1A). enters the device at temperature T1 and pressure P1 and initially travels vertically downward along path 300 Plate 152 prevents the vertical passage of the inlet port 120 to the outlet port 130. The polymer solution 200 then flows through the passage 300 towards the plate stack 104. 200A, where it enters the plurality of channels 106 and The robot moves along a path 200B (see FIGS. 3A and 3B) positioned within the robot. At the same time, the fluid 150 is transported through the tube 140, transferring heat from the fluid to the polymer solution. The plate then travels radially outward within channel 106 along path 200B. During the transfer through the tack, the temperature of the polymer solution increases above T1 and simultaneously the pressure The force drops to a pressure below P1.

[0051] Please note that this device can also be used as a cooler. If done, the temperature of the polymer solution is reduced during transport through the device. In the case where a cooler is used in a reaction system, it is used to cool the reaction (e.g., an exothermic reaction) The heat generated during the reaction can be extracted, and the temperature of the polymer solution increases with the amount of heat removed. The temperature of the polymer solution may increase or decrease depending on the amount of heat released from the reaction taking place. The mixture remains in a single phase while moving through the stack. In one embodiment, the single phase is a liquid phase. It is.

[0052] The polymer solution discharged from the outer periphery 109 of the plurality of channels 106 is plated with the shell. The space between the outer periphery of the stack is then moved along path 200C to the bottom of the device. It is transported from the bottom of the device along path 200D to the exit port 130 and then It remains single phase and is transported out of the device via exit port 130 along path 200E.

[0053] The polymer solution leaving the apparatus has a higher temperature than the inlet temperature T1 (in a reactive exothermic system); An outlet temperature T2, which may be lower or the same as the inlet pressure P1, and an outlet pressure T3, which may be lower than the inlet pressure P1. The nozzle has a mouth pressure P2.

[0054] Flow from bottom to top The term "bottom-to-top" flow is used in conjunction with Figures 2, 3A, and 3B (where the device is mounted vertically). It is used to detail the flow of the polymer solution in the It is called outside-to-inside flow because the liquid flows from the outside periphery of the device to the inside of the device. The terms "bottom-up" flow or "outside-in" flow are sometimes used when the device is It is just a way to explain to the reader how it works. If the device is mounted horizontally, the flow can be from left to right or right to left. do.

[0055] 2, 3A and 3B show embodiments where the polymer solution flows from the bottom to the top of the device. The arrangement of the plates 104 within the shell 102 is shown for this configuration (see FIG. 2). The flow direction is the same as in FIG. 1A. However, the flow direction is different from that in FIG. 1A. As shown in Figure 2, the polymer solution was introduced into the inlet port located at the bottom of the device. It enters the apparatus via 120 and exits through an exit port 130 located at the top of the device. A plate 152 located at the bottom of the plate stack provides a port from port 120 to port 130. The polymer solution is introduced into the inlet port 120 along a path 500 to prevent direct flow of the polymer solution. 102 and moves through paths 500A and 500B to connect plate 152 and outer shell 102 of the device. The polymer solution then enters the plate stack and travels upward between path 500. C (see Figures 3A and 3B) radially inward through the conduit to the periphery of each plate The polymer solution travels from 109 toward the inner periphery 107. The polymer solution travels through the conduit in a manner similar to that of FIG. 1A. It is heated or cooled as it moves through the In this case, the device does not use a support tube 158. The tube and tie rods are The plates are held together with a clamp.

[0056] During its travel through the plate stack, the temperature of the polymer solution rises above T1. In another embodiment, the pressure of the polymer solution is increased and simultaneously the pressure is decreased to a pressure less than P1. The temperature is reduced to a temperature below T1 and simultaneously the pressure is reduced to a pressure below P1. In this embodiment, the polymer solution remains in a single phase (e.g., liquid phase) while moving through the plate stack. In another embodiment, the single phase is a liquid phase.

[0057] Please note that this device can also be used as a cooler. If done, the temperature of the polymer solution is reduced during transport through the device. In the case where a cooler is used in a reaction system, it is used to cool the reaction (e.g., an exothermic reaction) The heat generated during the process can be extracted, and the temperature is released in response to the amount of heat removed. It can go up or down depending on the amount of heat given off.

[0058] The polymer solution exiting the plate stack is directed to device 100 via path 500D. This leads from the center to the exit 13 of the device via a path 500E. In one embodiment, the outlet 130 is a conduit for further transport of the polymer solution. The conduit may be connected to a pipe. The conduit may be part of a reactor system. In the process, the outlet 130 is connected to a conduit which then subjects the polymer solution to reduced pressure for phase separation. It is connected to a valve that releases the

[0059] Operating conditions In an exemplary embodiment, the inlet temperature T1 is 120 to 230° C., and the inlet pressure P 1 is 35~250kgf / cm 2 and the outlet temperature T2 is 150 to 300°C; Outlet pressure P2 is 20 to 200 kgf / cm 2 It is.

[0060] The polymer solution generally contains 10 to 95 weight percent based on the total weight of the polymer solution. The solution contains 1,000% by weight of the polymer, preferably 20 to 85% by weight. ~2,000,000 centipoise, preferably 50,000~1,000,000 centipoise More preferably, the viscosity is between 100,000 and 600,000 centipoise. The average viscosity of the solution, measured as detailed below, is 300,000 to 350,000. The polymer solution may have a viscosity of 40,000 to 2,000,000 kg grams per hour, preferably 100,000 to 200,000 kilograms per hour, more preferably is transported through the device at a rate of 50,000 to 150,000 kilograms per hour. is 0.5 to 50 kg / hour / conduit, preferably 1 to 5 kg / hour / conduit, more preferably Preferably, it is 3 to 4.5 kilograms per hour per conduit.

[0061] Fluid 150 has a maximum inlet temperature of 280-300°C and a minimum outlet temperature of 200-220°C. The fluid generally drops in temperature by 5-10 °C during heating of the polymer solution. When the device is used as a heater, the maximum inlet temperature of the fluid is always higher than the minimum outlet temperature. Alternatively, the device can be used as a chiller, in which case the minimum outlet temperature of the fluid is It is always higher than the maximum inlet temperature and the cooling fluid typically rises in temperature by 5-10°C.

[0062] The polymers that are mixed with the solvent can be thermoplastic polymers, lightly crosslinked polymers, or The polymer may be a blend of a thermoplastic polymer and a lightly crosslinked polymer. are oligomers, homopolymers, copolymers, block copolymers, alternating copolymers, lamellar copolymers, Random copolymers, graft copolymers, star block copolymers, dendrimers, etc. Or it may be a combination of these.

[0063] Examples of polymers that can be mixed with the solvent include polyolefins, polyacetals, Polyacrylic, polycarbonate, polystyrene, polyester, polyamide, polyamide Imide, polyarylate, polyarylsulfone, polyethersulfone, polyphenylene Polyethylene sulfide, polyvinyl chloride, polysulfone, polyimide, polyetherimide, poly Polytetrafluoroethylene, Polyether ketone, Polyether ether ketone, Polyethylene -Terketone, polybenzoxazole, polyoxadiazole, polybenzothiazinof Ethiazine, polybenzothiazole, polypyrazinoquinoxaline, polypyromellitoyl Polyquinoxaline, Polybenzimidazole, Polyoxindole, Polyoxoy Polyisoindoline, polydioxoisoindoline, polytriazine, polypyridazine, polypyridazine Perazine, polypyridine, polypiperidine, polytriazole, polypyrazole, polypi Roridin, polycarborane, polyoxabicyclononane, polydibenzofuran, polyphthalic acid Lithium, polyanhydrides, polyvinyl ethers, polyvinyl thioethers, polyvinyl alcohols polyvinyl ketone, polyvinyl halide, polyvinyl nitrile, polyvinyl ester , polysulfonate, polynorbornene, polysulfide, polythioester, poly Sulfonamide, polyurea, polyphosphazene, polysilazane, polyurethane, polysiloxane Sun, etc., or combinations thereof.

[0064] Exemplary polymers are polyolefins. Examples of polyolefins include polypropylene. and other propylene-based polymers, polyethylene and other ethylene-based One or more C2-C containing polymers 10 Olefin homopolymers and copolymers - (including graft copolymers), as well as olefin block copolymers. Such olefin-based polymers include high density polyethylene (HDPE), low density Polyethylene (LDPE), Linear Low Density Polyethylene (The Dow Chemical LLDPE sold under the trademark "DOWLEX" by Dowlex Co., Ltd. Polyethylene (ELIT) (e.g., those sold under the trademark "Aryloxycarbonyl E"), metallocenes, constrained geometry, polyvalent aryloxy ethers, These include polymers made via molecules such as ethers or single-site catalysts. Examples of such polymers are linear or substantially linear ethylene copolymers (e.g., The Dow Chemical Company has awarded "AFFINITY" and "ENG Products sold under the trademark "AGE" and ExxonMobil Chemical Sold by l Company under the trademarks "EXACT" and "EXCEED" propylene-based copolymers (The Dow Chemical Co. sold under the trademark "VERSIFY" by ExxonMobil, Inc. Sold under the trademark "VISTAMAXX" by Obil Chemical Company (The Dow Chemical Company, etc.) and olefin block copolymers (The Dow Chemical Company, etc.) (e.g., those sold under the trademark "INFUSE" by the INFUSE Company) and other polyolefin elastomers (The Dow Chemical Comp Sold under the trademark "NORDEL" or "NORDEL IP" by any PDM, etc.).

[0065] The solvent varies depending on the polymer being produced. Carbonate, butyrolactone, acetonitrile, benzonitrile, nitromethane, Non-proton benzene, sulfolane, dimethylformamide, N-methylpyrrolidone, etc. Some polymers are solvated using carboxylic, polar, or combinations of these solvents. Methanol, acetonitrile, nitromethane, ethanol, propanol polar protic solvents such as ethanol, isopropanol, butanol, or combinations thereof. Benzene, toluene, methylene chloride, carbon tetrachloride, hexane, dichloromethane, Other non-polar solvents such as ethyl ether, tetrahydrofuran, or combinations thereof At least one aprotic A co-solvent comprising a polar solvent and at least one non-polar solvent is used to increase the swelling power of the solvent. The polyolefins may also be modified to adjust the solvating power of the solvent. A suitable solvent is Isopar™ E from ExxonMobil.

[0066] The aforementioned polymers are produced in solution, high pressure, or slurry polymerization reactors, where the molybdenum The monomer and the resulting polymer are entrained in the solvent or diluent. Other polymer solutions may also be produced (intentionally or unintentionally) that contain volatile components. Volatile components include solvents (such as aromatic or aliphatic inert diluents), unreacted monomers, and and / or comonomers, and low molecular weight reaction by-products. The amount of solvent, unreacted monomer, unreacted comonomer, and / or other volatile components that is This can range from a large excess to merely a contaminating amount. Solution, high pressure, or slurry polymerization plans The molten polymer produced in the process is still processed in the unit after the initial flash devolatilization stage. At the time of purchase, the mixture often contains 10 to 60 weight percent or more of dissolved or entrained volatile components. Typically, the amount of residual volatile components remaining in a devolatilized polymer is determined according to ASTM D-1444. About 0.5 weight percent based on the total weight of the devolatilized polymer, as measured by 4526. %, preferably less than 0.1% by weight, and more preferably less than 0.05% by weight. It is.

[0067] The starting concentration of volatile components in the flowable material being devolatilized and the acceptable concentration in the degassed product. Depending on the level of residual volatiles present, a multi-stage (e.g., two or three stage) devolatilizer may be used. In addition, the devolatilizer can be a simple flash devolatilizer, an ionic liquid extractor, or the like. , extraction using supercritical fluids, distillation, steam stripping or carbon dioxide stripping In a separate devolatilization step, or in combination with other known devolatilization techniques, such as steam evaporating, In the case of gas stripping or carbon dioxide stripping, the present invention is carried out in the same devolatilization step. It can be used in combination with the device.

[0068] In one embodiment, the apparatus detailed above is used in conjunction with a pump and a pressure regulating device. This is shown in Figures 6 and 7. Figure 6 shows FIG. 7 shows a devolatilizer in which the flow is from top to bottom, and FIG. 8 shows a devolatilizer in which the flow is from bottom to top. The volatilization apparatus 400 includes a pump 402 located upstream of a device 404. The pump 402 has a pressure of 35 to 250 kgf / cm 2 The polymer solution is then pumped into the device 404 at a pressure of The apparatus is operable to pump the temperature of the polymer solution as described above. The pressure is increased and simultaneously decreased (and the polymer solution is kept in a single phase), and then the polymer The polymer solution is discharged in a single phase into the pressure regulating device 406. The polymer is cooled to a lower temperature. An additional heat exchanger (not shown) (acting as a cooler) may be provided as needed to operate the The device may be in fluid communication with the device via a

[0069] A pressure regulating device is located downstream of the apparatus and controls the pressure regulation to cause the polymer solution to flow in a single phase throughout the apparatus. The polymer with a significantly reduced volatile content is then transferred to the first tank ( The solvent may be collected in a separate process (not shown) and subjected to further downstream processing, while the solvent is collected In one embodiment, the devolatilizer is located downstream of the pressure regulating device. The device may also include a flushing container (not shown).

[0070] In one embodiment, the pump 402 is a positive displacement pump. Preferably, the pressure regulating device is a valve. The exemplary valve 406 is used to keep the polymer solution in a single phase until it is desired to do so. In one embodiment, the pressure regulating device is a nozzle. Or it may be an orifice.

[0071] Very high concentration of volatile components in the molten polymer, solvent from the molten polymer, unreacted In some embodiments for removal of monomers and comonomers, suitable devolatilization includes: Two or more steps in series to reduce the volatile content in the molten polymer This may require the use of the above equipment.

[0072] Most of the description in this specification applies to heating devices, but The same type of design can be used to remove heat of polymerization from a polymer reaction. As should be apparent to those skilled in the art, the cooling device is 1 operates in a similar manner, except that a cooling fluid is used within tube 150 instead of (See Figure 1A). The cooling liquid used is at a lower temperature than the polymer solution. The concept of improved heat transfer between a fluid and a viscous polymer solution at a minimal pressure drop remains a mystery. It will be believed to be advantageous for the apparatus detailed herein to be capable of being used in a variety of applications, including, but not limited to, the following: is explained in. EXAMPLES

[0073] Example 1 This is an example demonstrating the device disclosed herein. The plate heat exchanger has an outer diameter d1 160.2 cm (see Figure 1A), inner diameter d2 90 cm, total height The exchanger is designed in a cylindrical shell configuration of 360 cm (see Figure 1A). The exchanger includes a plurality of layers, each layer including a plate and a wall. Each layer of the exchanger includes 60 channels. Each channel has a height of 0.254 centimeters and each layer has a height of 0.2 It is separated by a 54 cm plate.

[0074] The banks of tubes carry the fluid and are arranged vertically in layers of the heat exchanger. Contains 60 banks of tubes. Each bank of tubes has an inner diameter of 1.42 cm and an outer diameter of It contains 13 carbon steel tubes, each 2.23 cm in diameter. The wall thickness of each is 2.28 cm. Each channel has an inner perimeter of 2.5 centimeters, an inner width of 6.3 centimeters, and The width of the perimeter of the tube is 0.0 ... There are 60 in total, conduits totaling 43,200.

[0075] Using standard heat transfer calculations of convection through the fluid and conduction across the tube walls, The overall heat transfer coefficient U of this exchanger is U = 130 W / m 2 ·K is calculated as 43,2 The total internal heat transfer area (A) of the 00 channels is 1,430 m 2 and the U×A (UA) value The product of these two is a 185,900W / K heat exchanger.

[0076] The equipment is operated at 159,000 kg / h of polymer solution and 160°C to 2 Solution temperature increase to 50°C and fluid temperature decrease from 290°C to 283°C (polymer in the device) - Considering the process of the solution, the logarithmic mean temperature difference of this exchanger is 74 °C, and the total heat load is calculated to be 13.8 million watts.

[0077] The total flow rate through each conduit is approximately 3.7 kg / hr. Assuming viscosity, and using standard pressure drop (Bernoulli) calculations, the pressure drop is 31.5kgf / cm 2 It is calculated as follows.

[0078] Without being limited by theory, the polymer solution is kept in a single phase within the heater, so the detailed apparatus The design works efficiently and allows for the maximum calculable heat transfer rate. When the solution changes phase, The heat transfer rate is greatly reduced and the solution loses heat through evaporation. Both of these are avoided and the equipment This ensures that the polymer solution in the device remains single-phase throughout its residence time in the device. The polymer solution in the device does not separate into two (or more) phases.

[0079] This design has a high solution viscosity of 100,000 to 2,000,000 centipoise, Advantageous in that it can handle average solution viscosities from 25,000 to 375,000 centipoise Also, it is preferably more than 30% by weight based on the total weight of the polymer and the solvent. At polymer concentrations of more than 40% by weight, more preferably more than 50% by weight, It can handle high flow rates from 0 to 170,000 kg / hour. This design allows the inlet port From the outlet port 35~200kgf / cm 2 This allows for a pressure drop of the polymer solution At the same time, the temperature of the polymer solution is more than 40° C., preferably more than 50° C., more preferably more than 60° C. The inlet temperature rises from the initial inlet temperature by an amount greater than 1000°C.

[0080] One advantage of this design is that it provides a 14~50kgf / cm2 flow rate from the inlet port to the outlet port. 2 The pressure drop of the polymer solution is reduced by the existing positive displacement pump (gear pump or screw pump) etc.)

[0081] Example 2 This is a comparative example, and is a shell-and-tube heat exchanger with the same fluids and flow rates as the above example. Shell and tube heat exchangers use standard designs and are The liquid flows through the tubes and the medium flows through the shell. Each tube has an inner diameter of 2.0 cm. Each tube is designed with an outer diameter of 2.5cm and a total length of 260cm. The mixing element is packed with twisted tape type mixing elements with an aspect ratio of 1.5. A total of 8,000 tubes are fitted into the 0 cm shell.

[0082] Both the heat transfer and pressure drop calculations for these mixers were calculated using Joshi's method. In this way, the Nusselt number is calculated to be 18.0, and the overall heat transfer coefficient U is 1 15W / m 2 ·K. The total internal heat transfer area of ​​the 8,000 tubes is 1,630 m 2 The UA value of the heat exchanger is 187,450 W / K. The logarithmic mean temperature of this exchanger is The difference is 74°C, and the total heat load is calculated to be approximately 12.7 million watts.

[0083] The pressure drop through the tube is calculated using different correlations and ranges from 60 to 110 kgf / c. m 2 The pressure drop will be in the range of 75 kgf / cm 2 It is. Therefore, the pressure drop is too high for this type of heat exchanger. The outlet pressure of the exchanger must be at least 20kgf / cm 2 Therefore, the total pressure The pressure drop can exceed the capacity of screw pumps or even gear pumps. Therefore, this type of heat exchanger is not suitable for this unit operation.

[0084] To reduce the pressure loss problem, the tube diameter can be increased. However, the pressure required to maintain the same number of tubes in this unit operation is much lower than the Shell S Fewer larger diameter tubes result in increased pressure drop. (faster velocities through them) to provide the heat transfer area required for heat transfer. A longer length is required, which again increases the pressure drop. Therefore, this type Exchangers have inherent limitations in this application.

[0085] The higher pressure drop makes it very difficult to keep the polymer solution in single phase towards the outlet of the exchanger. Once the solution is no longer single-phase but reaches the bubble point, the heat transfer rate decreases, making it difficult to dissolve the solution in the desired form. It becomes very difficult to heat the system to temperatures above 100°C. Furthermore, the system is unpredictable.

[0086] Example 3 This is also a comparative example. If the reactor is placed in a container where the liquid phase separates into two phases, several major problems arise. 1) The polymer solution becomes two-phase inside the channel, which reduces the heat transfer coefficient. 2) The size of this exchanger is too large - the stresses make it impossible to build such a device. The possibility is low. 3) The solution reaches a bubble point in the flat plate heater (FPH) core or at the entrance of the channel, and The heat transfer efficiency is reduced, so the fluid temperature cannot reach 290°C. In addition, the driving force for heat transfer is dramatically reduced at lower fluid temperatures. The examples shown are preferred examples.

[0087] Example 4 This details the use of the device in cooling mode to remove the heat of polymerization from a polymer solution. This is a theoretical example of the present invention. The flat plate cooler has an outer diameter d1 of 282 cm (see FIG. 1). A), the inner diameter d2 is 105 cm, the total height is 370 cm (see Fig. 1A). The exchanger is designed in a cylindrical shell configuration (see Fig. 1). The exchanger comprises several layers. The layers are plated. Each layer of the exchanger has 65 conduits. Each conduit has a diameter of 0.381 cm. The layers are separated by plates that are 0.254 centimeters high. is.

[0088] The banks of tubes carry the fluid and are arranged vertically in layers of the heat exchanger. It contains 65 banks of tubes. Each bank of tubes has an inner diameter of 1.58 cm and an outer diameter of It contains 25 carbon steel tubes, each 1.91 cm in diameter. The wall thickness of each is 1.65 cm. Each channel has an inner perimeter of 2.5 centimeters, an inner width of 11.1 centimeters, and The plate is assembled with a perimeter of 0.381 cm and a height of 0.18 inches. In total, the total number of conduits is 65 per layer, constituting a total of 37,800 conduits.

[0089] Using standard heat transfer calculations of convection through the fluid and conduction across the tube walls, The overall heat transfer coefficient U of this exchanger is U = 73 W / m 2 ·K is calculated as 37,80 The total internal heat transfer area (A) of the ducts is 4,852 m 2 and the product of U×A (UA) values The heat exchanger has a capacity of 354,200 W·K.

[0090] The polyethylene production rate was 22,000 kg / hour and the polyethylene yield was 94.5 kJ / mol. Taking into account the heat of polymerization of ethylene, the required heat removal is calculated to be 21.8 million watts. Assuming the temperature of the solution is 190°C and the average temperature of the cooling liquid is 130°C, the log-average The average temperature difference is 60°C, and the designed exchanger can remove the heat of polymerization.

[0091] The total flow rate through each conduit is approximately 44 kilograms per hour at an average viscosity of 6300 cP. Using standard pressure drop (Bernoulli) calculations, the pressure drop through the exchanger is 3.66 kgf / cm 2 It is calculated as follows.

[0092] definition "Used in reference to the dimensions (such as width or height) or cross-sectional area of ​​a zone within a channel. "Substantially uniform" means that it does not converge or expand at all, or is within 10% of the average of its dimensions. This means that the rates of convergence and / or expansion are within one cent of each other.

[0093] A "polymer" can be any combination of monomers, whether they are of the same type or different types. The general term "poly" refers to a compound prepared by polymerizing monomers, regardless of the type of monomer. "Oligomer" means "oligomer," "homopolymer," "copolymer," "terpolymer," and and "interpolymer."

[0094] An "interpolymer" is a polymer prepared by polymerization of at least two different types of monomers. The general term "interpolymer" refers to a polymer made from a copolymer. (usually used to refer to polymers prepared from two different monomers) and and the term "terpolymer" (usually a polymer prepared from three different types of monomers). It also includes those that are polymerized with four or more types of monomers. Also included are polymers made by combining

[0095] An "oligomer" is a compound that consists of only a few monomer units, such as a dimer, trimer, or tetramer. This refers to a polymer molecule.

[0096] "Bubble point pressure" means the highest pressure at which the first vapor bubbles form at a given temperature. .

[0097] A "polymer solution" is a solution in which the polymer and volatile substances are in a single phase (liquid phase). means a solution comprising

[0098] "Fluid" means a fluid that transfers heat from a source and transfers it to the plates of the device by indirect heat exchange. Suitable thermal fluids include steam, thermal oil, and other heat transfer fluids. For example, The Dow Chemical Company has launched the "DOWTHER These include products sold under the trademark "M(trademark)".

[0099] The viscosity of the solution was measured using Anton Paar Germany GmbH's The measurements were performed using a MCR102 rheometer. The rheometer is equipped with a C-ETD30 0 Electrical system is equipped. Cup and bob type system (combination of concentric cylinders) The 27 mm diameter cup and 25 mm diameter bob are There is a 1mm gap between the two. The bob is at 150 bar (approximately 153 kgf / cm 2 ) pressure It operates in rotational mode within a force cell. Viscosity measurements are taken at a pressure of 30 bar (approximately 31 kgf / c m 2- Nitrogen atmosphere), a certain range of temperatures (150-250°C), a certain range of poly mer concentration (20 to 90 weight percent), a range of shear rates (0.1 to over 100 A few seconds -1 )), and a range of polymer molecular weights (15,000 to 200,000 g / mol). In all cases, the solvent was ExxonMobil's Isop The viscosity measurements obtained ranged from 800 to 2,000,000 centipoise. The range is over 1000.

[0100] Although the present invention has been described with reference to several embodiments, it is understood by those skilled in the art that the scope of the present invention is not limited to the above-mentioned embodiments. Various modifications may be made without departing from the scope of the invention and equivalents may be substituted for its elements. It is understood that certain modifications may be made without departing from the essential scope of the invention. Many modifications may be made to adapt a particular situation or material to the teachings of the invention. The present invention is therefore presented as an embodiment of the present invention as disclosed as the best mode contemplated for carrying out the invention. The present invention is not limited to the specific embodiments, but includes all embodiments falling within the scope of the appended claims. It is intended to include states.

Claims

1. 1. An apparatus for heating or cooling a polymer solution, comprising: an inlet port for introducing a polymer solution into the shell, and the shell having an outlet port for removal of the polymer solution from the shell, the shell comprising a polymer and a solvent acting to dissolve the polymer; The shells are stacked one above the other to define a central passageway in fluid communication with the inlet port of the shell. and further defining a plurality of conduits, each conduit extending radially outward from the central passage. A plurality of plates within the shell, the plurality of conduits being in fluid communication with the central passage. and a plurality of plates for feeding the air into the shell from the inlet port of the shell. The polymer solution is maintained in a single phase during its passage through the device to the outlet port of the filter. An apparatus operated at effective pressures and temperatures.

2. The polymer solution is heated, cooled, or cooled at a constant temperature from the inlet port to the outlet port. The apparatus of claim 1 , wherein:

3. The polymer solution is introduced into the shell from the inlet port into the central passageway, from said outlet through said plurality of conduits and then to said outlet port of said shell.

2. The apparatus of claim 1.

4. The polymer solution is introduced into the shell from the inlet port to the periphery of the shell. from the periphery of the shell through the conduits to the center of the shell, and then to the shell The device of claim 1 , wherein the outlet port is a

5. The temperature of the polymer solution at the inlet port is between 120° C. and 230° C. The pressure of the polymer solution at the inlet port is between 35 and 250 kilograms per square centimeter. The device of claim 1 .

6. The temperature of the polymer solution at the outlet port is between 200° C. and 300° C. The pressure of the polymer solution at the inlet port is between 20 and 200 kilograms per square centimeter. The device of claim 1 .

7. The polymer solution has a shear rate of 100 to 2,000,000 at the shear rate at which the device operates.

10. The device of claim 1 having a solution viscosity of 1000 psi.

8. The apparatus of claim 1 , wherein each conduit has a varying width along its length.

9. The apparatus of claim 1 , wherein each conduit has a constant width along its entire length.

10. Each conduit has an increasing width over a portion of its length, The device of claim 1 having a decreasing width.

11. 2. The method of claim 1, wherein each conduit is in fluid communication with a wall that includes a tube through which the heat transfer fluid is transported. The equipment.

12. The polymer solution exits the outlet port at a temperature lower than the temperature of the inlet port.

13. The apparatus of claim 1 .

13. The polymer solution exits the outlet port at a temperature higher than the temperature of the inlet port.

13. The apparatus of claim 1 .

14. a pump in fluid communication with the device, the pump being disposed upstream of the device and configured to pump the polymer a pump operative to pump a solution through the device; a pressure regulating device disposed downstream of said apparatus to keep said solution in a single phase; The pressure of the polymer solution is reduced to facilitate the conversion of the polymer solution from a single phase to multiple phases. and a pressure regulating device operative to devolatilize or or any one of claims 1 to 13 which functions to promote a reaction in the polymer solution.

13. The device according to claim 12 .

15. The pump is a positive displacement pump and the pressure regulating device is a valve, an orifice, or the like.

15. The degassing device of claim 14, which is a nozzle.

16. an inlet port for introducing a polymer solution into the shell, and a shell having an exit port for removal from the shell; The shells are stacked one on top of the other to define a central passageway in fluid communication with the inlet port of the shell. and further defining a plurality of conduits, each conduit extending radially outward from the central passage. a plurality of plates within the shell, the plurality of conduits being in fluid communication with the central passage; discharging the single-phase polymer solution into an apparatus having a plurality of plates for discharging the single-phase polymer solution; During movement through the device from the inlet port to the outlet port of the shell, operating said apparatus at a pressure and temperature effective to maintain said polymer solution in a single phase; 、 removing the single-phase polymer solution from the outlet port of the apparatus; The temperature of the polymer solution at the outlet port is lower than the temperature of the polymer solution at the inlet port. and removing the material at a temperature equal to, or greater than, the temperature.

17. to facilitate conversion of the single-phase polymer solution to two phases, 17. The method of claim 16, further comprising reducing the pressure of the polymer solution.

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