JP2009051868A - Method and apparatus for treating polymer compound - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method and apparatus for treating a polymer compound, wherein materials are supplied to a reaction vessel at high temperature and high pressure while efficiently applying a pressure to the polymer by an extruder for material supply while preventing backward flow of gas to a hopper on an upstream side of the extruder, so that the polymer compound and a chemical agent are allowed to react with each other. <P>SOLUTION: When the chemical agent is injected into the polymer compound while extruding the polymer compound using the extruder 1 for material supply and a mixture of the polymer compound and the chemical agent is continuously fed into the reaction vessel 100 at high temperature and high pressure and brought into a reaction, a gear pump 30 for pressure increasing is set between the extruder 1 for material supply and the reaction vessel 100, a gear pump 29 for pressure reduction is set at a discharge part of the reaction vessel 100, and the internal pressure of the reaction vessel 100 is regulated by the gear pump 30 for pressure increasing and the gear pump 29 for pressure reduction. <P>COPYRIGHT: (C)2009,JPO&INPIT

Description

  The present invention relates to a method and apparatus for treating a polymer compound by modifying a polymer compound into a modification reaction, a decomposition reaction, a crosslinking point or a molecular chain of a crosslinked polymer to form a thermoplastic resin or wax, and particularly using an extruder. The present invention relates to a novel polymer compound processing method and apparatus for reacting a polymer compound with a drug in a supercritical state.

  In recent years, waste disposal costs are increasing year by year as environmental issues become important. The trend of recycling and recycling is also increasing for polymer compounds. Under these circumstances, research is being conducted on materials and chemical recycling by processing polymers using water, alcohol, carbon dioxide, etc. in high temperature and pressure, supercritical and subcritical conditions.

  In particular, thermosetting resins, cross-linked polymers, elastomers, and the like are difficult to recycle materials because they do not have fluidity even when heated because of a three-dimensional network of molecules. For this reason, in many cases, they are disposed of by landfill, etc., except that some are thermally recycled. For such thermosetting resins and cross-linked polymers, supercritical fluids are used to break down the three-dimensional network structure in the molecule to make it thermoplastic, and to recycle it, or to cut the polymer main chain and reduce the temperature. A method of recycling by waxing by increasing the molecular weight has been studied.

  In order to make such a technique practical, a process of continuously treating a polymer with a supercritical fluid is essential, and it has been proposed that the use of an extruder is suitable for this process.

  For example, in Patent Document 1, crosslinked polyethylene and water are supplied to a material supply extruder, and water is supercritical or subcritical in the material supply extruder, that is, a temperature of 200 to 1000 ° C. and a pressure of 2 to 100 MPa. Shows a method of extruding to a thermoplastic material. In Patent Document 2, a cross-linked polymer is extruded from a material supply extruder and introduced into a reactor together with a high-temperature and high-pressure fluid to produce a reactant, and the reactant is introduced into a separator to separate the reactant into a high-temperature fluid. It is shown that the reaction product is discharged to the outside by a degassing extruder.

JP 2001-253967 A Japanese Patent Laid-Open No. 2002-249618

  However, it is difficult to realize that the pressure is controlled by injecting a large amount of supercritical fluid into one extruder as in Patent Document 1. This is because the pressure of the extruder strongly correlates with the screw rotation speed, that is, the kneading force, and the amount of material supplied. This is because there are parameters indicating contradictory responses, such as a pressure change inside the extruder when the rotational speed is increased in order to promote the above. Moreover, since this method does not show an effective means for maintaining a high pressure, it cannot industrially process a large amount of a thermosetting resin or a crosslinked polymer.

  On the other hand, in Patent Document 2, after mixing the reactive agent and the thermosetting resin, a separation tank for separating the polymer and gas mixture is provided to separate them, and the separation tank is used to maintain a high pressure state. A pressure regulating valve is used upstream of the valve.

  If patent document 2 is utilized, a pressure can be controlled independently of these parameters. However, since the pressure of the extruder is maintained by using the supplied raw material resin as a seal, there is a safety problem that the hopper side seal of the extruder is broken when the raw material supply is stopped. is there.

  That is, this method does not consider a method for preventing a backflow of gas upstream of the material supply extruder. In examining the practical application of the device of Patent Document 2, we have found that depending on the conditions, gas may flow backward to the upstream side of the material supply extruder and may be ejected from the hopper.

  In addition, since there is a limit to the minimum amount of resin necessary for realizing the sealing performance, the operating conditions are also limited. In addition, this method also supplies raw materials while maintaining the resin pressure in the reaction vessel with an extruder, and also performs backflow prevention sealing, so it is used for work other than raw material supply to the reaction vessel, which is the original purpose of use of the extruder The energy of the motor is used, and the energy efficiency of the device is poor.

  In view of the above-described problems, the present invention realizes an apparatus in which a chemical gas does not flow back to a hopper upstream of a material supply extruder when a mixture of a reactive agent and a resin is kneaded in the material supply extruder. At the same time, it has been made by examining various techniques for maximizing the material supply capability of the extruder to the reaction vessel.

  The object of the present invention is to supply the raw materials to the reaction vessel while efficiently applying pressure to the polymer by the extruder while mixing the polymer compound and the drug while preventing the backflow of the hopper gas upstream of the material supply extruder. An object of the present invention is to provide a method and apparatus for treating a polymer compound by reacting the polymer compound with a drug in a high-temperature and high-pressure reaction vessel.

  In order to achieve the above object, the invention of claim 1 is directed to injecting a drug into the polymer compound while extruding the polymer compound using a material supply extruder, and reacting the mixture of the polymer compound and the drug at high temperature and high pressure. In a method of treating a polymer compound by continuously flowing and reacting in a container, a pressure-up gear pump is provided between the material supply extruder and the reaction container, and a pressure-reducing gear pump is provided at the discharge part of the reaction container. The polymer compound treatment method is characterized in that the pressure inside the reaction vessel is adjusted by the pressure-increasing gear pump and the pressure-reducing gear pump.

  The invention according to claim 2 is the polymer compound processing method according to claim 1, wherein the material supply extruder is a single screw extruder.

  Invention of Claim 3 is a processing method of the high molecular compound of Claim 1 or 2 which inject | pours a chemical | medical agent to the front end side of the extruder for material supply.

  Invention of Claim 4 is the processing method of the high molecular compound of Claim 1 or 2 which inject | pours a chemical | medical agent into the reaction container downstream of the gear pump for pressurization.

  A fifth aspect of the present invention is the method according to any one of the first to fourth aspects, wherein a degassing extruder is connected to the subsequent stage of the decompression gear pump, and the drug and the polymer processed product are separated by the degassing extruder. It is a processing method of a molecular compound.

  According to the sixth aspect of the present invention, after separating the drug with a degassing extruder, an impurity separation step of separating the impurity from the drug, and storing the drug from which the impurity has been separated and introducing it into the material supply extruder. It is a processing method of the high molecular compound of Claim 5 which has a chemical | medical agent storage process.

  According to the seventh aspect of the present invention, the degassing extruder has a vent mechanism in order to separate the drug by the degassing extruder, and the vent box connected to the vent mechanism includes a booster gear pump and a decompressor. The method for treating a polymer compound according to claim 5 or 6, wherein the polymer compound has a volume larger than that of a reaction vessel located between gear pumps.

  Invention of Claim 8 is the processing method of the high molecular compound in any one of Claims 1-7 in which the reaction in the said reaction container is either a modification | denaturation reaction, a decomposition reaction, and a bridge | crosslinking cleavage reaction.

  The invention of claim 9 is the method for treating a polymer compound according to any one of claims 1 to 8, wherein the polymer compound is a crosslinked polymer, and the drug is an alcohol or a mixture containing alcohols.

  The invention of claim 10 injects the drug into the polymer compound while extruding the polymer compound using a material supply extruder, and continuously mixes the polymer compound and drug mixture into a high-temperature and high-pressure reaction vessel. In an apparatus for treating a polymer compound by circulating and reacting, a pressure-up gear pump is provided between the material supply extruder and the reaction vessel, and a pressure-reduction gear pump is provided at a discharge portion of the reaction vessel. It is a processing apparatus of a high molecular compound.

  The invention of claim 11 is the polymer compound processing apparatus of claim 10, wherein the material supply extruder is a single screw extruder.

  A twelfth aspect of the present invention is the polymer compound processing apparatus according to the tenth or eleventh aspect, wherein the drug is injected into the tip side of the material supply extruder.

  A thirteenth aspect of the present invention is the polymer compound processing apparatus according to the tenth or eleventh aspect of the present invention, wherein the chemical is injected into a reaction vessel downstream of the pressurizing gear pump.

  A fourteenth aspect of the present invention is the polymer compound processing apparatus according to any one of the tenth to thirteenth aspects, wherein a degassing extruder for separating the drug and the polymer processed product is connected to the subsequent stage of the decompression gear pump. .

  According to the fifteenth aspect of the present invention, the degassing extruder has a vent mechanism in order to separate the drug by the degassing extruder, and the vent box connected to the vent mechanism includes a pressure-up gear pump and a pressure-reducing valve. The polymer compound processing apparatus according to claim 14, which has a volume larger than a volume of a reaction vessel located between gear pumps.

  In the present invention, the material supply and degassing extruder is a device in which a screw is arranged in a cylinder and a polymer such as a synthetic resin or food can be extruded by rotating the screw with the power of a motor. Say.

  In general, industrially used extruders include a twin-screw extruder using two screws, a single-screw extruder using a single screw, and specially a four-screw extruder and other multi-screw extruders. There is a machine. In general, as the number of axes increases, the transmission and cylinder of the extruder have a complicated structure, which is more expensive. On the other hand, an extruder with two or more axes can freely adjust the force applied to the material in the cylinder, so that the pressure distribution in the cylinder can be adjusted freely. Therefore, for example, when trying to seal a drug that is in a gaseous state of high temperature and high pressure with an extruder alone, it is often better to use a twin screw extruder.

  On the other hand, if the backflow of the gaseous drug is sealed using a gear pump, it is not always necessary to select a twin screw extruder. Therefore, in view of the cost of the apparatus, it is preferable to use a single screw extruder.

  The gear pump referred to here is a device having a structure in which a meshed gear closes a resin flow path, and only the resin contained in the groove is conveyed by the gear when the gear rotates. Accordingly, the amount of substance conveyed is determined by the number of rotations of the gear. Since the gears are engaged, there is a possibility that the resin or gas flows backward only through the gaps of the gears. When sealing with a cylinder of an extruder, the groove of the screw is continuously connected, so the flow path through which resin and gas can flow backwards is wide. Compared to this, the gear pump has almost no reverse flow path, and therefore can achieve higher sealing performance than the conventional method.

  The chemical gas discharged from the decompression gear pump is released from the pressure and separated from the resin. Therefore, a degassing extruder is provided after the decompression gear pump to quickly separate the chemical and the polymer-treated product. Is preferred. In addition, in order to remove impurities contained in gaseous chemicals due to differences in boiling point, an impurity separation step is provided to effectively use the thermal energy used for the reaction in the reaction vessel and to purify the chemical. can do.

  In addition, by making the vent box provided in the degassing extruder larger than the reaction vessel, the pressure in the degassing extruder will increase excessively even if the seal of the gear pump for decompression is broken. Can be prevented.

  Such an apparatus can be used to modify, decompose, and crosslink a polymer compound using a supercritical fluid or a high-temperature high-pressure gas. In particular, it can be used as a process technique for thermoplasticizing silane-crosslinked polyethylene with supercritical alcohol.

  Examples of alcohols or mixtures containing alcohols that can be used in the present invention include methyl alcohol, ethyl alcohol, n-propyl alcohol, i-propyl alcohol, n-butyl alcohol, i-butyl alcohol, n-pentyl alcohol, and i. -Pentyl alcohol, ethylene glycol, glycerin, benzyl alcohol, steroid alcohol, etc. can be mentioned. Like the alcohols, phenol having a hydroxyl group, cresol, 2,4,6-tribromophenol, salicylic acid, picrin Phenols such as acid, naphthol, catechol, resorcinol, hydroquinone and pyrogallol can also be used. These may be used alone or in combination of two or more.

  According to the present invention, a pressure increase gear pump is provided at the boundary between the material supply extruder and the reaction vessel, and a pressure reduction gear pump is provided at the discharge portion of the reaction vessel, thereby stabilizing the pressure inside the reaction vessel. As a result, it becomes possible to treat the polymer compound with the supercritical fluid, and it is possible to prevent the back flow of the drug, thereby enabling safer operation.

  A preferred embodiment of the present invention will be described below in detail with reference to the accompanying drawings.

  FIG. 1 is a flowchart showing one embodiment of a cross-linked polyethylene cross-linking treatment apparatus according to the present invention.

  The cross-linked polyethylene pulverized into pellets is fed into the material supply extruder 1 through a hopper 13. The material supply extruder 1 uses a cylinder inner diameter of 50 mm and L / D = 40.

  On the other hand, ethanol used as a drug required for the reaction is supplied from a drug tank 18 through an injection line 21 through a drug tank valve 17 and pressurized by a drug injection pump 15 and heated by a drug heater 14 to supply a material. It is injected from the front end side of the extruder 1 for use. The injection position by the injection line 21 is downstream from the position where the cross-linked polyethylene is pressurized to 1 MPa or more in the material supply extruder 1 and densified, and the length of the pressure part is L / D = 5. It is preferable that this is the case, thereby preventing leakage to the upstream side due to vaporization of the drug, and the polymer and the drug are kneaded in the extruder 1.

  As the material supply extruder 1, a single-screw extruder was used in order to reduce the cost of the extruder and to make it an apparatus capable of withstanding high pressure.

  In the medicine injection pump 15, it is necessary to pressurize more than the pressure of the medicine injection portion in the material supply extruder 1, and the polymer compound heated by the material supply extruder 1 by the medicine heater 14. It is desirable to raise the temperature so that the temperature does not drop. That is, it is desirable to heat the drug to the same level as the temperature of the polymer compound.

  In the material supply extruder 1, the charged cross-linked polyethylene and the injected chemical are mixed and stirred by the screw 1a. At this time, if at least a part of the material supply extruder 1 is brought to a temperature and pressure condition in which the ethanol as a medicine is in a supercritical state, the crosslinked polyethylene and ethanol are sufficiently mixed, and a good polymer processed product is obtained. Is obtained.

  A pressurizing gear pump 30 is connected to the tip of the extruder 1, and a flow-type reaction vessel 100 having a volume of 50 L is connected to the extruder 1 in order to ensure a sufficient reaction time at the subsequent stage. A decompression gear pump 29 is connected to the discharge side of the reaction vessel 100.

  As shown in FIG. 3, the gear pumps 30 and 29 are configured by engaging two gears 33 and 33 in a pump casing 32, and a polymer processed product from the inlet 34 is indicated by an arrow shown in the figure. It is discharged to the outlet 35 while being transferred. By controlling the rotation speed of the gears 33 and 33, the pressure of the polymer compound from the extruder 1 to the flow-type reaction vessel 100 is increased, and from the flow-type reaction vessel 100. The high pressure polymer compound can be discharged under reduced pressure. Thereby, the inside of the flow-type reaction vessel 100 can be maintained at an optimum pressure for performing the reaction (a pressure at which a supercritical state is reached).

  The cross-linked polyethylene polymer processed product plasticized with the material supply extruder 1 and the flow-type reaction vessel 100 and the chemical ethanol mixture are decompressed by the decompression gear pump 29 and discharged to the discharge pipe 36. In order to lower the pressure stepwise, the breaker plate 31 is attached to the pipe 36 as a resistor having a plurality of holes, and the pressure of the resin is reduced stepwise.

  Furthermore, the degassing extruder 2 is connected to the pipe 36, and the viscous liquid polymer processed product is extruded in the discharge direction of the extruder 2 by the screw 2a, and the gas is a back vent mechanism having a low pressure. By flowing into the vent box 8, the polymer processed product and the drug are separated. Here, the vent box 8 is 100 L, twice the volume of the reaction vessel 100.

  The vent box 8 is evacuated by a vacuum pump or a blower 19, whereby the drug is separated from the polymer processed product. At this time, the degassing extruder 2 is formed with a seal zone in which the resin filling rate is 100% between the die 3, the breaker plate 31, and the pipe 36 connecting the degassing extruder 2. The degree of vacuum of the vent box 8 was increased. As a result, the drug is sucked from above the impurity separation tank 16, and one polymer processed product is entangled with the screw 2a and sent to the die 3 of the degassing extruder 2 to be molded. As the degassing extruder 2, a single-screw or twin-screw extruder can be used. Here, a single-screw extruder was used. The die 3 is formed as a strand 5 and cooled and solidified by the cooler 4 below the melting point or softening point of the polymer processed product. The strand 5 becomes a pellet 7 by the strand cutter 6.

  In the degassing extruder 2, a vent may be provided between the die 3 and the pipe 36 connected to the degassing extruder 2 from the breaker plate 31 in order to completely remove the drug from the resin. In that case, it is possible to prevent vents and chemicals from overflowing from the bend box 8 when the vent is provided downstream of the seal zone where the resin filling rate is 100% in the degassing extruder 2. .

  On the other hand, ethanol, which is a chemical separated from the polymer processed product in the vent box 8, is sent to the impurity separation tank 16 through the tank pressure adjusting valve 12. In the impurity separation tank 16, impurities generated during the reaction and mixed in ethanol as a drug are separated based on the difference in boiling point. Ethanol is returned to the drug tank 18 and impurities are sucked by the blower 19 and cooled and recovered by the drug reservoir / condenser 20.

  The apparatus configuration shown in FIG. 1 is particularly effective in the case where the fluidity of the polymer treated product is low and a sufficient reaction time between the polymer treated product and the chemical must be ensured.

  When maintaining the pressure in the reaction vessel with a reaction extruder as in Patent Document 2, if the flow of the polymer compound stops, the alcohol and the polymer processed product will flow into the hopper at once.

  On the other hand, since the pressure is maintained by the gear pump 30 even when the flow of the polymer compound is stopped by using the pressurizing gear pump 30, the backflow of the gaseous chemical or polymer compound in the flow type reaction vessel 100 to the hopper 13 is achieved. Can be prevented.

  The polymer treated product thus obtained can stably supply the liquid polymer treated product and the gaseous chemical agent to the degassing extruder 2 via the decompression gear pump 29, thereby suppressing pressure fluctuations. However, continuous and smooth molding of the polymer processed product becomes possible.

  When such an apparatus is used, the processing amount of the cross-linked polyethylene is 2-100 kg / h per unit time allowed by the discharge capacity of the extruder, and processing by continuous stable operation for 5 hours or more is possible, and the pressure fluctuation range is limited. It was possible to make it within 1 MPa.

  In addition, even when the supply of the material was stopped, the drug and the polymer processed product staying in the reaction vessel 100 did not flow rapidly back to the hopper 13.

  FIG. 2 is a flowchart showing another embodiment of the cross-linked polyethylene cross-linking treatment apparatus according to the present invention.

  In the present embodiment, the injection position of the medicine in the embodiment of FIG. 1 is the flow-type reaction vessel 100 downstream of the pressurizing gear pump 30.

  Such an apparatus configuration is more desirable when emphasizing prevention of the backflow of the drug, whereas the method of the embodiment of FIG. 1 is desirable when emphasizing kneading of the drug and the polymer compound.

  Here, in order to supplement the kneading effect of the extruder, the size of the reaction vessel 100 was set to 60 L, and the residence time that could be maintained at high temperature and high pressure was lengthened. Thus, the polymer compound and the drug can be kneaded using the effect of natural diffusion of the drug instead of the stirring effect of the extruder 1.

  As a result, as in the embodiment of FIG. 1, the processing amount of the cross-linked polyethylene is 2 to 100 kg / h per unit time allowed by the discharge capacity of the extruder, and processing by continuous stable operation for 5 hours or more is possible. It was possible to make the fluctuation range within 1 MPa.

  In addition, even when the supply of the material was stopped, the drug and the polymer processed product staying in the reaction vessel 100 did not flow rapidly back to the hopper 13.

  In FIG. 2, 9 is a vent provided in the degassing extruder 2, and 10 is a vent box heater.

  Next, a comparative example will be described with reference to FIG. 4 with respect to the embodiment shown in FIGS.

  In the apparatus configuration of the comparative example of FIG. 4, the pressure increase gear pump 30 is not provided on the discharge side of the extruder 1, and the pressure reduction gear pump 29 is connected to the discharge side of the flow-type reaction vessel 100.

  As a result, when the supply of the material was stopped, the chemicals and the polymer processed product staying in the reaction vessel 100 abruptly flowed back to the hopper 13 and the operation could not be continued. Moreover, the discharge amount could not be processed at 80 kg / h or more due to the torque limit of the reaction extruder 1.

  From the above results, by providing the pressure increasing gear pump 30 on the discharge side of the extruder 1, it becomes possible to stably treat the polymer compound with the supercritical fluid and to prevent the back flow of the drug, Safer driving is possible.

It is a whole block diagram which shows one Embodiment of the processing apparatus of the high molecular compound of this invention. It is a whole block diagram which shows other embodiment of the processing apparatus of the high molecular compound of this invention. It is a figure which shows the structure of the gear pump shown in FIG. 1, FIG. It is a whole block diagram of the processing apparatus of the high molecular compound as a comparative example.

Explanation of symbols

1 Extruder for material supply
2 Degassing Extruder 3 Dies 4 Cooler 5 Strand 6 Strand Cutter 7 Pellet 8 Vent Box 9 Vent 10 Vent Box Heater 12 Tank Pressure Adjustment Valve 13 Raw Material Hopper 14 Chemical Heating Heater 15 Chemical Injection Pump 16 Impurity Separation Tank 17 Chemical Tank Valve 18 Drug tank 19 Blower 20 Condenser / drug storage tank 29 Pressure reduction gear pump 30 Pressure increase gear pump 31 Breaker plate 100 Flow-type reaction vessel

Claims (15)

  While extruding a polymer compound using a material supply extruder, the drug is injected into the polymer compound, and the mixture of the polymer compound and the drug is continuously circulated into a high-temperature and high-pressure reaction vessel to cause a reaction. In the method for treating a molecular compound, a pressure-up gear pump is provided between the material supply extruder and the reaction vessel, and a pressure-reduction gear pump is provided at the discharge portion of the reaction vessel. The processing method of the high molecular compound characterized by adjusting the pressure of water.   The method for treating a polymer compound according to claim 1, wherein the material supply extruder is a single screw extruder.   The method for treating a polymer compound according to claim 1 or 2, wherein the drug is injected into the leading end side of the material supply extruder.   The method for treating a polymer compound according to claim 1 or 2, wherein the chemical is injected into a reaction vessel on the downstream side of the gear pump for pressurization.   The processing method of the high molecular compound in any one of Claims 1-4 which connect the degassing extruder to the back | latter stage of the gear pump for pressure reduction, and isolate | separate a chemical | medical agent and a polymer processed material with the degassing extruder.   An impurity separation step of separating impurities from the drug after separating the drug by a degassing extruder, and a drug storage step of storing the drug from which the impurities have been separated and introducing the drug into the material supply extruder. 5. A method for treating a polymer compound according to 5.   In order to separate the drug by the degassing extruder, the degassing extruder has a vent mechanism, and a reaction is performed in which the vent box connected to the vent mechanism is located between the pressure boosting gear pump and the pressure reducing gear pump. The processing method of the high molecular compound of Claim 5 or 6 which has a volume larger than the volume of a container.   The method for treating a polymer compound according to any one of claims 1 to 7, wherein the reaction in the reaction vessel is any one of a denaturation reaction, a decomposition reaction, and a crosslinking cleavage reaction.   The method for treating a polymer compound according to any one of claims 1 to 8, wherein the polymer compound is a crosslinked polymer, and the drug is an alcohol or a mixture containing an alcohol.   While extruding a polymer compound using a material supply extruder, the drug is injected into the polymer compound, and the mixture of the polymer compound and the drug is continuously circulated into a high-temperature and high-pressure reaction vessel to cause a reaction. An apparatus for treating a molecular compound, comprising: a pressure increasing gear pump provided between the material supply extruder and the reaction vessel; and a pressure reducing gear pump provided at a discharge portion of the reaction vessel.   The polymer compound processing apparatus according to claim 10, wherein the material supply extruder is a single screw extruder.   The polymer compound processing apparatus according to claim 10 or 11, wherein the drug is injected into a front end side of the material supply extruder.   The apparatus for treating a polymer compound according to claim 10 or 11, wherein the chemical is injected into a reaction vessel downstream of the pressurizing gear pump.   The processing apparatus of the high molecular compound in any one of Claims 10-13 to which the deaeration extruder which isolate | separates a chemical | medical agent and a polymeric processed material is connected to the back | latter stage of the gear pump for pressure reduction.   In order to separate the drug by the degassing extruder, the degassing extruder has a vent mechanism, and a reaction is performed in which the vent box connected to the vent mechanism is located between the pressure increase gear pump and the pressure reduction gear pump. The polymer compound processing apparatus according to claim 14, which has a volume larger than a volume of the container.

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