JP2015120642A - Continuous reaction apparatus, and continuous synthesis method using the same - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a reaction apparatus that can produce a compound with high productivity.SOLUTION: Provided is a continuous reaction apparatus as shown in the figure, comprising: a first raw-material supply part 12; a second raw-material supply part 14; a reaction part 18; and a control part 22 for controlling: the amount of first raw-material supplied to the reaction part from the first raw-material supply part; the amount of second raw-material supplied to the reaction part from the second raw-material supply part; the temperature of first raw-material supplied to the reaction part from the first raw-material supply part; and the temperature of second raw-material supplied to the reaction part from the second raw-material supply part.

Description

  The present invention relates to a continuous reaction apparatus for continuously reacting raw materials and a continuous synthesis method using the same.

  As a mass production technique of a compound produced by synthesis such as an organic compound or a polymer compound, a method of producing in a batch type is common. However, in the batch method, it is necessary to increase the size of the reaction apparatus as a production apparatus in proportion to the amount of the organic compound and polymer compound to be produced. In addition, when synthesizing organic compounds using raw materials that require handling, or when synthesizing polymer compounds using polymerization initiators that require handling such as living anionic polymerization, safety is increased. Since it is necessary to provide a manufacturing apparatus having various mechanisms in consideration, when the main body of the reaction apparatus is enlarged, various mechanisms in consideration of safety are also enlarged and complicated. For this reason, there exists a problem that manufacturing cost, running cost, and maintenance cost increase.

  On the other hand, as a method different from the batch method, a continuous reaction apparatus using a microreactor and a continuous synthesis method using the same have been proposed (see Patent Document 1). For example, Patent Document 1 discloses that a first reaction solution and a second reaction solution are mixed to rapidly raise the temperature or rapidly cool, instantly form a reaction field at a predetermined temperature, and synthesize homogeneous fine particles. A micromixing device having a structure in which the entire micromixing section is installed in a high-pressure resistant jacket capable of circulating a cooling or heating medium is described. As synthesis using such a microreactor, synthesis of silver colloid as metal nanoparticles and synthesis of metal oxide nanoparticles using high-temperature and high-pressure water have been proposed. There are also reports on the high selectivity in the halogen-lithium exchange reaction and the formylation reaction between the generated organolithium and dimethylformamide. However, in the reaction by the microreactor, although the reaction mode is continuous, the flow rate of the raw material to the reactor is several tens to several hundreds mL / h, which is not suitable for mass synthesis. In addition, since the reaction systems that can be used are limited, in a system that involves precipitation of a salt that is insoluble in the reaction system solvent after the reaction, the problem of salt precipitation to the reactor and clogging by this salt has not been solved.

  In addition, as a continuous reaction apparatus and a continuous synthesis method using the same, there is a continuous synthesis using a static stirrer suitable for mass synthesis, particularly a static stirrer, instead of a microreactor (see Patent Documents 2 to 4). . As a continuous synthesis method of an organic compound or an organic metal substance using a static stirrer, Patent Document 2 discloses a continuous reaction of cyanuric acid fluoride and an amine, Patent Document 3 manufactures an aqueous calcium nitrate solution, Patent Reference 4 describes that a hydrolysis reaction of a metal alkoxide is performed.

  As a continuous synthesis method of a polymer compound using a static stirrer, Patent Document 5 describes a continuous production method of a biodegradable polyester polymer, and Patent Document 6 describes a method of producing a lactone copolymer. Patent Document 7 describes a continuous process for producing a polyurethane that can be melt-processed, Patent Document 8 describes a process for continuously producing a polyester-based polymer, and Patent Document 9 describes a process for producing a polyester block copolymer. Yes. Further, as a continuous synthesis method of a polymer compound using a static stirrer and using a polymerization initiator, Patent Document 10 describes a continuous production method of a living cationic polymer, and Patent Document 11 describes a heavy polymer by anionic polymerization. A continuous production method of coalescence is described.

JP 2010-075914 A Japanese Patent Laid-Open No. 8-48896 JP 2008-150244 A JP 2009-274909 A Japanese Patent No. 3309502 Japanese Patent No. 3448927 Japanese Patent No. 4533735 Japanese Patent No. 3590383 JP 2008-7740 A JP 2010-241908 A JP-A-6-56910

  Here, the synthesis described in Patent Documents 2 to 4 is a synthesis example in which any reaction system can react in the atmosphere, and the raw material solution is under strict control of the amount of water and oxygen in the reaction system. It is not a synthesis example with flow rate and temperature control. In particular, there is no precedent for synthesis using a reactive agent that requires attention in handling, such as an organolithium reagent and an organoaluminum reagent.

  In addition, the methods described in Patent Documents 5 to 9 are limited to the production of polyester by bimolecular condensation polymerization and cannot be applied to continuous polymerization using an initiator. In addition, in the methods described in Patent Documents 10 and 11, it is actually difficult to produce a living polymer with controlled molecular weight and degree of dispersion and with good reproducibility.

  In addition, as an example of producing a block copolymer, Patent Document 10 describes a method for producing a living cationic polymer in which an active species during polymerization is a cation. Not manufacturing.

  Thus, there is room for improvement with respect to a method and apparatus for synthesizing a compound by a continuous synthesis reaction using a static stirrer or a so-called static mixer. For example, when synthesizing organic compounds and organometallic compounds using organomagnesium halide reagents, organolithium reagents, organoaluminum reagents, etc., when synthesizing polymer compounds and block polymers by living anion polymerization, it is highly productive. It is desirable to be able to produce compounds.

  This invention is made | formed in view of the above, Comprising: It aims at providing the continuous reaction apparatus which can obtain a reaction material with high productivity, and the continuous synthesis method using this.

  In order to solve the above-described problems and achieve the object, the present invention is a continuous reaction apparatus comprising a first raw material container for storing a first raw material, and the first raw material stored in the first raw material container. A first heat exchanger for exchanging heat between the first supply line to be circulated and the first raw material flowing through the first supply line, and supplying the first raw material heat-exchanged by the heat exchanger; A first raw material supply unit; a second raw material container for storing a second raw material; a second supply line for circulating the second raw material stored in the second raw material container; and the second raw material flowing through the second supply line. A second heat exchanger for exchanging heat with the second raw material supply section for supplying the second raw material heat-exchanged by the heat exchanger, and the first raw material from the first raw material supply section Is continuously supplied, and the second raw material is continuously supplied from the second raw material supply unit. A reaction line to be fed, a static stirrer that statically stirs the first raw material and the second raw material installed in the reaction line and supplied to the reaction line, and the first raw material and the A reaction part that stirs the second raw material to continuously generate a reaction product of the first raw material and the second raw material, and an amount of the first raw material that is supplied from the first raw material supply part to the reaction part And a control unit that controls the temperature and the amount and temperature of the second raw material supplied from the second raw material supply unit to the reaction unit.

  In addition, the continuous reaction apparatus may include other raw material containers for storing other raw materials different from at least one of the first raw material and the second raw material, and other materials for circulating the other raw materials stored in the other raw material containers. A heat exchanger that exchanges heat between the supply line and the other raw material flowing through the other supply line, and another raw material supply unit that supplies the other raw material heat-exchanged by the heat exchanger At least one, the reaction section includes a plurality of the static stirrers, the plurality of static stirrers are connected in series to the reaction line, and the temperature control mechanism is a plurality of the static stirrers The other raw material supply unit is arranged with respect to the most upstream static stirrer, and the other supply line has the reaction between the static stirrer on the upstream side and the static stirrer on the downstream side. The static stirrer connected to the line and upstream The other raw material flowing through the other supply line is supplied to the reaction line through which the reactant to be discharged flows, and the reaction section is discharged from the static agitator on the upstream side by the static agitator on the downstream side. The reaction product and the other raw material are statically stirred to continuously synthesize the reaction product of the reaction product and the other raw material, and the control unit supplies the reaction unit to the reaction unit from the other raw material supply unit It is preferable to control the amount and temperature of the other raw material to be processed.

  In order to solve the above-described problems and achieve the object, the present invention is a continuous reaction apparatus in which two or more kinds of raw materials including at least a first raw material and a second raw material are supplied and supplied. A static stirrer that statically stirs the raw material, and controls the flow rate and temperature at which the raw material is introduced into the static stirrer and the reaction temperature of the static stirrer.

  In order to solve the above-described problems and achieve the object, the present invention is a continuous reaction apparatus in which two or more liquid raw materials including at least a first raw material and a second raw material are supplied and supplied. A static stirrer that statically stirs the above liquid raw material, a mechanism that supplies two or more types of liquid raw materials individually and continuously to the static stirrer, and a reaction product generated by the static stirrer is continuously And a mechanism for discharging out of the system.

  In order to solve the above-described problems and achieve the object, the present invention provides a continuous synthesis method, wherein the first reaction material is supplied from the first raw material supply unit to the reaction unit using the continuous reaction apparatus described above. While adjusting the amount and temperature of one raw material and the amount and temperature of the second raw material supplied from the second raw material supply unit to the reaction unit, the first raw material and the second raw material are continuously added to the reaction unit. And the first raw material and the second raw material supplied to the reaction section are agitated and reacted with the static stirrer, and the resulting reaction product is downstream from the static stirrer. And a step of discharging.

  In order to solve the above-described problems and achieve the object, the present invention provides a continuous synthesis method, wherein the first reaction material is supplied from the first raw material supply unit to the reaction unit using the continuous reaction apparatus described above. While adjusting the amount and temperature of one raw material and the amount and temperature of the second raw material supplied from the second raw material supply unit to the reaction unit, the first raw material and the second raw material are continuously added to the reaction unit. And the first raw material and the second raw material supplied to the reaction section are stirred with the static stirrer while controlling the temperature, and the resulting reaction product is mixed with the upstream static material. The step of discharging downstream from the stirrer and the amount and temperature of the other raw material supplied from the other raw material supply unit to the reaction unit are adjusted, and the other raw material is continuously supplied to the reaction unit. The reactant discharged downstream from the upstream static stirrer Stirring the other raw materials with the downstream static stirrer to cause a synthesis reaction, and performing the process of discharging the obtained reactant from the downstream static stirrer to the downstream side at least once. Is included.

  The continuous reaction apparatus and the continuous synthesis method using the same according to the present invention have an effect that a reactant can be obtained with high productivity. Further, the continuous reaction apparatus and the continuous synthesis method using the same according to the present invention perform precise control of the introduction flow rate and temperature of two or more kinds of raw material solutions, and continuously react the raw materials to perform batch reaction. Compared with the case of synthesis with the corresponding equipment volume equipment, mass production of several tens to several hundred times is possible.

  Furthermore, the continuous reaction apparatus and the continuous synthesis method using the same according to the present invention include an organomagnesium halide reagent, an organolithium reagent, and an organoaluminum reagent that need to be carried out at a very low concentration of water and oxygen in the reaction system. In the synthesis field that uses the above, or when synthesizing organometallic compounds, the mass production efficiency can be improved, the apparatus can be downsized, and the manufacturing cost and maintenance cost of the apparatus can be greatly reduced. it can.

FIG. 1 is a schematic diagram showing a schematic configuration of an embodiment of a continuous reaction apparatus. FIG. 2 is a cross-sectional view showing a schematic configuration of the static stirrer. FIG. 3 is a schematic diagram showing a schematic configuration of an internal element of the static stirrer. FIG. 4 is a schematic diagram showing a schematic configuration of a modified example of the metering pump. FIG. 5 is a schematic diagram showing a schematic configuration of another embodiment of the continuous reaction apparatus. FIG. 6 is a schematic diagram showing a schematic configuration of another embodiment of the continuous reaction apparatus. FIG. 7 is a schematic diagram showing a schematic configuration of another embodiment of the continuous reaction apparatus. FIG. 8 is a schematic diagram showing a schematic configuration of another embodiment of the continuous reaction apparatus. FIG. 9 is an explanatory diagram for explaining the operation of the continuous reaction apparatus.

  Hereinafter, the present invention will be described in detail with reference to the drawings. The present invention is not limited by the following modes for carrying out the invention (hereinafter referred to as embodiments). In addition, constituent elements in the following embodiments include those that can be easily assumed by those skilled in the art, those that are substantially the same, and those in a so-called equivalent range. Furthermore, the constituent elements disclosed in the following embodiments can be appropriately combined.

  Hereinafter, an embodiment of a continuous reaction apparatus will be described with reference to FIGS. 1 to 3. FIG. 1 is a schematic diagram showing a schematic configuration of an embodiment of a continuous reaction apparatus. FIG. 2 is a cross-sectional view showing a schematic configuration of the static stirrer. FIG. 3 is a schematic diagram showing a schematic configuration of an internal element of the static stirrer.

  A continuous reaction apparatus 10 shown in FIG. 1 includes a first raw material supply unit 12 that supplies a first raw material, a second raw material supply unit 14 that supplies a second raw material, a first raw material supply unit 12 and a second raw material supply unit. The first raw material and the second raw material are supplied and supplied from the pressure adjusting unit 16 that supplies gas (inert gas) to 14 and pressurizes the inside of the path, and the first raw material supply unit 12 and the second raw material supply unit 14. The first raw material and the second raw material are statically stirred and chemically reacted to generate a compound, the recovery unit 20 that recovers the compound generated in the reaction unit 18, and the control unit 22 that controls each unit. And having. Here, in the continuous reaction apparatus 10, it is preferable that the atmosphere of the synthesis reaction is an inert gas atmosphere such as argon gas, nitrogen gas, or helium gas. Therefore, in the continuous reaction apparatus 10, it is preferable that the first raw material and the second raw material are stored, the flowing region, the synthesized compound stored region, and the flowing region have an inert gas atmosphere. Moreover, it is preferable that the continuous reaction apparatus 10 forms various mechanisms, a distribution channel, etc. with stainless steel, a fluororesin, etc. Thereby, the continuous reaction apparatus 10 can suppress that each part contaminates a raw material, or each part corrodes. In addition, the continuous reaction apparatus 10 should just be able to suppress the contamination of a raw material and to suppress corrosion of each part, and can be formed with various materials.

  Moreover, the continuous reaction apparatus 10 can use various substances as the first raw material and the second raw material, and can produce various compounds. Further, one of the first raw material and the second raw material may be used as a polymerization initiator for starting the other polymerization reaction of the first raw material and the second raw material. One of the first raw material and the second raw material may be a solution (raw material solution) containing an element and a compound as raw materials. The relationship between the raw material and the compound to be produced will be described later.

  The first raw material supply unit 12 is a mechanism that stores the first raw material and supplies the first raw material to the reaction unit 18. The first raw material supply unit 12 includes a first raw material container 30a, a control valve 31a, a metering pump 32a, a heat exchanger 34a, a mass meter 35a, an upstream pressure sensor 36a, a flow meter 38a, and a downstream side. It has a pressure sensor 40a, an upstream temperature sensor 42a, and a downstream temperature sensor 44a. Each part of the first raw material supply unit 12 is connected by a first supply line La. The first supply line La has one end connected to the first raw material container 30 a and the other end connected to the reaction unit 18. The first supply line La conveys the first raw material stored in the first raw material container 30 a to the reaction unit 18. The first raw material supply unit 12 includes a control valve 31a, a metering pump 32a, an upstream pressure sensor 36a, a flow meter 38a, and the like from the first raw material container 30a to the reaction unit 18 on the path of the first supply line La. The downstream pressure sensor 40a, the upstream temperature sensor 42a, the heat exchanger 34a, and the downstream temperature sensor 44a are arranged in this order.

  The first raw material container 30a is a tank that stores the first raw material. The first raw material container 30a is supplied with an inert gas by a pressure adjusting unit 16 to be described later, and the inside thereof is pressurized. The first raw material container 30a is preferably a tank having a pressure resistance of 0.5 MPa or more and 2 MPa or less. A dip tube 46a is inserted into the first raw material container 30a. One end of the dip tube 46a is disposed near the bottom surface of the first raw material container 30a, and the other end is connected to the first supply line La. The first raw material container 30a discharges the stored first raw material to the dip tube 46a when the internal space is pressurized by a pressure adjusting unit 16 described later. The dip tube 46a is stored in the first raw material container 30a and sends the supplied first raw material to the first supply line La.

  The control valve 31a is disposed on the downstream side of the connection portion between the first supply line La and the first raw material container 30a. The control valve 31a is a valve capable of switching at least opening and closing. When the control valve 31a is in the open state, the first raw material in the first raw material container 30a flows through the first supply line La, and in the closed state, the first raw material in the first raw material container 30a is in the first state. 1 The supply line La is not allowed to flow. The control valve 31a switches whether to supply the first raw material from the first supply line La to the reaction unit 18 or to stop the supply by switching between opening and closing.

  The metering pump 32a is disposed downstream of the control valve 31a of the first supply line La. The metering pump 32a is a mechanism that adjusts the flow rate of the first raw material flowing through the first supply line La. As the metering pump 32a, a double diaphragm pump, a Mono pump, a plunger pump, a triple plunger pump, or the like can be used. As the metering pump 32a, basically, any precise flow rate control can be performed, and various types of pumps can be used. The metering pump 32a adjusts various control parameters such as the number of revolutions to set the flow rate of the first raw material flowing through the first supply line La to a predetermined flow rate.

  The heat exchanger 34a performs heat exchange with the first raw material flowing through the first supply line La. In the heat exchanger 34a of the present embodiment, a refrigerant is circulated as a heat medium that exchanges heat with the first raw material, and the first raw material is cooled by the refrigerant. The heat exchanger 34a adjusts the temperature of the first raw material (the introduction temperature of the first raw material) by adjusting the circulation amount of the refrigerant and adjusting the amount of heat to be exchanged.

  The mass meter 35a measures the mass of the first raw material container 30a. The mass meter 35a can measure the amount of the first raw material stored in the first raw material container 30a by measuring the mass of the first raw material container 30a. A load cell can be used as the mass meter 35a. The upstream pressure sensor 36a is provided on the upstream side of the flow meter 38a of the first supply line La, more specifically, between the metering pump 32a and the flow meter 38a, and the first pressure sensor 36a on the upstream side of the flow meter 38a. The pressure of the first raw material flowing through the supply line La is measured. The flow meter 38a is provided between the metering pump 32a of the first supply line La and the heat exchanger 34a, in the present embodiment, between the upstream pressure sensor 36a and the downstream pressure sensor 40a. The flow rate of the first raw material flowing through one supply line La is measured. As the flow meter 38a, a liquid mass flow meter, an ultrasonic flow meter, a Coriolis flow meter, or the like can be used. The downstream pressure sensor 40a is provided on the downstream side of the flow meter 38a of the first supply line La, more specifically, between the flow meter 38a and the heat exchanger 34a. The pressure of the first raw material flowing through one supply line La is measured. The upstream temperature sensor 42a is provided on the upstream side of the heat exchanger 34a of the first supply line La, more specifically, between the metering pump 32a and the heat exchanger 34a, and on the upstream side of the heat exchanger 34a. The temperature of the first raw material in the first supply line La, that is, the temperature of the first raw material before passing through the heat exchanger 34a is measured. The downstream temperature sensor 44a is provided on the downstream side of the heat exchanger 34a of the first supply line La, more specifically, between the heat exchanger 34a and the reaction unit 18, and downstream of the heat exchanger 34a. The temperature of the first raw material in the first supply line La, that is, the temperature of the first raw material after passing through the heat exchanger 34a is measured. The mass meter 35 a, the upstream pressure sensor 36 a, the flow meter 38 a, the downstream pressure sensor 40 a, the upstream temperature sensor 42 a, and the downstream temperature sensor 44 a send the measurement results to the control unit 22.

  The first raw material supply unit 12 sends the first raw material stored in the first raw material container 30a to the reaction unit 18 through the first supply line La. Here, the first raw material supply unit 12 reacts a predetermined amount of the first raw material by adjusting the flow rate of the first raw material flowing through the first supply line La (the introduction flow rate of the first raw material) with the metering pump 32a. Send to part 18. Further, the first raw material supply unit 12 cools the first raw material flowing through the first supply line La by the heat exchanger 34a, and adjusts the temperature of the first raw material (the introduction temperature of the first raw material). The first raw material having a temperature can be supplied to the reaction unit 18. Here, the flow rate of the first raw material flowing through the first supply line La is preferably 10 ml or more and 20000 ml or less (that is, 10 ml / min or more and 20000 ml / min or less) per minute, and is 100 ml or more and 5000 ml or less (that is, 100 ml / min or less) per minute. More preferably 5000 ml / min or less), and further preferably 500 ml or more and 2000 ml or less per minute (that is, 500 ml / min or more and 2000 ml / min or less). The flow rate is the same for other raw material supply units described later.

  The second raw material supply unit 14 is a mechanism that stores the second raw material and supplies the second raw material to the reaction unit 18. The second raw material supply unit 14 includes a second raw material container 30b, a control valve 31b, a metering pump 32b, a heat exchanger 34b, a mass meter 35b, an upstream pressure sensor 36b, a flow meter 38b, and a downstream side. It has a pressure sensor 40b, an upstream temperature sensor 42b, and a downstream temperature sensor 44b. Each part of the second raw material supply unit 14 is connected by a second supply line Lb. A dip tube 46b is inserted into the second raw material container 30b. The dip tube 46b is connected to the second supply line Lb. Since the second raw material supply unit 14 stores and supplies the second raw material to the reaction unit 18 only different from the first raw material supply unit 12, the basic configuration is the same as that of the first raw material supply unit 12. Description of is omitted.

  The second raw material supply unit 14 sends the second raw material stored in the second raw material container 30b to the reaction unit 18 through the second supply line Lb. Here, the second raw material supply unit 14 reacts a predetermined amount of the second raw material by adjusting the flow rate of the second raw material flowing through the second supply line Lb (the introduction flow rate of the second raw material) with the metering pump 32b. Send to part 18. In addition, the second raw material supply unit 14 cools the second raw material flowing through the second supply line Lb by the heat exchanger 34b, and adjusts the temperature of the second raw material (the introduction temperature of the second raw material), thereby obtaining a predetermined value. A second raw material having a temperature can be supplied to the reaction unit 18.

  The pressure adjusting unit 16 supplies an inert gas to the first raw material container 30a and the second raw material container 30b, pressurizes the insides of the first raw material container 30a and the second raw material container 30b, and adjusts the pressure. And the distribution channel of the 2nd raw material is made into an inert atmosphere. The pressure adjusting unit 16 includes a high-pressure cylinder 50, a gas supply pipe 51, a pressure reducing valve 52, branch pipes 55a and 55b, and gas control valves 56a and 56b.

  The high pressure cylinder 50 is filled with an inert gas. The gas supply pipe 51 is a pipe connected to the high-pressure cylinder 50 and guides the inert gas discharged from the high-pressure cylinder 50. The pressure reducing valve 52 is provided in the gas supply pipe 51 and reduces the pressure of the inert gas flowing through the gas supply pipe 51 to a predetermined pressure or less. The pressure regulator 54 is disposed on the downstream side of the pressure reducing valve 52 of the gas supply pipe 51. The pressure regulator 54 adjusts the pressure of the inert gas that has passed through the pressure reducing valve 52. The pressure adjusting unit 16 is provided with a pressure regulator 54 and flows through the gas supply pipe 51 with the pressure regulator 54 to adjust the pressure of the inert gas, thereby increasing the pressure of the first raw material container 30a and the second raw material container 30b. Can be further stabilized. As the pressure regulator 54, for example, UR-7340 manufactured by HORIBA STEC can be used. As the pressure regulator 54, for example, UR-7340 manufactured by HORIBA STEC Co., Ltd. can be used for more stable pressure regulation. The pressure adjusting unit 16 preferably pressurizes the first raw material container 30a and the second raw material container 30b with a pressure of 2 MPa or less, and more preferably pressurizes with a pressure of 1.5 MPa or less.

  The branch pipe 55a has one end connected to the gas supply pipe 51 and the other end connected to the first raw material container 30a. The branch pipe 55a supplies the inert gas supplied from the gas supply pipe 51 to the first raw material container 30a. The gas control valve 56a is provided in the branch pipe 55a, controls the opening and closing of the branch pipe 55a, and switches whether to supply the inert gas to the first raw material container 30a. The branch pipe 55b has one end connected to the gas supply pipe 51 and the other end connected to the second raw material container 30b. The branch pipe 55b supplies the inert gas supplied from the gas supply pipe 51 to the second raw material container 30b. The gas control valve 56b is provided in the branch pipe 55b and controls opening / closing of the branch pipe 55b to switch whether to supply the inert gas to the second raw material container 30b.

  The pressure adjusting unit 16 supplies the inert gas in the high-pressure cylinder 50 to the first raw material container 30a and the second raw material container 30b via the gas supply pipe 51 and the branch pipes 55a and 55b, so that the first raw material container 30a. And the second raw material container 30b are pressurized and in an inert gas atmosphere. The pressure adjusting unit 16 adjusts the pressure of the first raw material container 30a and the second raw material container 30b by the pressure regulator 54 and the gas control valves 56a and 56b.

  The reaction unit 18 stirs and reacts the first raw material supplied from the first raw material supply unit 12 and the second raw material supplied from the second raw material supply unit 14 to generate a compound. The reaction unit 18 includes a static stirrer 60 that stirs the first raw material and the second raw material, a temperature control mechanism 62 that controls the temperature of the static stirrer 60, an upstream temperature sensor 64, and a downstream temperature sensor 66. Have. The reaction unit 18 further includes a reaction line L1. The reaction line L1 is connected to the first supply line La, the second supply line Lb, and the recovery unit 20. In the reaction unit 18, an upstream temperature sensor 64, a static stirrer 60, and a downstream temperature sensor 66 are arranged in this order from the upstream side in the material flow direction on the reaction line L1.

  The static stirrer 60 is a stirrer without a drive unit, and is a so-called static mixer. As the static agitator 60, a commercially available static agitator can be used. As shown in FIG. 2, the static stirrer 60 includes, for example, a cylindrical tube 90 having an appropriate length, and a plurality of internal elements 92 disposed inside the cylindrical tube 90. The first raw material and the second raw material flow into the cylindrical tube 90. The diameter of the cylindrical tube 90 may be constant or constant depending on the position. As shown in FIG. 3, the internal element 92 is disposed inside the cylindrical tube 90 and is a baffle plate that blocks a part of the cylindrical tube 90. The internal element 92 is a plate inclined with respect to the extending direction of the cylindrical tube 90, and swirls the fluid flowing through the cylindrical tube 90. Thereby, the static stirrer 60 stirs the first raw material and the second raw material. The static stirrer 60 is not particularly limited in the diameter and shape of the pipe, the shape of the filler, and the number of spacer units, as long as two or more kinds of raw materials can be efficiently mixed and stirred. Instead of the internal element 92, a spacer such as a bead or Raschig ring may be filled therein, or a baffle plate may be installed in the pipe. The inner element 92 is not particularly limited, but any of the right element and the left element can be used as the direction of twisting the rectangular plate. The length of the inner element 92 is preferably 1.2 to 2.0 times the inner diameter of the static stirrer 60, but is not limited thereto.

  Here, the flow rate of the liquid material transported in the cylindrical tube 90 is 10 mm to 3000 mm per second (that is, 10 mm / s or more and 3000 mm / s or less), more preferably 200 mm to 2000 mm per second (that is, 200 mm / s or more). 2000 mm / s or less). The static stirrer 60 is preferably one that has a high stirring effect of the internal element 92 and can ensure a flow rate of the raw material solution of a certain level or higher. The cylindrical tube 90 preferably has an inner diameter of 5 mm to 100 mm, and more preferably 10 mm to 50 mm. By setting the inner diameter of the cylindrical tube 90 to 5 mm or more, the flow rate of the first raw material and the second raw material can be set to a predetermined value or more, and the amount of compound produced can be increased. In addition, the cylindrical tube 90 has an inner diameter of 100 mm or less, whereby the two raw materials can be suitably stirred and can be reacted uniformly.

  The temperature control mechanism 62 is disposed on the outer periphery of the static stirrer 60 and controls the temperature of the material flowing through the static stirrer 60. The temperature control mechanism 62 is a pipe outside the double pipe that covers the outer periphery of the static stirrer 60, and performs precise temperature control by allowing the temperature-controlled refrigerant to pass through the outer periphery of the static stirrer 60. The configuration of the temperature control mechanism 62 is not limited to a double tube type. The temperature control mechanism 62 controls the temperature of the object flowing through the static stirrer 60 by exchanging heat with the object flowing through the static stirrer 60. In this embodiment, two raw materials are stirred by the static stirrer 60, and the heated compound is cooled by chemical reaction. Although the temperature of the object controlled by the temperature control mechanism 62 varies depending on the object to be reacted, it is preferably −100 ° C. or higher and + 20 ° C. or lower, more preferably −60 ° C. or higher and −10 ° C. or lower.

  The upstream temperature sensor 64 is provided on the upstream side of the static stirrer 60 in the reaction line L 1, and the temperature of the material in the reaction line L 1 on the upstream side of the static stirrer 60, that is, before passing through the static stirrer 60. Measure the temperature of the material. The downstream temperature sensor 66 is provided on the downstream side of the static stirrer 60 in the reaction line L 1, and after passing through the static stirrer 60, that is, the temperature of the compound in the reaction line L 1 on the downstream side of the static stirrer 60. The temperature of the compound (material) is measured. The upstream temperature sensor 64 and the downstream temperature sensor 66 send the measured results to the control unit 22.

  The static stirrer 60 has a much higher surface area per unit volume than a batch reactor, is easy to cool and heat, and the contents can be efficiently moved in the static stirrer 60, so that the reaction rate is excellent. . Thereby, the reaction part 18 can produce | generate a compound with high productivity. In addition, the reaction can be suitably managed by controlling the temperature in the static stirrer 60 by the temperature control mechanism 62.

  The reaction unit 18 may have an event such that the reaction area of the static stirrer 60 is too small to complete the reaction, or an exotherm during the reaction is too large to cool the reaction solution sufficiently. In this case, the static stirrer 60 may be connected to a plurality of machines in series.

  In addition, in order to complete the reaction, a certain amount of heat may be required. In that case, a plurality of static stirrers 60 are connected in series, and a temperature control mechanism 62 is provided for each of them. Thus, the temperature of the static stirrer 60 may be raised as it goes from upstream to downstream. The temperature control mechanism 62 can adjust the temperature in the range of −10 ° C. or more and 100 ° C. or less, more preferably 0 ° C. or more and 80 ° C. or less, for example.

  The collection unit 20 has a collection container 70. The collection container 70 is a container for storing a compound. The collection container 70 stores the compound discharged from the reaction line L1. The collection container 70 may include a heat exchanger and control the temperature at which the compound is stored.

  The control unit 22 controls the operation of each unit of the continuous reaction apparatus 10. The control unit 22 controls the production of the compound by controlling the flow rate and temperature of the first raw material and the second raw material based on the measurement result of each unit, and controlling the temperature in the reaction unit 18.

  The continuous reaction apparatus 10 is introduced into the static stirrer 60 after precisely controlling the flow rate of the raw material solution such as the first raw material and the second raw material. In the continuous reaction apparatus 10, the flow rate fluctuation error is preferably ± 2% or less, more preferably ± 1% or less, and further preferably ± 0.5% or less.

  The continuous reaction apparatus 10 can precisely control the flow rate of the raw material solution by controlling the flow rates of the first raw material and the second raw material by the metering pumps 32a and 32b, and the flow rate fluctuation error is ± 2% or less, Preferably, it can be suppressed to ± 1% or less, more preferably ± 0.5% or less.

  The continuous reaction apparatus 10 cools the first raw material and the second raw material before being supplied to the static stirrer 60 using the heat exchangers 34a and 34b in advance, and performs temperature control so that the static stirrer 60 is obtained. Even when a rapid chemical reaction occurs and a relatively large amount of reaction heat is generated in a short time, it is possible to prevent the temperature from becoming too high in the static stirrer 60. Thereby, the production | generation time of a compound can be performed suitably with the static stirrer 60. FIG.

  In the continuous reaction apparatus 10, the concentration of the raw material solution such as the first raw material and the second raw material is preferably 0.1 mol / l or more and 10 mol / l or less, and is 0.5 mol / l or more and 3 mol / l or less. It is more preferable.

  Here, the continuous reaction apparatus 10 uses the heat exchangers 34 a and 34 b to cool the first raw material and the second raw material in advance and performs temperature control, but is not limited thereto. The continuous reaction apparatus 10 may control the temperature of the first raw material and the second raw material in advance using the heat exchangers 34a and 34b, and the first raw material and the second raw material using the heat exchangers 34a and 34b. Heating or cooling may be switched according to the first raw material and the second raw material. Further, since the continuous reaction apparatus 10 can suitably control the reaction in the reaction unit 18, a temperature control mechanism 62 is provided corresponding to the static stirrer 60 in the reaction unit 18, and the temperature in the static stirrer 60 is set. Although it is preferable to control, it does not need to provide. These points are the same in other embodiments.

  In the continuous reaction apparatus 10, the pipes for feeding the raw materials such as the first supply line La and the second supply line Lb and the pipes for reacting the raw materials such as the reaction lines L1 have a shape with a small number of bent portions, that is, a layout with many straight lines It is preferable. Thereby, the pressure loss at the time of sending a raw material can be decreased, and the supply amount of the raw material can be controlled with higher accuracy.

  FIG. 4 is a schematic diagram showing a schematic configuration of a modified example of the metering pump. A part including the part connected to the metering pump 32a and the metering pump 32a of the first supply line La shown in FIG. The sealing mechanism 102 has an inert gas atmosphere around the metering pump 32a, and the metering pump 32a is air-sealed. The seal mechanism 102 includes a storage box 104 and an inert gas supply unit 106. The storage box 104 is a box in which the metering pump 32a is disposed. The closed shape has no portion connected to the outside except for the hole into which the first supply line La to which the metering pump 32a is connected is inserted. The storage box 104 closes the hole into which the first supply line La is inserted with a sealing material such as resin or rubber so that there is no gap between the hole and the first supply line La. The storage box 104 may include a check valve that discharges the internal gas to the outside. The storage box 104 seals the metering pump 32a from the atmosphere by sealing the space in which the metering pump 32a is disposed. The inert gas supply unit 106 supplies an inert gas into the storage box 104. The inert gas is nitrogen (N), argon (Ar), or the like.

  The continuous reaction apparatus can seal the metering pump 32a by sealing the metering pump 32a that feeds the raw material with the seal mechanism 102 and setting the region where the metering pump 32a is disposed as an inert gas atmosphere. Here, the metering pump 32a is liquid-sealed so that the raw material does not leak. Therefore, in the continuous reaction apparatus, by providing a sealing mechanism, the outside which is liquid-sealed by various mechanisms for feeding the raw material can be air-sealed by the sealing mechanism, and the mechanism for feeding the raw material can be a double seal. it can. Thereby, it can suppress that a raw material reacts with air | atmosphere, and can perform reaction more safely. Moreover, in the said embodiment, although the seal | sticker mechanism 102 made the area | region where the metering pump 32a is arrange | positioned the inert gas atmosphere, the gas supplied to the inside of a storage box is not limited to an inert gas. The sealing mechanism 102 may be an atmosphere filled with a gas that does not react with the raw material, and a gas other than an inert gas may be used.

  In the above-described embodiment, the metering pump 32a is described as an example, but the metering pump 32b is the same. Further, the present invention is not limited to a metering pump, and various mechanisms for feeding raw materials, for example, a mass flow controller to be described later, are preferably provided with a sealing mechanism. Thereby, the outside which is liquid-sealed by various mechanisms for feeding the raw material can be air-sealed by the sealing mechanism, and the mechanism for feeding the raw material can be a double seal. Thereby, it can suppress that a raw material reacts with air | atmosphere, and can perform reaction more safely.

  Next, another embodiment of the continuous reaction apparatus will be described with reference to FIGS. FIG. 5 is a schematic diagram showing a schematic configuration of another embodiment of the continuous reaction apparatus. Since the continuous reaction apparatus 10a shown in FIG. 5 has the same configuration as that of the continuous reaction apparatus 10 except for a part of the configuration, the same configuration parts as those of the continuous reaction apparatus 10 are denoted by the same reference numerals. Omitted. The continuous reaction apparatus 10a includes a first raw material supply unit 12a for supplying a first raw material, a second raw material supply unit 14a for supplying a second raw material, a gas ( The first raw material and the second raw material are supplied from the pressure adjusting unit 16 that supplies the inert gas) and pressurizes the passage, and the first raw material supply unit 12a and the second raw material supply unit 14a. The raw material and the second raw material are statically agitated and reacted to generate a compound, a recovery unit 18 that recovers the compound generated in the reaction unit 18, and a control unit 22a that controls each unit. .

  The control unit 22a of the continuous reaction apparatus 10a performs feedback control, for example, PID control, on the operation of the metering pump 32a and the opening degree of the control valve 31a based on the measurement result of the flow meter 38a of the first raw material supply unit 12a. Further, the control unit 22a performs feedback control, for example, PID control, on the operation of the metering pump 32b and the opening of the control valve 31b based on the measurement result of the flow meter 38b of the second raw material supply unit 14a.

  The continuous reaction apparatus 10a performs control to reduce the flow rate error by controlling the operation of each part of the first raw material supply unit 12a and the second raw material supply unit 14a based on the measurement results of the flow meters 38a and 38b. Can do. Moreover, in the said embodiment, although it controlled based on the measurement result of the flowmeters 38a and 38b, based on the measurement result of the mass meters 35a and 35b, each part of the 1st raw material supply part 12a and the 2nd raw material supply part 14a was used. Control may be performed, or each part of the first raw material supply unit 12a and the second raw material supply unit 14a may be controlled based on the measurement results of the upstream pressure sensors 36a and 36b and the downstream pressure sensors 40a and 40b. Good. Moreover, the continuous reaction apparatus 10a may control operation | movement of the pressure adjustment part 16 based on a measurement result.

  Although the control part 22a of the continuous reaction apparatus 10a feedback-controls the operation | movement of the metering pumps 32a and 32b and the opening degree of the control valves 31a and 31b, it is not limited to this. The controller 22a may control only the rotation speeds of the metering pump 32a and the metering pump 32b. Thus, by controlling the flow rate only by the rotation speed of the metering pump 32a and the metering pump 32b, it is not necessary to provide the control valves 31a and 31b, and the apparatus configuration can be simplified. In addition, since the control valves 31a and 31b are not provided, the airtightness of the path through which the first raw material and the second raw material flow can be increased with a simple structure. Thereby, there is a low possibility that the gas flows from the outside into the path through which the first raw material and the second raw material flow or the first raw material and the second raw material flow out from the path through which the first raw material and the second raw material flow. It can be manufactured with a simple structure. Moreover, the continuous reaction apparatus 10a can omit the control valves 31a and 31b by controlling the flow rate only by the number of rotations of the metering pump 32a and the metering pump 32b, and eliminates the pressure loss caused by the control valves 31a and 31b. The raw material can be sent efficiently and with high accuracy. The continuous reaction apparatus 10a is preferably provided with various sensors in order to detect an abnormality in the conveyance of the raw material even when the flow rate is controlled only by the rotation speed of the metering pump 32a and the metering pump 32b.

  FIG. 6 is a schematic diagram showing a schematic configuration of another embodiment of the continuous reaction apparatus. Since the continuous reaction apparatus 10b shown in FIG. 6 has the same configuration as the continuous reaction apparatus 10 except for a part of the configuration, the same configuration parts as those of the continuous reaction apparatus 10 are denoted by the same reference numerals. Omitted. The continuous reaction apparatus 10b is configured to supply gas to the first raw material supply unit 12b for supplying the first raw material, the second raw material supply unit 14b for supplying the second raw material, the first raw material supply unit 12b, and the second raw material supply unit 14b. The first raw material and the second raw material are supplied from the pressure adjusting unit 16 that supplies the inert gas) and pressurizes the inside of the path, and the first raw material supply unit 12b and the second raw material supply unit 14b. And a second raw material are statically agitated and reacted to generate a compound, a recovery unit 20 that recovers the compound generated in the reaction unit 18, and a control unit 22 that controls each unit.

  The first raw material supply unit 12 b is a mechanism that stores the first raw material and supplies the first raw material to the reaction unit 18. The first raw material supply unit 12b includes a first raw material container 30a, a control valve 31a, a heat exchanger 34a, a mass meter 35a, an upstream pressure sensor 36a, an upstream temperature sensor 42a, and a downstream temperature sensor 44a. And a flow rate control device 80a. Each part of the first raw material supply unit 12b is connected by a first supply line La.

  The flow rate control device 80a is disposed upstream of the upstream pressure sensor 36a of the first supply line La, that is, between the control valve 31a and the upstream pressure sensor 36a. The flow rate control device 80a is a liquid mass flow controller capable of precisely controlling the flow rate of the first raw material solution, a mechanism for measuring the flow rate of the first supply line La at the installed position, and the first supply line. Both of the mechanisms for adjusting the flow rate of La are provided. The flow control device 80a controls the flow rate of the first supply line La based on the measurement result of the flow rate of the first supply line La. Thereby, the 1st raw material supply part 12b can control the flow volume of the 1st raw material precisely.

  The second raw material supply unit 14 b is a mechanism that stores the second raw material and supplies the second raw material to the reaction unit 18. The second raw material supply unit 14b includes a second raw material container 30b, a control valve 31b, a heat exchanger 34b, a mass meter 35b, an upstream pressure sensor 36b, an upstream temperature sensor 42b, and a downstream temperature sensor 44b. And a flow rate control device 80b. Each part of the second raw material supply unit 14b is connected by a second supply line Lb. The 2nd raw material supply part 14b controls the flow volume of the 2nd raw material which flows through the 2nd supply line Lb with the flow control device 80b.

  The continuous reaction apparatus 10b can control the flow rates of the first raw material and the second raw material with high accuracy by providing flow control devices 80a and 80b instead of the metering pump and the flow meter. Thereby, the continuous reaction apparatus 10b can produce | generate a compound with high productivity by providing flow control device 80a, 80b instead of a metering pump and a flowmeter.

  Here, in each of the above embodiments, the two raw materials, the first raw material and the second raw material, are stirred to produce the compound, but the present invention is not limited to this. The continuous reaction apparatus can produce a compound by stirring and reacting two or more kinds of raw materials. That is, the continuous reaction apparatus can produce a compound by stirring and reacting three or more kinds of raw materials.

  FIG. 7 is a schematic diagram showing a schematic configuration of another embodiment of the continuous reaction apparatus. Since the continuous reaction apparatus 110 shown in FIG. 7 has the same configuration as the continuous reaction apparatus 10 except for a part of the configuration, the same configuration parts as those of the continuous reaction apparatus 10 are denoted by the same reference numerals, Omitted. The continuous reaction apparatus 110 includes a first raw material supply unit 112 that supplies a first raw material, a second raw material supply unit 113 that supplies a second raw material, a third raw material supply unit 114 that supplies a third raw material, A gas (inert gas) is supplied to the fourth raw material supply unit 115 for supplying the raw material, the first raw material supply unit 112, the second raw material supply unit 113, the third raw material supply unit 114, and the fourth raw material supply unit 115. The first raw material, the second raw material, and the third raw material from the pressure adjusting unit 116 that pressurizes the passage, the first raw material supply unit 112, the second raw material supply unit 113, the third raw material supply unit 114, and the fourth raw material supply unit 115. The raw material and the fourth raw material are supplied, and the supplied first raw material, the second raw material, the third raw material, and the fourth raw material are sequentially statically stirred and reacted to generate a compound, and the reactive unit 118 The recovery unit 120 for recovering the compound produced in step 1, and control each unit It has a control section 122, a. The collection unit 120 and the control unit 122 have the same configuration as the collection unit 20 and the control unit 22.

  The configurations of the first raw material supply unit 112, the second raw material supply unit 113, the third raw material supply unit 114, and the fourth raw material supply unit 115 are the same as those of the first raw material supply unit 12 and the second raw material supply unit 14. is there.

  The first raw material supply unit 112 is a mechanism that stores the first raw material and supplies the first raw material to the reaction unit 118. The first raw material supply unit 112 includes a first raw material container 30a, a control valve 31a, a metering pump 32a, a heat exchanger 34a, a mass meter 35a, an upstream pressure sensor 36a, a flow meter 38a, and a downstream side. Pressure sensor 40a. Each part of the first raw material supply unit 112 is connected by a first supply line La. A dip tube 46a is inserted into the first raw material container 30a. The dip tube 46a is connected to the first supply line La. The first supply line La has one end connected to the first raw material container 30 a and the other end connected to the reaction unit 18. The first supply line La conveys the first raw material stored in the first raw material container 30a to the reaction unit 118. In addition, the 1st raw material supply part 112 may further be provided with the upstream temperature sensor and the downstream temperature sensor similarly to the 1st raw material supply part 12. This is the same for the other raw material supply units.

  The second raw material supply unit 113 is a mechanism that stores the second raw material and supplies the second raw material to the reaction unit 118. The second raw material supply unit 113 includes a second raw material container 30b, a control valve 31b, a metering pump 32b, a heat exchanger 34b, a mass meter 35b, an upstream pressure sensor 36b, a flow meter 38b, and a downstream side. Pressure sensor 40b. Each part of the second raw material supply unit 113 is connected by a second supply line Lb. A dip tube 46b is inserted into the second raw material container 30b. The dip tube 46b is connected to the second supply line Lb.

  The third raw material supply unit 114 is a mechanism that stores the third raw material and supplies the third raw material to the reaction unit 118. The third raw material supply unit 114 includes a third raw material container 30c, a control valve 31c, a metering pump 32c, a heat exchanger 34c, a mass meter 35c, an upstream pressure sensor 36c, a flow meter 38c, and a downstream side. Pressure sensor 40c. Each part of the third raw material supply unit 114 is connected by a third supply line Lc. A dip tube 46c is inserted into the third raw material container 30c. The dip tube 46c is connected to the third supply line Lc. Here, in the third raw material supply unit 114, the third supply line Lc is connected to the reaction line L1 at a position downstream of the first supply line La.

  The fourth raw material supply unit 115 is a mechanism that stores the fourth raw material and supplies the fourth raw material to the reaction unit 118. The fourth raw material supply unit 115 includes a fourth raw material container 30d, a control valve 31d, a metering pump 32d, a heat exchanger 34d, a mass meter 35d, an upstream pressure sensor 36d, a flow meter 38d, and a downstream side. And a pressure sensor 40d. Each part of the fourth raw material supply unit 115 is connected by a fourth supply line Ld. A dip tube 46d is inserted into the fourth raw material container 30d. The dip tube 46d is connected to the fourth supply line Ld. Here, in the fourth raw material supply unit 115, the fourth supply line Ld is connected to the reaction line L1 at a position downstream of the third supply line Lc.

  The pressure adjusting unit 116 supplies an inert gas to the first raw material container 30a, the second raw material container 30b, the third raw material container 30c, and the fourth raw material container 30d, and the first raw material container 30a, the second raw material container 30b, Pressurize the inside of the three raw material containers 30c and the fourth raw material container 30d, adjust the pressure, and inactivate the flow path of the first raw material container 30a, the second raw material container 30b, the third raw material container 30c, and the fourth raw material container 30d. Make the atmosphere. The pressure adjusting unit 116 includes a high-pressure cylinder 50, a gas supply pipe 51, a pressure reducing valve 52, branch pipes 55a, 55b, 55c, and 55d, and gas control valves 56a, 56b, 56c, and 56d.

  The branch pipe 55c has one end connected to the gas supply pipe 51 and the other end connected to the third raw material container 30c. The branch pipe 55c supplies the inert gas supplied from the gas supply pipe 51 to the third raw material container 30c. The gas control valve 56c is provided in the branch pipe 55c, controls opening and closing of the branch pipe 55c, and switches whether to supply the inert gas to the third raw material container 30c. The branch pipe 55d has one end connected to the gas supply pipe 51 and the other end connected to the fourth raw material container 30d. The branch pipe 55d supplies the inert gas supplied from the gas supply pipe 51 to the fourth raw material container 30d. The gas control valve 56d is provided in the branch pipe 55d, controls the opening and closing of the branch pipe 55d, and switches whether to supply the inert gas to the fourth raw material container 30d.

  The reaction unit 118 stirs and reacts the first raw material supplied from the first raw material supply unit 112 and the second raw material supplied from the second raw material supply unit 113 to generate an intermediate compound. The reaction unit 118 stirs and reacts with the intermediate compound and the third raw material supplied from the third raw material supply unit 114 to generate another intermediate compound. The reaction unit 118 stirs and reacts with another intermediate compound and the fourth raw material supplied from the fourth raw material supply unit 114 to generate a compound. The reaction unit 118 includes a static stirrer 60a that stirs the first raw material and the second raw material, a static stirrer 60b that stirs the intermediate compound discharged from the static stirrer 60a and the third raw material, and a static stirrer 60b. A static stirrer 60c that stirs another intermediate compound discharged from the fourth raw material, a temperature control mechanism 62a that controls the temperature of the static stirrer 60a, and a temperature control mechanism 62b that controls the temperature of the static stirrer 60b. And a temperature control mechanism 62c for controlling the temperature of the static stirrer 60c. The reaction unit 118 further includes a reaction line L1. The reaction line L1 is connected to the first supply line La, the second supply line Lb, the third supply line Lc, the fourth supply line Ld, and the recovery unit 120. In the reaction unit 118, a static stirrer 60a, a static stirrer 60b, and a static stirrer 60c are arranged in this order from the upstream side in the material flow direction on the reaction line L1. The reaction line L1 is connected to the first supply line La and the second supply line Lb on the upstream side of the static stirrer 60a, and between the static stirrer 60a and the static stirrer 60b, the third supply line Lc is connected. To the fourth supply line Ld between the static stirrer 60b and the static stirrer 60c.

  The static stirrer 60a, the static stirrer 60b, and the static stirrer 60c have the same configuration as the static stirrer 60. The temperature control mechanism 62 a, the temperature control mechanism 62 b, and the temperature control mechanism 62 c have the same configuration as the temperature control mechanism 62.

  The static stirrer 60a stirs and reacts the first raw material supplied from the first raw material supply unit 112 and the second raw material supplied from the second raw material supply unit 113 to generate an intermediate compound. The static stirrer 60b stirs and reacts the intermediate compound generated by the static stirrer 60a and the third raw material supplied from the third raw material supply unit 114 to generate another intermediate compound. The static stirrer 60c stirs and reacts with another intermediate compound and the fourth raw material supplied from the fourth raw material supply unit 115 to generate a compound.

  The continuous reaction apparatus 110 is configured as described above, and a plurality of static stirrers 60a, 60b, and 60c are provided in the reaction unit 118, and two or more kinds of raw materials are suitably mixed by sequentially mixing four kinds of raw materials. It can be made to react continuously. Thereby, the reaction material which made the several raw material react can be produced | generated suitably. Moreover, the continuous reaction apparatus 110 circulates the refrigerant in the temperature control mechanism 62a, the temperature control mechanism 62b, and the temperature control mechanism 62c in the same manner as the temperature control mechanism 62, and cools the material flowing through the static stirrers 60a, 60b, and 60c. However, the present invention is not limited to this, and a part of the temperature control mechanism 62a, the temperature control mechanism 62b, and the temperature control mechanism 62c may be a mechanism that heats the material flowing through the static stirrers 60a, 60b, and 60c. The continuous reaction apparatus 110 may include a static stirrer that does not include a temperature control mechanism among the plurality of static stirrers 60a, 60b, and 60c.

  FIG. 8 is a schematic diagram showing a schematic configuration of another embodiment of the continuous reaction apparatus. Since the continuous reaction apparatus 110a shown in FIG. 8 has the same configuration as the continuous reaction apparatus 110 except for a part of the configuration, the same configuration parts as those of the continuous reaction apparatus 110 are denoted by the same reference numerals. Omitted. The continuous reaction apparatus 110a includes a first raw material supply unit 112a that supplies a first raw material, a second raw material supply unit 113a that supplies a second raw material, a third raw material supply unit 114a that supplies a third raw material, A gas (inert gas) is supplied to the fourth raw material supply unit 115a for supplying the raw material, the first raw material supply unit 112a, the second raw material supply unit 113a, the third raw material supply unit 114a, and the fourth raw material supply unit 115a. The first raw material, the second raw material, and the third raw material are formed from the pressure adjusting unit 116 that pressurizes the path, the first raw material supply unit 112a, the second raw material supply unit 113a, the third raw material supply unit 114a, and the fourth raw material supply unit 115a. The raw material and the fourth raw material are supplied, and the supplied first raw material, the second raw material, the third raw material, and the fourth raw material are sequentially statically stirred and reacted to generate a compound, and the reactive unit 118 Recovery to recover the compound produced in A 120, a control unit 122 for controlling each section, a.

  The first raw material supply unit 112a, the second raw material supply unit 113a, the third raw material supply unit 114a, and the fourth raw material supply unit 115a are the same as the first raw material supply unit 12b and the second raw material supply unit 14b, and the metering pump and the flow rate. Instead of the meter, flow control devices 80a, 80b, 80c, and 80d are provided.

  Similarly to the continuous reaction apparatus 110, the continuous reaction apparatus 110a can produce a compound with high productivity as well as the continuous reaction apparatus 110 by controlling the flow rate with the flow rate control devices 80a, 80b, 80c, and 80d. Moreover, the continuous reaction apparatus 110a can produce a compound with high productivity similarly to the continuous reaction apparatus 110 by feeding back the flow rate based on various measurement results even when three or more kinds of raw materials are reacted. .

  Here, the continuous reaction apparatus has been described as a case where a liquid raw material is used as a raw material to be reacted, but is not limited thereto. In the continuous reaction apparatus, one of the raw materials may be a solid. For the transportation of the solid raw material, it is preferable to use, for example, a combination of a microdisplacer and an ejector of Yoshikawa Corporation. The amount of the solid raw material transported by the micro-discharger is preferably 0.1 ml to 1600 ml / min (that is, 0.1 ml / min to 1600 ml / min), and preferably 0.5 to 160 ml / min (that is, 0.5 ml). / Min to 160 ml / min). The solid raw material is preferably finely divided. Specifically, the solid raw material preferably has particles of 0.001 mm to 5 mm, more preferably 0.01 mm to 0.5 mm. In the continuous reaction apparatus, the solid raw material discharged from the micro-discharger is mixed with a solvent (liquid) and dispersed in an ejector to form a suspension, and is transported to a heat exchanger by a metering pump. At this time, the amount of solvent supplied to the ejector is preferably 200 to 2000 ml / min (that is, 200 to 2000 ml / min). Moreover, in the said embodiment, although the example which makes a 1st raw material and a 2nd raw material react was demonstrated, cooling with various heat exchangers, it is not limited to this. The continuous reaction apparatus can also be used in a configuration in which the first raw material and the second raw material are subjected to a heat exchanger and then reacted in the reaction section.

  The continuous reactors 10, 10a, 10b, 110, and 110a can suitably stir two or more kinds of raw materials by the above-described configuration, and can react the raw materials to generate a compound. Specifically, in a continuous reaction using a static stirrer or so-called static mixer, the introduction flow rate and temperature of a solution containing two or more raw materials are precisely controlled, and the reaction is performed as an inert atmosphere. By setting the concentration of water and oxygen in the system to be extremely low, various compounds can be produced with high productivity.

  The continuous reaction apparatus 10, 10a, 10b, 110, 110a can produce a synthesis (reaction) of an organic compound or an organometallic compound using an organomagnesium halide reagent, an organolithium reagent, an organoaluminum reagent, or the like with high productivity. it can.

  In addition, the outstanding performance of polymers polymerized (reacted) by the living anion polymerization method in the field of electronic materials, synthetic rubber, adhesives, medical materials, and other advanced organic materials utilizing self-composition technology has been highlighted. It is The continuous reaction apparatus 10, 10a, 10b, 110, 110a becomes a continuous polymerization apparatus capable of living polymerization, and is a polymer that is polymerized by a living anion polymerization method by polymerizing using one or more kinds of raw material polymers and a polymerization initiator as raw materials. Can be mass-produced at low cost and high productivity.

  In addition, technological development using diblock and triblock copolymers has attracted attention, and in particular, dot patterns and line patterns formed using block copolymer-specific self-composition technology have been adapted for fine processing. There is a demand for practical industrialization by increasing the density of magnetic disks and increasing the integration of semiconductor integrated circuits. Furthermore, application to the medical field using amphiphilic block copolymers, expansion to electrolyte membranes for solid polymer fuel cells, high value-added adhesives, synthetic rubbers, etc. are also expected. The continuous reaction apparatus 10, 10a, 10b, 110, 110a becomes a continuous polymerization apparatus capable of living anion polymerization, and polymerizes (reacts and synthesizes) using two or more kinds of raw material polymers and a polymerization initiator as raw materials. The polymer can be mass-produced at low cost and high productivity.

  Next, an embodiment of a continuous synthesis method using the above-described continuous reaction apparatus 10, 10a, 10b will be described. In this continuous synthesis method, the amount and temperature of the first raw material supplied from the first raw material supply unit 12 to the reaction unit 18 and the amount and temperature of the second raw material supplied from the second raw material supply unit 14 to the reaction unit 18 are determined. A step of continuously supplying the first raw material and the second raw material to the reaction unit 18 while adjusting, and a static stirrer while controlling the temperature of the first raw material and the second raw material supplied to the reaction unit 18 Agitating at 60, and discharging the resulting reactants from the static agitator 60 downstream.

  First, the control valves 31a and 31b are opened, and the first raw material and the second raw material stored in the first raw material container 30a and the second raw material container 30b pass through the first supply line La and the first through the dip tubes 46a and 46b. 2 flows to the supply line Lb. The amounts of the first raw material and the second raw material that have flowed to the first supply line La and the second supply line Lb are measured as mass reduction amounts of the first raw material container 30a and the second raw material container 30b by the mass meters 35a and 35b. Is done. The controller 22 adjusts the supply amounts of the first raw material and the second raw material based on the measured decrease amounts of the mass of the first raw material container 30a and the second raw material container 30b.

  The first raw material and the second raw material that have flowed through the first supply line La and the second supply line Lb are directed toward the reaction unit 18 by the metering pumps 32a and 32b via the flow meters 38a and 38b and the heat exchangers 34a and 34b. Be transported. Here, the flow rates of the first raw material and the second raw material are measured by the flow meters 38a and 38b, and the first supply line La and the second supply are measured by the upstream pressure sensors 36a and 36b and the downstream pressure sensors 40a and 40b. The pressures of the first raw material and the second raw material on the upstream side and the downstream side of the flow meters 38a and 38b in the line Lb are measured, respectively. The controller 22 adjusts the supply amounts of the first raw material and the second raw material according to the measured pressures of the first raw material and the second raw material.

  The first raw material and the second raw material conveyed to the heat exchangers 34a and 34b are heat-exchanged with the heat medium (for example, refrigerant) in the heat exchangers 34a and 34b, and adjusted to a desired supply temperature. . Here, the temperature of the first raw material and the second raw material on the upstream side and the downstream side of the heat exchangers 34a and 34b is the upstream temperature sensor 42a, provided on the upstream side and the downstream side of the heat exchangers 34a and 34b, respectively. 42b and the downstream temperature sensors 44a and 44b. The control unit 22 adjusts the temperatures of the first raw material and the second raw material supplied to the reaction unit 18 based on the temperatures of the first raw material and the second raw material measured by the downstream temperature sensors 44a and 44b. Further, the control unit 22 adjusts the temperature of the heat doubler in the heat exchangers 34a and 34b based on the temperatures of the first raw material and the second raw material measured by the upstream temperature sensors 42a and 42b, and after the heat exchange. The supply amounts of the first raw material and the second raw material are adjusted so that the first raw material and the second raw material have a desired temperature.

  The 1st raw material and 2nd raw material which were heat-exchanged by heat exchanger 34a, 34b are conveyed to the static stirrer 60 via the reaction line L1. Here, the 1st raw material and 2nd raw material which were adjusted to desired temperature are statically stirred, and the reaction material of a 1st raw material and a 2nd raw material produces | generates. The produced reaction product is collected in the collection container 70. The temperature of the first raw material and the second raw material supplied to the static stirrer 60 is measured by the upstream temperature sensor 64, and the temperature of the reactant is measured by the downstream temperature sensor 66. The control unit 22 controls the temperature in the static stirrer 60 to be in a desired range by a temperature control mechanism 62 provided in the static stirrer 60. Moreover, the control part 22 controls the quantity and temperature of the 1st raw material and 2nd raw material which are supplied to the static stirrer 60 so that the temperature in the static stirrer 60 may become a desired temperature range. In the continuous reaction apparatus 10b, the supply amounts of the first raw material and the second raw material are adjusted by the flow rate control devices 80a and 80b instead of the metering pumps 32a and 32b and the flow meters 38a and 38b.

  As described above, according to the continuous synthesis method according to the above embodiment, the amount and temperature of the first raw material and the second raw material supplied to the reaction unit 18 by the control unit 22 are controlled. The reaction temperature with the two raw materials can be accurately controlled. The first raw material and the second raw material stored in the first raw material container 30a and the second raw material container 30b are continuously supplied from the first supply line La and the second supply line Lb to the static agitator 60 through the reaction line L1. Therefore, contact of the first raw material and the second raw material with the atmosphere can be prevented. Therefore, the reactant can be obtained with high productivity.

  Next, an embodiment of a continuous synthesis method using the above-described continuous reaction apparatuses 110 and 110a will be described. In this continuous synthesis method, the amount and temperature of the first raw material supplied from the first raw material supply unit 30a to the reaction unit 118 and the amount and temperature of the second raw material supplied from the second raw material supply unit 30b to the reaction unit 118 are adjusted. However, the step of continuously supplying the first raw material and the second raw material to the reaction unit 118, and the first raw material and the second raw material supplied to the reaction unit 118 while controlling the temperature, the static stirrer 60a. The step of discharging the obtained reactant from the static stirrer 60a to the downstream side and adjusting the amount and temperature of other raw materials supplied to the reaction unit 118 from the other raw material supply units 30c and 30d, Other raw materials are continuously supplied to the reaction unit 118, and the reactants and other raw materials discharged downstream from the static stirrer 60a are stirred by the static stirrers 60b and 60c while controlling the temperature. The reaction product obtained by static stirrer 60b, 60c Comprising a step of performing at least once the process of discharging the downstream side.

  First, the first raw material and the second raw material are supplied to the static stirrer 60a in the same manner as in the continuous synthesis method using the continuous reaction apparatus 10, 10a, 10b, and a reaction product of the first raw material and the second raw material is generated. . The generation of the reactant is controlled by the control unit 122. In the present embodiment, for convenience of explanation, the upstream temperature sensors 42a and 42b and the downstream temperature sensors 44a and 44b are omitted.

  The control valve 31c is opened, and the third raw material stored in the third raw material container 30c flows to the third supply line Lc via the dip tube 46c. The amount of the third raw material that has flowed to the third supply line Lc is measured by the mass meter 35c as a decrease in the mass of the third raw material container 30c. The control unit 122 adjusts the supply amounts of the first raw material and the second raw material based on the measured decrease amount of the mass of the third raw material container 30c.

  The 3rd raw material which flowed to the 3rd supply line Lc is conveyed toward the reaction part 118 via the flowmeter 38c and the heat exchanger 34c by the metering pump 32c. Here, the flow rate of the third raw material is measured by the flow meter 38c, and the third raw material on the upstream side and the downstream side of the flow meter 38c in the third supply line Lc is measured by the upstream pressure sensor 36c and the downstream pressure sensor 40c. Are measured respectively. The control unit 122 adjusts the supply amount of the third raw material according to the measured pressure of the third raw material.

  The third raw material conveyed to the heat exchanger 34c is heat-exchanged with a heat medium (for example, refrigerant) in the heat exchanger 34c, and adjusted to a desired supply temperature. The control part 122 adjusts the supply amount of the 3rd raw material so that the 3rd raw material after heat exchange may become desired temperature while adjusting the temperature of the heat double in the heat exchanger 34c.

  The 1st raw material and the 2nd raw material which were heat-exchanged by the heat exchanger 34c are conveyed to the static stirrer 60b via the reaction line L1. Here, the reaction product of the third raw material, the first raw material, and the second raw material adjusted to a desired temperature is statically stirred, and the reaction product of the first raw material, the reaction product of the second raw material, and the third raw material is obtained. Generate. The produced reaction product is discharged toward the static stirrer 60c on the downstream side of the reaction line L1. The control unit 122 controls the temperature in the static stirrer 60b to be within a desired range by a temperature control mechanism 62b provided in the static stirrer 60b. Moreover, the control part 122 controls the quantity and temperature of the 3rd raw material supplied to the static stirrer 60b so that the temperature in the static stirrer 60b may become a desired temperature range. In the continuous reaction device 110a, the supply amount of the third raw material is adjusted by the flow rate control device 80c instead of the metering pump 32c.

  Further, the control valve 31d is opened, and the fourth raw material stored in the fourth raw material container 30d flows to the fourth supply line Ld via the dip tube 46d. The amount of the fourth raw material that has flowed to the fourth supply line Ld is measured by the mass meter 35d as a decrease in the mass of the fourth raw material container 30d. The control unit 122 adjusts the supply amounts of the first raw material and the second raw material based on the measured decrease amount of the mass of the fourth raw material container 30d.

  The 4th raw material which flowed to the 4th supply line Ld is conveyed toward the reaction part 118 via the flowmeter 38d and the heat exchanger 34d by the metering pump 32d. Here, the flow rate of the third raw material is measured by the flow meter 38d, and the fourth raw material on the upstream side and the downstream side of the flow meter 38d in the fourth supply line Ld is measured by the upstream pressure sensor 36d and the downstream pressure sensor 40d. Are measured respectively. The control unit 122 adjusts the supply amount of the fourth raw material according to the measured pressure of the fourth raw material.

  The fourth raw material conveyed to the heat exchanger 34d is heat-exchanged with a heat medium (for example, a refrigerant) in the heat exchanger 34d, and adjusted to a desired supply temperature. The control unit 122 adjusts the supply temperature of the first raw material and the second raw material so that the temperature of the heat doubler in the heat exchanger 34c is adjusted and the fourth raw material after the heat exchange has a desired temperature.

  The 4th raw material heat-exchanged by the heat exchanger 34c is conveyed to the static stirrer 60c via the reaction line L1. Here, a reaction product of the fourth raw material, the first raw material, the second raw material, and the third raw material adjusted to a desired temperature is statically agitated to obtain a reaction product of the first raw material, the second raw material, and the third raw material. A reaction product with the fourth raw material is generated. The produced reaction product is discharged from the static stirrer 60c toward the recovery unit 120. The control unit 122 controls the temperature in the static stirrer 60c to be in a desired range by a temperature control mechanism 62c provided in the static stirrer 60c. Moreover, the control part 122 controls the quantity and temperature of the 4th raw material supplied to the static stirrer 60c so that the temperature in the static stirrer 60c may become a desired temperature range. In the continuous reaction apparatus 110a, the supply amounts of the third raw material and the fourth raw material are adjusted by the flow rate control devices 80c and 80d instead of the metering pumps 32c and 32d.

  As described above, according to the continuous synthesis method according to the present embodiment, the amount of the first raw material to the fourth raw material and the temperature supplied to the reaction unit 118 are controlled by the control unit 122, respectively. The reaction temperature of the fourth raw material can be accurately controlled. Further, the first raw material to the fourth raw material stored in the first raw material container 30a to the fourth raw material container 30d are passed through the reaction line L1 from the first supply line La to the fourth supply line Ld, and the static agitators 60a to 60c. Therefore, contact with the atmosphere of the first raw material to the fourth raw material can be prevented. Therefore, the reactant can be obtained with high productivity.

  Hereinafter, compounds that can be produced by the continuous reaction apparatus 10, 10a, 10b, 110, 110a (hereinafter simply referred to as a continuous reaction apparatus), that is, reactants will be exemplified. In addition, when reacting the raw material illustrated below, when the continuous reaction apparatus 10 produces | generates the reaction material illustrated below, since a raw material can be made to react more appropriately, it supplies to a static stirrer (reaction part). It is preferable to control the temperature and flow rate of the raw material, but the continuous reaction device 10 may continuously supply the raw material to a static stirrer, continuously react, and discharge the reactant. Further, the mechanism for supplying the raw material to the static stirrer is not limited to the above embodiment. The continuous reaction apparatus can produce an organic compound or an organometallic compound.

  The continuous reaction apparatus includes at least one of the raw materials, for example, one of the first raw material and the second raw material, one of the first raw material, the second raw material, the third raw material, and the fourth raw material, an organic magnesium halide, an organic lithium, Organoaluminum can be used.

  Moreover, it is also preferable that a continuous reaction apparatus synthesize | combines the raw material from which salt precipitates by reaction by stirring of a static stirrer, and produces | generates a reaction material. As described above, the continuous reaction apparatus has a larger static stirrer than a microreactor or the like, and therefore, even when used for synthesis in which salt is deposited, clogging of a pipeline can be suppressed. Thereby, even when the raw material from which the salt is precipitated is synthesized, the reaction product can be continuously generated.

Moreover, the continuous reaction apparatus can produce | generate the reaction material represented by the following general formula (A).
(R ^A ) ₃ M _A Formula (A)
(In the formula (A), R ^A represents a linear or branched substituted alkyl group or alkoxyalkyl group having 1 to 10 carbon atoms, and M _A represents a Group III metal.)

In the continuous reaction apparatus, a compound represented by the following general formula (B) can be used as one of the first raw material and the second raw material, and a compound represented by the following general formula (C) can be used as the other.
R ^B -Y Formula (B)
M _B (X _A ) Formula ₃ (C)
(In the formulas (B) and (C), R ^B represents a linear or branched substituted alkyl group or alkoxyalkyl group having 1 to 10 carbon atoms, and Y represents lithium or magnesium halide. M _B represents a Group III metal, and X _A represents a halogen atom.

In addition, the continuous reaction apparatus uses a compound represented by the following general formula (D) as one of the first raw material and the second raw material, and a compound represented by the following general formula (E) as the other, A compound represented by the formula (F) can be produced.
R ^C Li Formula (D)
M _C Cl Formula ₃ (E)
(R ^D ) ₃ M _D formula (F)
(In the formulas (D) to (F), R ^C and R ^D each independently represent a methyl group, an ethyl group, a propyl group or a butyl group, and M _C and M _D are each independently a gallium atom or Represents an indium atom.)

  Hereinafter, the organic compound produced | generated with a continuous reaction apparatus is demonstrated more concretely. Although it does not specifically limit as a synthesis | combination of an organic compound, It can use suitably for the synthesis | combination of a system | strain with a quick reaction rate, It can use suitably for the production | generation of the compound synthesize | combined by the following reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by a reaction between a Grineer reagent and an electrophile.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by a reaction between an organolithium reagent and an electrophile.

As shown in the following reaction formula, the continuous reaction apparatus can suitably generate a compound generated by a reaction between an organic sodium compound and carbon dioxide.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by a cyanohydrin production reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by the Wittig reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by a reduction reaction with BH ₃ or the like.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by an oxidation reaction with potassium permanganate or the like.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by the halogenation reaction of alcohol.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by the halogen addition reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by a selective electrophilic addition reaction to a conjugated diene.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by the Diels-Alder reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by the epoxidation reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by halogenation of an aromatic electrophilic substitution reaction (Friedel-Crafts reaction).

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by nitration of an aromatic electrophilic substitution reaction (Friedel-Crafts reaction).

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by acylation of an aromatic electrophilic substitution reaction (Friedel-Crafts reaction).

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by the aldol reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by a reaction (stereoselective reaction) between a lithium enolate reagent and an electrophile.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by enol silyl ether (Mukayama method).

As shown in the following reaction formula, the continuous reaction apparatus can suitably generate a compound generated by the addition reaction of allylsilane.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by the addition reaction of cuprate.

As shown in the following reaction formula, the continuous reaction apparatus can suitably generate a compound generated by a transfer reaction of an epoxy compound.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by the Baeyer-Villiger transfer.

As shown in the following reaction formula, the continuous reaction apparatus can suitably generate a compound generated by a radical substitution reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably generate a compound generated by a radical coupling reaction.

  Here, when the organic compound is synthesized, the temperature of the raw material solution to be used needs to be adjusted according to the organic compound to be produced. Moreover, regarding the supply amount per unit time of the raw material solution to the static stirrer, the whole is preferably 20 L / h or more and 200 L / h or less, and more preferably 30 L / h or more and 100 L / h or less. . By making the supply amount per unit time of the raw material total solution 100 L or more, the production amount per hour can be increased. By setting it as 500 L / h or less, it can suppress that the pressure to a reaction system, especially a static stirrer becomes high, and can suppress that a load is applied to an apparatus and causes a failure. In addition, this supply amount differs depending on the pipe diameter of the static stirrer and needs to be optimized as appropriate.

  Next, the organometallic compound produced | generated with a continuous reaction apparatus is demonstrated. Although it does not specifically limit as a synthesis | combination of an organometallic compound, It can use suitably for the synthesis | combination of a system | strain with a quick reaction rate, and can use it suitably for the production | generation of the compound synthesize | combined by the following reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by organic sodium compound synthesis.

As shown in the following reaction formula, the continuous reaction apparatus can suitably generate a compound generated by organic magnesium compound synthesis.

As shown in the following reaction formula, the continuous reaction apparatus can suitably generate a compound generated by organic lithium compound synthesis.
CH ₃ Cl + Li → CH ₃ Li + LiCl

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by a transmetalation reaction.
C ₆ H ₅ MgBr + B (OCH ₃ ) ₃ → C ₆ H ₅ B (OCH ₃ ) _{2
C 6 H 5 Br + t-} C 4 H 9 Li → C 6 H 5 Li
C ₆ H ₅ Li + ZnCl ₂ → C ₆ H ₅ ZnCl
_{CH 3 OC 6 H 5 + t} -C 4 H 9 Li → o-CH 3 OC 6 H 5 Li
_{o-CH 3 OC 6 H 4} Li + ClSn (n-C 4 H 9) 3 → o-CH 3 OC 6 H 4 Sn (n-C 4 H 9) 3

As shown in the following reaction formula, the continuous reaction apparatus can suitably generate a compound generated by organic zinc compound synthesis.

As shown in the following reaction formula, the continuous reaction apparatus can suitably generate a compound generated by organic samarium compound synthesis.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by a metal-metal exchange reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by an ortho metallization reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by an insertion reaction into a metal-carbon bond.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by a hydrosilylation reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by an insertion reaction into a metal-heteroatom bond.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by an electrophilic substitution reaction.

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by organic group II metal compound synthesis.
ZnCl ₂ + 2CH ₃ MgCl → Zn (CH ₃ ) ₂ + 2MgCl ₂
ZnCl ₂ + 2CH ₃ Li → Zn (CH ₃ ) ₂ + 2LiCl

As shown in the following reaction formula, the continuous reaction apparatus can suitably produce a compound produced by organic group III metal compound synthesis.
GaCl ₃ + 3CH ₃ MgCl → Ga (CH ₃ ) ₃ + 3MgCl ₂
GaCl ₃ + (CH ₃ ) ₃ Al → Ga (CH ₃ ) ₃ + AlCl ₃
GaCl ₃ + 3CH ₃ Li → Ga (CH ₃ ) ₃ + 3LiCl
GaMg + 3CH ₃ I → Ga (CH ₃ ) ₃ + MgI _{2 + 1}
InCl ₃ + CH ₃ MgCl → In (CH ₃ ) ₃ + 3MgCl ₂
InCl ₃ + (CH ₃ ) ₃ Al → In (CH ₃ ) ₃ + AlCl ₃
InCl ₃ + 3CH ₃ Li → In (CH ₃ ) ₃ + 3LiCl

  Here, when the organometallic compound is synthesized, the temperature of the raw material solution to be used needs to be adjusted according to the organometallic compound to be produced. Moreover, regarding the supply amount per unit time of the raw material solution to the static stirrer, the whole is preferably 20 L / h or more and 200 L / h or less, and more preferably 30 L / h or more and 100 L / h or less. . By setting the supply amount per unit time of the raw material total solution to 20 L or more, the production amount per hour can be increased. By setting it as 200 L / h or less, it can suppress that the pressure to a reaction system, especially a static stirrer becomes high, and can suppress that a load is applied to an apparatus and causes a failure. In addition, this supply amount differs depending on the pipe diameter of the static stirrer and needs to be optimized as appropriate.

  As mentioned above, although an organic compound and an organometallic compound were illustrated, this invention is not limited to these illustrated and illustrated chemical structures.

  Next, the high molecular compound produced | generated by continuous living anion polymerization with a continuous reaction apparatus is demonstrated. When a continuous reaction apparatus produces a polymer compound by continuous living anion polymerization, a raw material monomer solution and a polymerization initiator solution are supplied as raw materials and stirred to cause a polymerization reaction (synthesis reaction). A polymer compound is produced. In the continuous living anion polymerization reaction using a static stirrer, the continuous reaction apparatus reduces the amount of water and oxygen in the reaction system to the limit, and the inside of the apparatus after vacuum drying is in a high purity inert gas atmosphere. The flow rates of one or more raw material monomer solutions and polymerization initiator solutions are measured to control each flow rate. For example, the flow rate fluctuation is controlled within ± 1%, and the introduction temperature and polymerization temperature are controlled. It becomes possible. Thereby, the continuous reaction apparatus can produce | generate the high molecular compound produced | generated by continuous living anion polymerization with high productivity.

  Here, the flow control of the raw material monomer and the initiator will be described. According to the method described in Patent Document 11, the monomer solution and the initiator solution whose concentration was adjusted were adjusted only to the flow rate calculated by performing only with the solvent used in advance only by the pressure and pressure feeding method from the argon gas cylinder, and the polymerization was performed. It was possible to do itself. However, in practice, the flow rate of the solvent itself and the flow rate of the adjusted raw material solution and initiator solution actually differ even if the argon gas pressure is set to the same pressure. Deviation occurs with the flow rate. Furthermore, fluctuations in the reaction system pressure including a static stirrer are also added. For this reason, it is difficult to control the fluctuation range of each raw material and the flow rate of the initiator within ± 1%, and the molecular weight (Mw) of the resulting polymer compound is shifted from the target value by ± 10% or more. Also, the degree of dispersion is 1.2 (Mw / Mn) or more, and the value of molecular weight and degree of dispersion is different for each polymerization lot with respect to the reproducibility of polymerization. For this reason, it is difficult to use the liquid feeding means of the apparatus described in Patent Document 11 as the apparatus for commercial mass production.

  In contrast, the continuous reaction apparatus of the present embodiment can measure each flow rate of the raw material monomers and the initiator solution at the time of introducing the static stirrer, and based on the preliminary actual flow rate adjustment result before polymerization. Setting during actual polymerization is possible. Further, the continuous reaction apparatus is provided with a flange pump, preferably a triple plunger pump, as a metering pump for each raw material supply section (liquid feed line). The continuous reaction apparatus can finely adjust the flow rate by measuring with a flow meter at any time during use.

  FIG. 9 is an explanatory diagram for explaining the operation of the continuous reaction apparatus. As shown in FIG. 9, the continuous reaction apparatus of this embodiment can perform stable liquid feeding with little fluctuation when feeding a raw material (raw material monomer solution) at a predetermined flow rate. Thereby, compared with the conventional method, flow control capability can be improved dramatically. With the continuous reaction apparatus of this embodiment, the flow rate fluctuation width of each raw material monomer is preferably controlled within ± 1%, and more preferably within ± 0.5%.

  In the continuous reaction apparatus, the supply amount of the raw material monomer solution to the static stirrer per unit time is preferably 20 L / h or more and 200 L / h or less as a whole, more preferably 30 L / h or more and 100 L / h. preferable. When the supply amount of the raw material monomer solution per unit time is 20 L or more, the production amount per hour can be increased, and by setting it to 200 L / h or less, it is possible to reduce the load on the apparatus and It is possible to suppress the cause. Since the optimum amount of the continuous reactor is different depending on the pipe diameter of the static stirrer, it is preferable to optimize it appropriately.

In the continuous reaction apparatus, the optimum number of mixing elements in the static stirrer varies depending on the viscosity of the reaction solution. Here, the reaction field Reynolds number (Re = ρvD _H / μ: Re = Reynolds number, ρ = fluid density (g / cm ³ ) in the static stirrer for each number of elements, v = flow velocity in the mixer tube (cm / s) ), D _H = mixer pipe inner diameter (cm), μ = solution viscosity (g / cm ³ )) is usually preferably 100 to 500. On the other hand, the continuous reaction apparatus can obtain good reaction efficiency even when the Reynolds number is 1 to 300 in the case of continuous polymerization. This is considered to be achieved by performing polymerization with a high reaction rate by precise control of the flow rate and the reaction temperature. Moreover, a continuous reaction apparatus can obtain more favorable reaction efficiency by making Reynolds number into 20 or more and 300 or less.

  In addition, the continuous reaction apparatus performs preliminary temperature adjustment for each line at the time of liquid feeding in the temperature adjustment bath before introduction of the static stirrer regarding the introduction temperature of each raw material monomer and the polymerization initiator and the control of the polymerization temperature. The temperature can be finely adjusted by measuring each temperature after temperature adjustment. In addition, the temperature between the connected static stirrers and the temperature after flowing out of the static stirrer can be observed and controlled. In the continuous reaction apparatus, the temperature control before and after the polymerization is preferably performed within ± 10 ° C., more preferably within ± 5 ° C.

  The polymerization solvent used in the present invention is an ether solvent, among them diethyl ether, dipropyl ether, diisopropyl ether, dibutyl ether, methyl-t-butyl ether, methylcyclopentyl ether, tetrahydrofuran, furfuryl methyl ether, crown ethers. , Diethylene glycol dimethyl ether, triethylene glycol dimethyl ether, 1,4-dioxane and the like. Examples of the nonpolar solvent include cyclopentane, cyclohexane, methylcyclohexane, benzene, toluene, xylene and the like, and two or more kinds of them may be mixed as a polymerization solvent. The present invention is not limited to these solvents.

  Furthermore, as a polymerization initiator used for living anion polymerization, alkyllithium reagents, especially methyllithium, n-butyllithium, s-butyllithium, t-butyllithium, naphthalenelithium, triphenylmethyllithium, phenyllithium, benzyl Lithium, 1,4-dilithiobutane, 1,4-dilithio-1,1,4,4-tetraphenylbutane and the like can be mentioned. Further, alkyl sodium reagents, naphthalene sodium, triphenylmethyl sodium and the like can be preferably exemplified. Furthermore, lithium methoxide, sodium methoxide, potassium methoxide, lithium ethoxide, sodium ethoxide, potassium ethoxide, sodium isopropoxide and the like can be exemplified depending on the reactivity of the monomer for polymerization. It is not limited to.

（式中Ｒ^１は、炭素数１から１０のアルキル基、炭素数１から１０のアルコキシ基、トリアルキルシリルオキシ基、アルコキシアルキル基、炭素数１から１０のアルコキシカルボニル基、炭素数１から１０のアルコキシカルボニルオキシ基、ハロゲン原子を表し、Ｒ^２は水素原子、またはメチル基を表す。ｍは０から５の整数を表す。） Next, the raw material monomer will be described in detail. As a raw material monomer, the styrene-type monomer shown by a following formula is illustrated suitably.

(Wherein R ¹ is an alkyl group having 1 to 10 carbon atoms, an alkoxy group having 1 to 10 carbon atoms, a trialkylsilyloxy group, an alkoxyalkyl group, an alkoxycarbonyl group having 1 to 10 carbon atoms, or 1 to 10 carbon atoms) And R ² represents a hydrogen atom or a methyl group, and m represents an integer of 0 to 5.)

Examples of R ¹ include a t-butyloxy group and an ethoxyethoxy group as a hydroxy group protector. Other examples include a hydrogen atom, a methoxy group, an ethoxy group, a fluorine atom, a chlorine atom, and a bromine atom.

（式中、Ｒ^３は水素原子、炭素数１から３０のアルキル基、トリアルキルシリル基、アルコキシアルキル基を表し、Ｒ^４、Ｒ^５はそれぞれ水素原子、メチル基、シアノ基、アルコキシカルボニル基、トリアルキルシリル基を示す。） Moreover, as a raw material monomer, the acrylate-type monomer shown by a following formula is illustrated suitably. Styrene monomers are preferably exemplified.

(In the formula, R ³ represents a hydrogen atom, an alkyl group having 1 to 30 carbon atoms, a trialkylsilyl group or an alkoxyalkyl group, and R ⁴ and R ⁵ represent a hydrogen atom, a methyl group, a cyano group, an alkoxycarbonyl group, Represents a trialkylsilyl group.)

R ⁴ and R ⁵ are each preferably a hydrogen atom or a methyl group, and R ³ can be exemplified by a methyl group, an ethyl group, a trimethylsilyl group, and the like. Examples of protectors of acrylic acid and crotonic acid include a t-butyl group, ethoxy group, and the like. An ethyl group is preferably exemplified.

（式中、Ｒ^６、Ｒ^７、Ｒ^８、Ｒ^９はそれぞれ水素原子、炭素数１から１０のアルキル基を表す。） As the raw material monomer, a butadiene-based monomer represented by the following formula is preferably exemplified.

(Wherein R ⁶ , R ⁷ , R ⁸ and R ⁹ each represent a hydrogen atom or an alkyl group having 1 to 10 carbon atoms)

R ⁶ , R ⁷ , R ⁸ and R ⁹ are each preferably a hydrogen atom or a methyl group. Specifically, 1,3-butadiene, isoprene, 2-ethyl-1,3-butadiene, 2,3-dimethyl-1,3-butadiene, 1,3-pentadiene and the like are preferably exemplified.

（式中Ｒ^１０、Ｒ^１１はそれぞれ水素原子、炭素数１から１０のアルキル基、シアノ基、アルコキシカルボニル基を表す。） As a raw material monomer, the acryl-type monomer shown by a following formula is illustrated suitably.

(Wherein R ¹⁰ and R ¹¹ each represent a hydrogen atom, an alkyl group having 1 to 10 carbon atoms, a cyano group, or an alkoxycarbonyl group.)

  Of these, acrylonitrile, dicyanovinyl, dimethoxycarbonylvinyl and the like are preferable. As mentioned above, although the specific monomer was illustrated, this invention is not limited to these.

  Next, the block copolymer produced | generated by continuous living anion polymerization with a continuous reaction apparatus is demonstrated. When producing a block copolymer by continuous living anionic polymerization, the continuous reaction apparatus supplies two or more raw material monomer solutions and a polymerization initiator solution as raw materials and sequentially stirs them, thereby causing a polymerization reaction (synthesis reaction). To produce a block copolymer. The continuous reaction apparatus reduces the amount of water and oxygen in the reaction system to the limit, and the inside of the apparatus after vacuum drying is in a high purity inert gas atmosphere, in a continuous living anion polymerization reaction using a static stirring apparatus, Measure the introduction flow rates of two or more raw material monomer solutions and polymerization initiator solutions, control each flow rate, for example, control the flow rate fluctuation within ± 2%, and control the introduction temperature and polymerization temperature. Can be done. Thereby, the continuous reaction apparatus can produce | generate the block copolymer produced | generated by continuous living anion polymerization with high productivity. About the flow control of a raw material monomer and an initiator, it is the same as that of the case of the high molecular compound mentioned above. The polymerization solvent, polymerization initiator, and raw material monomer used are the same as in the case of the polymer compound described above.

  EXAMPLES Hereinafter, although a synthesis example (polymerization example) and a comparative synthesis example (comparative polymerization example) are shown and this invention is demonstrated concretely, this invention is not restrict | limited to the following synthesis example. First, an example in which an organic compound or an organometallic compound is synthesized using Synthesis Example 1 to Synthesis Example 15 and Comparative Synthesis Example 1 to Comparative Synthesis Example 6 will be described.

[Synthesis Example 1]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) to be used, dehydration purification was performed with CaH ₂ , and an isobutyl magnesium bromide / THF solution (5.0 N) was prepared with isobutyl bromide and Mg metal in the THF solution. A commercially available THF solution (5.0 N) of n-butyraldehyde was prepared.
(Continuous reaction)
After the entire system in the continuous reaction apparatus (hereinafter also simply referred to as “inside apparatus”) was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared isobutylmagnesium bromide solution and n-butyraldehyde solution is filled into a pressure vessel (corresponding to the raw material container of this embodiment), and two triple plunger pumps (corresponding to the metering pump of this embodiment) are filled. The solution was fed to a static stirrer. The raw material solution is measured for flow velocity with a Coriolis flow meter (corresponding to the flow meter), and the pre-reaction solution (raw material) is cooled with a cooling spiral tube (corresponding to the heat exchanger of this embodiment), and then Mixing was carried out by sending the solution to a static stirrer to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min to 0.4 L / min. Regarding the raw material temperature, both solutions were controlled from 0 ° C. to 10 ° C., and this continuous reaction was carried out for 10 hours. The correspondence relationship between the embodiment and the specific configuration of the synthesis example, such as the correspondence between the cooling spiral tube and the heat exchanger of the present embodiment, is the same in the other synthesis examples.
(Post-processing)
The obtained reaction solution is sent to a distillation container (corresponding to the recovery container of the present embodiment) in the apparatus, hydrolyzed (reacted) of alkoxymagnesium bromide with water equal to or more than the reaction equivalent, and then THF. Excess solvent was removed by continuous atmospheric distillation of the solution. By distilling the reaction solution at around 180 ° C., 18.0 kg of 6-methyl-4-octanol was obtained. The yield was 85%.

[Synthesis Example 2]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) to be used, dehydration purification was performed with CaH ₂ , and an allyllithium / THF solution (5.0 N) was prepared from this THF solution and a commercially available THF solution of allyllithium. A commercially available THF solution (5.0N) of methyl isobutyl ketone was also prepared.
(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared allyllithium / THF solution and methylisobutylketone solution were filled in pressure vessels, respectively, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.6 L / min to 0.8 L / min. Regarding the raw material temperature, both solutions were controlled from 0 ° C. to 10 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained reaction solution is sent to a distillation container in the apparatus, and alkoxylithium is hydrolyzed (reaction stopped) using water of a reaction equivalent or higher, and then the atmospheric pressure distillation of the THF solution is continuously performed. The excess solvent was removed. The reaction solution was distilled at around 190 ° C. to obtain 34.6 kg of 2,4-dimethyl-4-octanol. The yield was 82%.

[Synthesis Example 3]
(Preparation of raw material reagents)
In order to reduce the amount of water in tetrahydrofuran (THF) to be used, dehydration purification was performed with CaH ₂ to prepare an Et ₂ AlCN / THF solution (5.0 N) from commercially available Et ₂ AlCN (Nagata Reagent) and this THF solution. did. In addition, a commercially available THF solution (5.0 N) of cyclohexanone was prepared.
(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared Et ₂ AlCN / THF solution and cyclohexanone solution was filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min to 0.4 L / min. Regarding the raw material temperature, both solutions were controlled from 15 ° C. to 25 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The resulting reaction solution is sent to a distillation vessel in the apparatus, and alkoxydiethylaluminum is hydrolyzed (stops reaction) at -10 ° C. or lower using water of a reaction equivalent or higher, followed by atmospheric distillation of the THF solution. Was carried out continuously to remove excess solvent. By distilling the reaction solution at around 180 ° C., 15.0 kg of 1-cyanocyclohexyl alcohol was obtained. The yield was 78%.

[Synthesis Example 4]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) to be used, dehydration purification was performed with CaH ₂ , and a THF solution (5. 0N) was prepared. A commercially available THF solution (5.0 N) of n-butyraldehyde was also prepared.

(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared (methoxymethyl) triphenylphosphonium chloride solution and n-butyraldehyde solution was filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.6 L / min to 0.8 L / min. Regarding the raw material temperature, both solutions were controlled from 20 ° C. to 25 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained reaction solution was sent to a distillation vessel in the apparatus, and atmospheric distillation of the THF solution was continuously performed to remove excess solvent. By distilling the reaction solution at around 125 ° C., 25.9 kg of 1-hexenyl methyl ether was obtained. The yield was 73%.

[Synthesis Example 5]
(Preparation of raw material reagents)
In order to reduce the amount of water in tetrahydrofuran (THF) to be used, dehydration purification was performed with CaH ₂ to prepare a 5.0 N solution from a commercially available borane / THF solution. A commercially available THF solution (5.0 N) of cyclohexanone was also prepared.
(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere.
The borane / THF solution and the cyclohexanone solution prepared above were each filled into a pressure vessel and fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.4 L / min to 0.6 L / min. Regarding the raw material temperature, both solutions were controlled from −10 ° C. to 0 ° C., and this continuous reaction was performed for 10 hours.
(Post-processing)
The obtained reaction solution is sent to a distillation vessel in the apparatus, and alkoxyborane is hydrolyzed (stops the reaction) using hydrogen peroxide solution of a reaction equivalent or more, followed by continuous atmospheric distillation of the THF solution. Excess solvent was removed by performing. By distilling the reaction solution at around 160 ° C., 26.9 kg of cyclohexanol was obtained. The yield was 88%.

[Synthesis Example 6]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) to be used, dehydration purification was performed with CaH ₂ , and a PBr ₃ / THF solution (5.0 N) was prepared from commercially available tribromophosphine and this THF solution. A mixed THF solution (5.0 N / 6.0 N) was prepared from commercially available cyclohexanol and commercially available pyridine.
(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared tribromophosphine solution and cyclohexanol / pyridine mixed solution was filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.6 L / min to 0.8 L / min. Regarding the raw material temperature, both solutions were controlled from −10 ° C. to −5 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained reaction solution was sent to a distillation vessel in the apparatus, and atmospheric distillation of the THF solution was continuously performed to remove excess solvent. By distilling the reaction solution at around 167 ° C., 35.9 kg of bromocyclohexene was obtained. The yield was 72%.

[Synthesis Example 7]
(Preparation of raw material reagents)
In order to reduce the amount of water in tetrahydrofuran (THF) to be used, dehydration purification was performed with CaH ₂ , and a cyclohexene / THF solution (1.0 N) was prepared from commercially available cyclohexene and this THF solution. A commercially available hydrogen chloride gas cylinder was also prepared.
(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared cyclohexene solution was filled in a pressure vessel, and the solution was fed to a static stirrer using a triple plunger pump. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. On the other hand, hydrogen chloride gas was also connected to a static stirrer, and the gas flow rate was controlled by a gas flow meter. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rate of the solution was adjusted to 0.1 L / min to 0.3 L / min, and the hydrogen chloride gas flow rate was adjusted to 4 L / min to 5 L / min. The raw material temperature was controlled from −10 ° C. to 0 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained reaction solution was sent to a distillation vessel in the apparatus and distilled at around 142 ° C., whereby 9.8 kg (yield 95%) of chlorocyclohexene was obtained.

[Synthesis Example 8]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene to be used, dehydration purification is carried out with molecular sieves, and commercial cyclohexane and t-butylcumyl peroxide (manufactured by Kayabutyl C Kayaku Akzo) are mixed and dissolved in this benzene solution. Were 5.0N and 0.5N, respectively. In addition, a commercially available toluene solution (5.0 N) of thionyl chloride was prepared.
(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared cyclohexane and t-butyl cumyl peroxide mixed solution and thionyl chloride solution were filled in a pressure vessel, respectively, and the solution was fed to a static stirrer using two triple plunger pumps. The raw material solution was measured for flow rate with a Coriolis flowmeter, the pre-reaction solution was heated with a spiral tube (for heating), then sent to a static stirrer, the static stirrer itself was also heated, and the introduced solution was mixed and continuously The reaction was carried out. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min to 0.4 L / min. Regarding the raw material temperature, both solutions were controlled from 50 ° C. to 60 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained reaction solution is sent to a distillation vessel in the apparatus, and an excess organic peroxide is decomposed using a peroxide decomposer (phenyl-β-naphthylamine diphenylamine), followed by atmospheric distillation of the toluene solution. By performing continuously, excess solvent was removed. By distilling the reaction solution at around 180 ° C., 11.8 k of chlorocyclohexane was obtained. The yield was 65%.

[Synthesis Example 9]
(Preparation of raw material reagents)
In order to reduce the amount of water in the diethyl ether used, dehydration purification was performed with CaH ₂ to dissolve allyltriphenyltin to prepare a 5N diethyl ether solution. Moreover, phenyl lithium (5.5N) was prepared. The raw material mole was set to be allyltriphenyltin: PhLi = 1: 1.1.
(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared phenyllithium solution and allyltriphenyltin solution were filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.6 L / min to 0.8 L / min. Regarding the raw material temperature, both solutions were controlled from -30 ° C to -20 ° C. This continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained reaction solution was sent to a filled container and diethyl ether was continuously distilled at atmospheric pressure to remove excess solvent, and about 33 kg of a mixed solution of allyllithium was obtained. The reaction yield from normality measurement was 88%.

[Synthesis Example 10]
(Preparation of raw material reagents)
In order to reduce the amount of water in use, dehydration purification was performed with CaH ₂ , and an allylmagnesium bromide / diethyl ether solution (5.5 N) was prepared from allyl bromide and Mg metal in the diethyl ether solution. Further, nBuSnCl ₃ was dissolved in dehydrated diethyl ether to prepare a 5N nBuSnCl ₃ / diethyl ether solution. The reaction molar ratio by raw material was set to nBuSnCl ₃ : allyl lithium = 1: 3.3.
(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere.
The allyl lithium solution and the nBuSnCl ₃ solution prepared above were filled in pressure vessels, respectively, and fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.6 L / min to 0.8 L / min. Regarding the raw material temperature, both solutions were controlled from -5 ° C to -10 ° C. This continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained reaction solution was sent to a distillation vessel in the apparatus, and atmospheric distillation of diethyl ether was continuously performed to remove excess solvent. Furthermore, 64.8 kg of triallylbutyltin was obtained by distilling this mixed solution under reduced pressure to about 0.2 mmHg and at around 90 ° C. The yield was 64%.

[Synthesis Example 11]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ , and a PhLi / THF solution (5.5 N) was prepared using a commercially available phenyl lithium reagent and this THF solution. In addition, a commercially available solution of SnCl ₂ in THF (5.0 N) was prepared.
(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere.
The phenyl lithium solution and SnCl ₂ solution prepared above were filled in pressure vessels, respectively, and fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.6 L / min to 0.8 L / min. Regarding the raw material temperature, both solutions were controlled from 0 ° C. to 10 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained reaction solution was sent to a distillation vessel in the apparatus, and an excess solvent was removed by performing atmospheric distillation of the THF solution. By distilling the reaction solution at around 190 ° C., 57.8 kg (yield 82%) of PhSnCl was obtained.

[Synthesis Example 12]
(Preparation of raw material reagents)
In order to reduce the amount of water in the diethyl ether used, dehydration purification was performed with CaH ₂ , zinc chloride was dissolved in the diethyl ether, and a 5N ZnCl ₂ / diethyl ether solution was prepared. Further, an ethyl lithium / diethyl ether solution (2.8N) (manufactured by Kemetal Co., Ltd.) was prepared. The reaction molar ratio by raw material was set to ZnCl ₂ : CH ₃ CH ₂ Li = 1: 2.2.
(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared ethyllithium solution and zinc chloride solution was filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.6 L / min to 0.8 L / min. Regarding the raw material temperature, both solutions were controlled from -5 ° C to -10 ° C. This continuous reaction was carried out for 10 hours.
(Post-processing)
The resulting reaction solution was sent to a distillation vessel in the apparatus, and atmospheric distillation of diethyl ether was continuously performed to remove excess solvent. Then, 32.4 kg of diethylzinc was obtained by heating and distillation separation at 117 ° C. The yield was 81%.

（連続反応）
まず、装置内の系全体を真空乾燥させた後、反応は高純度アルゴン雰囲気下で行った。
前記で準備した上記式の１−オクテンとＦｅ触媒溶液とトリエチルシラン溶液をそれぞれ圧力容器に充填、２台のトリプルプランジャーポンプを用いて静的攪拌機への送液を行った。原料溶液はコリオリ流量計で流速の測定が行われ、冷却用のスパイラル管で反応前溶液を冷却、その後静的攪拌機へ送液、混合され連続反応を実施した。また、原料の温度管理は、静的攪拌機の上流側、及び連結された静的攪拌機間に装備されている温度センサを用いて行った。両原料溶液の流速は０．３Ｌ／ｍｉｎ〜０．４Ｌ／ｍｉｎに調整した。原料温度に関しては、両溶液ともに１０℃から２５℃に制御し、この連続反応を１０時間行った。
（後処理）
得られた反応溶液は、本装置内の蒸留容器に送液、続いてＴＨＦ溶液の常圧蒸留を連続で行うことで、余分な溶剤を除去した。この反応溶液を１８０℃付近で蒸留することで、トリエチルノニルシランが３２．１ｋｇ得られた。収率は、９２％であった。 [Synthesis Example 13]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ , and commercially available 1-octene and an Fe catalyst (see the following formula) were dissolved in this THF solution, and 1-octene, Fe A catalyst / THF solution (5.0 N, 0.1 N) was prepared. Further, a commercially available THF solution (5.0 N) of triethylsilane was prepared.

(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere.
The above-prepared 1-octene, Fe catalyst solution and triethylsilane solution prepared in the above were filled in a pressure vessel and fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min to 0.4 L / min. Regarding the raw material temperature, both solutions were controlled from 10 ° C. to 25 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained reaction solution was sent to a distillation container in the apparatus, and then the atmospheric solvent was continuously distilled to remove excess solvent. This reaction solution was distilled at around 180 ° C. to obtain 32.1 kg of triethylnonylsilane. The yield was 92%.

[Synthesis Example 14]
(Preparation of raw material reagents)
A commercially available rhodium chloride trihydrate was dissolved in an ethanol solution to prepare a RhCl ₃ / EtOH solution (1.0 N). A commercially available ethanol solution (3.0 N) of triphenylphosphine was also prepared.
(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared RhCl ₃ / EtOH solution and triphenylphosphine solution was filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.05 L / min to 0.15 L / min. Regarding the raw material temperature, both solutions were controlled from 70 ° C. to 75 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained reaction solution was sent to a distillation vessel in the apparatus, and then an ethanol solution was subjected to atmospheric distillation to remove excess solvent. By separately purifying the reaction solution, 15.3 kg of Wilkinson's catalyst (see the following formula) was obtained. The yield was 38%.

[Synthesis Example 15]
(Preparation of raw material reagents)
To reduce the water content of the diethyl ether used performs dehydrated purified by CaH _2, dissolved GaCl 3 40.2 g, was prepared diethyl ether solution of GaCl ₃ of 5N. Further, a methyllithium / diethyl ether solution (1.5N) (manufactured by Kemetal Co., Ltd.) was prepared. The reaction molar ratio by raw material was set to GaCl ₃ : CH ₃ Li = 1: 3.3.
(Continuous reaction)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared methyllithium solution and gallium trichloride solution was filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.6 L / min to 0.8 L / min. Regarding the raw material temperature, both solutions were controlled from -5 ° C to -10 ° C. This continuous reaction was carried out for 10 hours.
(Adduct replacement)
The resulting reaction solution was sent to a distillation vessel in the apparatus, and atmospheric distillation of diethyl ether was continuously performed to remove excess solvent. Next, triphenylphosphine / tetraethylene glycol dimethyl ether (molar ratio 1: 1.5) was injected into the obtained reaction solution. The mixed solution was subjected to vacuum distillation near room temperature, whereby diethyl ether coordinated to trimethylgallium was subjected to adduct exchange with triphenylphosphine. The obtained exchange solution was heated and distilled at 80 ° C. to obtain 29.8 kg of trimethylgallium. The yield was 80%.

[Comparative Synthesis Example 1]
(Preparation of raw material reagents)
In order to reduce the amount of water in tetrahydrofuran (THF) to be used, dehydration purification was performed with CaH ₂ , and an isobutyl magnesium bromide / THF solution (2.0 N) was prepared with isobutyl bromide and Mg metal in the THF solution. In addition, a commercially available THF solution (2.0 N) of n-butyraldehyde was prepared.
(Batch reaction)
A 10 L reaction vessel corresponding to the same volume as that required for installing the continuous reaction apparatus of this example was vacuum dried, and then the reaction was performed in a high purity argon atmosphere. Next, 3 L of the prepared n-butyraldehyde / THF solution was introduced into the reaction vessel, cooled to −10 ° C., and then 3 L of isobutyl magnesium bromide solution was injected over 3 hours. At this time, care was taken so that the internal temperature of the reaction did not exceed 0 ° C. After completion of the injection, the reaction vessel was further warmed to room temperature and further reacted for 7 hours.
(Post-processing)
The obtained reaction solution was subjected to hydrolysis (reaction stop) of alkoxymagnesium bromide using 1 L of water, followed by atmospheric distillation of the THF solution to remove excess solvent. The reaction solution was separated and washed with a butyl acetate / water system, excess ethyl acetate in the upper ethyl acetate layer was removed by atmospheric distillation, and the concentrated solution was distilled at around 180 ° C. to give 6-methyl-4 -0.63 kg of octanol was obtained. The yield was 92%.

[Comparative Synthesis Example 2]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) to be used, dehydration purification was performed with CaH ₂ , and an allyllithium / THF solution (2.0 N) was prepared from this THF solution and a commercially available THF solution of allyllithium. A commercially available THF solution (2.0 N) of methyl isobutyl ketone was also prepared.
(Batch reaction)
A 10 L reaction vessel corresponding to the same volume as that required for installing the continuous reaction apparatus of this example was vacuum dried, and then the reaction was performed in a high purity argon atmosphere. 3 L of the allyllithium / THF solution prepared above was introduced into the reaction vessel and cooled to −10 ° C., and then 3 L of methyl isobutyl ketone / THF solution was injected over 5 hours. At this time, care was taken so that the internal temperature of the reaction did not exceed 10 ° C. After completion of the injection, the reaction vessel was further warmed to room temperature and reacted for another 5 hours.
(Post-processing)
The obtained reaction solution was subjected to hydrolysis (reaction stop) of alkoxylithium using 1 L of water, followed by atmospheric distillation of the THF solution to remove excess solvent. This reaction solution was separated and washed with a butyl acetate / water system, excess ethyl acetate in the upper ethyl acetate layer was removed by atmospheric distillation, and this concentrated solution was distilled at around 190 ° C. to give 2,4- 0.73 kg of dimethyl-4-octanol was obtained. The yield was 94%.

[Comparative Synthesis Example 3]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ to prepare a 2.0N solution from a commercially available borane / THF solution. A commercially available THF solution (2.0 N) of cyclohexanone was also prepared.
(Batch reaction)
A 10 L reaction vessel corresponding to the same volume as that required for installing the continuous reaction apparatus of this example was vacuum dried, and then the reaction was performed in a high purity argon atmosphere. Next, 3 L of the prepared cyclohexanone / THF solution was introduced into the reaction vessel, cooled to 5 ° C., and then 3 L of borane / THF solution was injected over 3 hours. At this time, care was taken so that the internal temperature of the reaction did not exceed 25 ° C. After completion of the injection, the reaction vessel was further warmed to room temperature and further reacted for 7 hours.
(Post-processing)
The resulting reaction solution was hydrolyzed (reacted) with alkoxyborane using hydrogen peroxide water in an amount equal to or greater than the reaction equivalent, followed by atmospheric distillation of the THF solution to remove excess solvent. The reaction solution was separated and washed with a butyl acetate / water system, excess ethyl acetate in the upper ethyl acetate layer was removed by atmospheric distillation, and the concentrated solution was distilled at around 160 ° C. 50 kg was obtained. The yield was 83%.

[Comparative Synthesis Example 4]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) to be used, dehydration purification was performed with CaH ₂ , and an allylmagnesium bromide / diethyl ether solution (2.2 N) was obtained with allyl bromide and Mg metal in this diethyl ether solution. Prepared. Further, n-BuSnCl ₃ was dissolved in dehydrated diethyl ether to prepare a 2N n-BuSnCl ₃ / diethyl ether solution. The reaction molar ratio by raw material was set to n-BuSnCl ₃ : allyl lithium = 1: 3.3.
(Batch reaction)
A 10 L reaction vessel corresponding to the same volume as that required for installing the continuous reaction apparatus of this example was vacuum dried, and then the reaction was performed in a high purity argon atmosphere. Next, 3 L of the prepared nBuSnCl ₃ / diethyl ether solution was introduced into the reaction vessel, cooled to −5 ° C., and then 3 L of allylmagnesium bromide / diethyl ether solution was injected over 2 hours. At this time, care was taken so that the internal temperature of the reaction did not exceed 25 ° C. After completion of the injection, the reaction vessel was further warmed to room temperature and reacted for another 8 hours.
(Post-processing)
The resulting reaction solution was subjected to atmospheric distillation of diethyl ether to remove excess solvent. Further, 1.55 kg of triallylbutyltin was obtained by distilling the mixed solution under reduced pressure to about 0.2 mmHg and at around 90 ° C. The yield was 78%.

[Comparative Synthesis Example 5]
(Preparation of raw material reagents)
A commercially available rhodium chloride trihydrate was dissolved in an ethanol solution to prepare a RhCl ₃ / EtOH solution (1.0 N). A commercially available ethanol solution (3.0 N) of triphenylphosphine was also prepared.
(Batch reaction)
A 10 L reaction vessel corresponding to the same volume as that required for installing the continuous reaction apparatus of this example was vacuum dried, and then the reaction was performed in a high purity argon atmosphere. ₃ L of the RhCl ₃ / EtOH solution prepared above was introduced into the reaction vessel, and 3 L of ethanol solution of triphenylphosphine was injected at room temperature over 2 hours. At this time, the reaction solution was further heated to 50 ° C. and reacted for 8 hours.
(Post-processing)
The obtained reaction solution was subjected to atmospheric distillation of an ethanol solution to remove excess solvent. By separately purifying the reaction solution, 1.25 kg of Wilkinson's catalyst was obtained. The yield was 45%.

[Comparative Synthesis Example 6]
(Preparation of raw material reagents)
In order to reduce the amount of water in the diethyl ether used, dehydration purification was performed with CaH ₂ to dissolve GaCl _3, and a 2.42N GaCl ₃ diethyl ether solution was prepared. Further, a methyl lithium / diethyl ether solution (6.0 N) (manufactured by Kemetal Co., Ltd.) was prepared. The reaction molar ratio by raw material was set to GaCl ₃ : CH ₃ Li = 1: 3.3.
(Batch reaction)
A 10 L reaction vessel corresponding to the same volume required for installation with the continuous reaction apparatus of this example was vacuum dried, and then the reaction was performed in a high purity argon atmosphere. After 3 L of the GaCl ₃ / diethyl ether solution prepared above was introduced into the reaction vessel and cooled to −20 ° C., 3 L of methyl lithium / diethyl ether solution was injected over 2 hours. At this time, care was taken so that the internal temperature of the reaction did not exceed 25 ° C. After completion of the injection, the reaction vessel was further reacted at 10 ° C. for 8 hours.
(Adduct replacement)
Diethyl ether of the resulting reaction solution was subjected to atmospheric distillation to remove excess solvent. Next, triphenylphosphine / tetraethylene glycol dimethyl ether (molar ratio 1: 1.5) was injected into the obtained reaction solution. The mixed solution was subjected to vacuum distillation near room temperature, whereby diethyl ether coordinated to trimethylgallium was subjected to adduct exchange with triphenylphosphine. The obtained exchange solution was heated and distilled at 80 ° C. to obtain 0.22 kg of trimethylgallium. The yield was 78%.

Table 1 below shows the results of comparison between the examples and the comparative examples. The comparison magnification in the following table is the continuous synthesis amount / batch synthesis amount.

  As shown in Table 1, the continuous reaction apparatus of this embodiment can precisely control the introduction flow rate and temperature of two or more raw material solutions, and the apparatus volume equipment corresponding to the continuous reaction apparatus of this embodiment. Compared with the case of using the conventional batch polymerization synthesizer, mass production of several tens to several hundred times is possible. Therefore, the continuous reaction apparatus of this embodiment can produce many organic compounds or organometallic compounds with a small apparatus scale. As described above, the continuous reaction apparatus of the present embodiment can dramatically improve the mass production efficiency, dramatically improve the controllability of synthesis, and drastically reduce the cost of necessary equipment investment. In particular, in the field of synthesis of compounds that use organomagnesium halide reagents, organolithium reagents, organoaluminum reagents, etc. that need to be carried out at very low concentrations of water and oxygen in the reaction system, or to synthesize organometallic compounds Also in the field, mass production efficiency can be dramatically improved, and controllability of synthesis can be dramatically improved. Moreover, since the apparatus can be miniaturized and can be manufactured efficiently in a short time, the cost of required facility investment can be drastically reduced.

  Next, an example in which a polymer is synthesized using Synthesis Example 16 to Synthesis Example 21 and Comparative Synthesis Example 7 to Comparative Synthesis Example 10 will be described. The present invention will be specifically described with reference to synthesis examples and comparative synthesis examples, but the present invention is not limited to the following synthesis examples.

[Synthesis Example 16]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ . The styrene monomer was dehydrated using sodium. The styrene monomer was diluted with a purified THF solution to prepare a 0.96N solution. A 0.01N solution was prepared from a purified THF solution with commercially available s-butyllithium.
(Continuous polymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared styrene monomer / THF solution and s-butyllithium solution was filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min. Further, the maximum flow rate fluctuation rate at this time was 0.3%. Regarding the raw material temperature, both solutions were controlled from −40 ° C. to −30 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. The THF solution was continuously distilled at atmospheric pressure to remove excess solvent, and after preparing a polymerization solution of about 0.65 kg / L, 17.3 kg of polystyrene was obtained by a spray drying method. The yield was 96%. Polystyrene had a molecular weight (Mw) of 10200 and a dispersity (Mw / Mn) of 1.04.

[Synthesis Example 17]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ . The t-butoxystyrene monomer was dehydrated using sodium. This t-butoxystyrene monomer was diluted with a purified THF solution to prepare a 0.567N solution. A 0.01N solution was prepared from a purified THF solution with commercially available s-butyllithium.
(Continuous polymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere.
The t-butoxystyrene monomer / THF solution and the s-butyllithium solution prepared above were filled in a pressure vessel, respectively, and fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min. The maximum flow rate fluctuation rate at this time was 0.5%. Regarding the raw material temperature, both solutions were controlled from −30 ° C. to −20 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. By continuously performing atmospheric distillation of the THF solution, the excess solvent was removed, and after preparing a polymerization solution of about 0.65 kg / L, 16.9 kg of poly t-butoxystyrene was obtained by a spray drying method. The yield was 94%. Poly t-butoxystyrene had a molecular weight (Mw) of 9900 and a dispersity (Mw / Mn) of 1.03.

[Synthesis Example 18]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ . In addition, methyl methacrylate was dehydrated using sodium. The methyl methacrylate monomer was diluted with a purified THF solution to prepare a 1.0N solution. A 0.01N solution was prepared from a purified THF solution with commercially available triphenylmethyl sodium.
(Continuous polymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared methyl methacrylate monomer / THF solution and triphenylmethyl sodium solution was filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min. The maximum flow rate fluctuation rate at this time was 0.5%. Regarding the raw material temperature, both solutions were controlled from −10 ° C. to −0 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. The THF solution was continuously distilled at atmospheric pressure to remove excess solvent, and after preparing a polymerization solution of about 0.7 kg / L, 16.6 kg of polymethyl methacrylate was obtained by a spray drying method. The yield was 92%. The polymethyl methacrylate had a molecular weight (Mw) of 10100 and a dispersity (Mw / Mn) of 1.04.

[Synthesis Example 19]
(Preparation of raw material reagents)
In order to reduce the amount of water in the hexane used, dehydration purification was performed with CaH ₂ . In addition, a 4.62-N solution was prepared in a 1,3-butadiene / hexane solution at low temperature and dehydrated. A 0.025N solution was prepared from a THF solution purified in the same manner as commercially available s-butyllithium.
(Continuous polymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared 1,3-butadiene / hexane solution and s-butyllithium solution were filled in each pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The raw material solution was measured for flow rate with a Coriolis flow meter, cooled by a spiral tube for cooling, and then sent to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min. The maximum flow rate fluctuation rate at this time was 0.5%. Regarding the raw material temperature, both solutions were controlled from 10 ° C. to 20 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. By continuously performing an atmospheric distillation of the THF / hexane solution, excess solvent was removed, and after preparing a polymerization solution of about 0.55 kg / L, 34.6 kg of polybutadiene rubber was obtained by a spray drying method. The yield was 81%. The polybutadiene rubber had a molecular weight (Mw) of 9600 and a dispersity (Mw / Mn) of 1.07.

[Synthesis Example 20]
(Preparation of raw material reagents)
Acrylonitrile was dissolved in dehydrated dimethylacetamide to be used to prepare 4.71N acrylonitrile / dimethylacetamide solution. A 0.025N solution was prepared from a dehydrated dimethylacetamide solution similar to commercially available potassium t-butoxide.
(Continuous polymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared acrylonitrile / dimethylacetamide solution and potassium t-butoxide solution was filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min. Further, the maximum flow rate fluctuation rate at this time was 0.3%. Regarding the raw material temperature, both solutions were controlled from 30 ° C. to 40 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using hydrogen chloride water. Excess solvent was removed by continuously performing vacuum distillation of the dimethylacetamide solution to prepare a polymerization solution of about 0.55 kg / L, and 33.7 kg of polybutadiene rubber was obtained by a spray drying method. The yield was 75%. The polybutadiene rubber had a molecular weight (Mw) of 12300 and a dispersity (Mw / Mn) of 1.21.

[Synthesis Example 21]
(Preparation of raw material reagents)
In order to reduce the amount of water in the hexane and tetrahydrofuran used, dehydration purification was performed with CaH ₂ . Further, a 3.12N solution was prepared in a 1,3-butadiene / hexane solution at low temperature and dehydrated, and a 0.78N solution was prepared from styrene and THF dehydrated and purified with sodium. A 0.025N solution was prepared from a THF solution purified in the same manner as commercially available s-butyllithium.
(Continuous polymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere.
The 1,3-butadiene / hexane solution, the styrene / THF solution prepared above, and the s-butyllithium solution as a polymerization initiator were filled in a pressure vessel, respectively, and the mixture was transferred to a static stirrer using three triple plunger pumps. Liquid feeding was performed. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min. Further, the maximum flow rate fluctuation rate at this time was 0.3%. Regarding the raw material temperature, both solutions were controlled from 10 ° C. to 20 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. The excess solvent is removed by continuously performing atmospheric distillation of the THF / hexane solution to prepare a polymerization solution of about 0.55 kg / L, and then 33.8 kg of a styrene-butadiene random copolymer is obtained by a spray drying method. Obtained. The yield was 75%. The styrene-butadiene random copolymer had a molecular weight (Mw) of 10300 and a dispersity (Mw / Mn) of 1.05.

[Comparative Synthesis Example 7]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ . The styrene monomer was dehydrated using sodium. A 1.0N solution was prepared from a purified THF solution with commercially available s-butyllithium.
(Batch polymerization)
A 10 L reaction vessel corresponding to the same volume as that required for installing the continuous reaction apparatus of this example was vacuum dried, and then the reaction was performed in a high purity argon atmosphere. Next, 50 ml of the prepared s-butyllithium / THF solution and 5 L of purified tetrahydrofuran were filled in each reaction vessel, the internal temperature was cooled to -70 ° C, 500 g of styrene monomer was injected over 3 hours, and -70 ° C was further added. The reaction was carried out for 5 hours, and the reaction was stopped using 20 ml of methanol. Thereafter, the internal temperature of the reaction was heated to 25 ° C.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel, and the THF solution was subjected to atmospheric distillation to remove excess solvent. After preparing a polymerization solution of about 0.65 kg / L, the polystyrene was reduced to 0 by spray drying. .47 kg was obtained. The yield was 94%. Polystyrene had a molecular weight (Mw) of 10800 and a dispersity (Mw / Mn) of 1.12.

[Comparative Synthesis Example 8]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ . The styrene monomer was dehydrated using sodium. The styrene monomer was diluted with a purified THF solution to prepare a 0.96N solution. A 0.01N solution was prepared from a purified THF solution with commercially available s-butyllithium.
(Continuous polymerization without precise flow control)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared styrene monomer / THF solution and s-butyllithium solution was filled in a pressure vessel, and the solution was fed to a static stirrer by a pressure method from an argon cylinder. At this time, the pre-reaction solution was cooled with a cooling spiral tube, and then sent to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min. However, the maximum flow rate fluctuation rate at this time was 27%. Regarding the raw material temperature, both solutions were controlled from −40 ° C. to −30 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. The THF solution was continuously distilled at atmospheric pressure to remove excess solvent, and after preparing a polymerization solution of about 0.65 kg / L, 17.1 kg of polystyrene was obtained by a spray drying method. The yield was 95%. Polystyrene had a molecular weight (Mw) of 11100 and a dispersity (Mw / Mn) of 1.13.

[Comparative Synthesis Example 9]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ . Methyl methacrylate was dehydrated and purified using sodium. Furthermore, a 1.0N solution was prepared from a purified THF solution with commercially available sodium triphenylmethyl.
(Batch polymerization)
A 10 L reaction vessel corresponding to the same volume as that required for installing the continuous reaction apparatus of this example was vacuum dried, and then the reaction was performed in a high purity argon atmosphere. Next, 50 ml of the prepared s-butyllithium / THF solution and 5 L of purified tetrahydrofuran were charged into the reaction vessel, the internal temperature was cooled to −20 ° C., 500 g of methyl methacrylate monomer was injected over 3 hours, and −20 The reaction was carried out for 5 hours while maintaining the temperature, and the reaction was stopped using 20 ml of methanol. Thereafter, the internal temperature of the reaction was heated to 25 ° C.
(Post-processing)
The resulting polymerization solution is fed to a distillation vessel, and the THF solution is subjected to atmospheric distillation to remove excess solvent. After preparing a polymerization solution of about 0.65 kg / L, polymethyl methacrylate is prepared by spray drying. 0.45 kg was obtained. The yield was 89%. Polymethyl methacrylate had a molecular weight (Mw) of 12000 and a dispersity (Mw / Mn) of 1.13.

[Comparative Synthesis Example 10]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ . In addition, methyl methacrylate was dehydrated using sodium. The methyl methacrylate monomer was diluted with a purified THF solution to prepare a 1.0N solution. A 0.01N solution was prepared from a purified THF solution with commercially available triphenylmethyl sodium.
(Continuous polymerization without precise flow control)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared methyl methacrylate monomer / THF solution and triphenylmethyl sodium solution was filled in a pressure vessel, and the solution was fed to a static stirrer by a pressurization method from an argon cylinder. The flow rate of the raw material solution was measured with a Coriolis flowmeter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out a continuous reaction. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min. However, the maximum flow rate fluctuation rate at this time was 33%. Regarding the raw material temperature, both solutions were controlled from −10 ° C. to −0 ° C., and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. The atmospheric distillation of the THF solution was continuously performed to remove excess solvent. After preparing a polymerization solution of about 0.7 kg / L, 14.2 kg of polymethyl methacrylate was obtained by a spray drying method. The yield was 79%. Polymethyl methacrylate had a molecular weight (Mw) of 11800 and a dispersity (Mw / Mn) of 1.12.

The comparison results are shown in Table 2 below. The comparison magnification in the following table is the continuous synthesis amount / batch synthesis amount.

  As shown in Table 2, the continuous reaction apparatus of this embodiment measures the introduction flow rates of one or more raw material monomer solutions and a polymerization initiator solution using a flow meter (muff flow) in a continuous living anion polymerization reaction. When performing polymerization using the conventional batch polymerization synthesizer of the equipment volume equipment corresponding to the continuous reaction apparatus of this embodiment by performing stable control of each flow rate and controlling the introduction temperature and polymerization temperature Compared with, it is possible to mass-produce a polymer compound several tens of times. Furthermore, the controllability of the molecular weight and dispersity of the resulting polymer compound is extremely high. Therefore, the continuous reaction apparatus of this embodiment can produce many polymer polymers with a small apparatus scale. From the above, the continuous reaction apparatus of the present embodiment can dramatically improve mass production efficiency and dramatically improve the controllability of the polymer. Moreover, since the apparatus can be miniaturized and can be manufactured efficiently in a short time, the cost of required facility investment can be drastically reduced.

  Next, an example in which a block polymer copolymer is synthesized using Synthesis Example 22 to Synthesis Example 32 and Comparative Synthesis Example 11 to Comparative Synthesis Example 14 will be described. EXAMPLES Hereinafter, although a synthesis example and a comparative synthesis example are shown and this invention is demonstrated concretely, this invention is not restrict | limited to the following synthesis example.

[Synthesis Example 22]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene used, dehydration purification was performed with CaH ₂ . The styrene monomer and t-butoxystyrene monomer were dehydrated using triphenylmethyllithium. The styrene monomer and t-butoxystyrene monomer were diluted with a purified benzene solution to prepare a 0.74N solution. Furthermore, a 0.01N solution was prepared from commercially available s-butyllithium and a purified benzene solution.
(Continuous diblock copolymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared styrene monomer / benzene solution and s-butyllithium solution were filled in pressure vessels, respectively, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flow meter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out continuous polymerization. Further, the t-butstyrene / benzene solution was introduced into the latter half of a static stirrer connected by a separate triple plunger pump, and additional block polymerization was carried out. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw materials and the initiator solution were adjusted to 0.2 L / min. Moreover, each raw material monomer and the maximum flow rate fluctuation rate at this time were 0.4%. Regarding the raw material temperature, all solutions were controlled from -20 ° C to -10 ° C, and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. By continuously performing atmospheric distillation of the benzene solution, the excess solvent is removed, and after preparing a polymerization solution of about 0.60 kg / L, a styrene-t-butstyrene copolymer represented by the following formula is obtained by a spray drying method. 22.1 kg of coalescence was obtained. The yield was 93%. The styrene-t-butoxystyrene copolymer had a molecular weight (Mw) of 20100 and a dispersity (Mw / Mn) of 1.05.

[Synthesis Example 23]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene used, dehydration purification was performed with CaH ₂ . The styrene monomer was subjected to a dehydration reaction using triphenylmethyllithium. The styrene monomer was diluted with a purified benzene solution to prepare a 1.16N solution. Furthermore, an isoprene / toluene 1.16N solution was also prepared separately, and a 0.01N solution was prepared from commercially available s-butyllithium and a purified benzene solution.
(Continuous diblock copolymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared styrene monomer / benzene solution and s-butyllithium solution were filled in pressure vessels, respectively, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flow meter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out continuous polymerization. Further, the isoprene / benzene solution was introduced into the latter half of a static stirrer connected by another triple plunger pump, and additional block polymerization was carried out. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.2 L / min. Moreover, each raw material monomer and the maximum flow rate fluctuation rate at this time were 0.2%. The raw material temperature was controlled from −20 ° C. to −10 ° C. in the styrene reaction stage and from 50 ° C. to 60 ° C. in the isoprene reaction stage, and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. By continuously performing atmospheric distillation of the benzene solution, the excess solvent is removed, and after preparing a polymerization solution of about 0.60 kg / L, a styrene-isoprene copolymer represented by the following formula is obtained by a spray drying method. 10.9 kg was obtained. The yield was 91%. The styrene-isoprene copolymer had a molecular weight (Mw) of 20100 and a dispersity (Mw / Mn) of 1.04.

[Synthesis Example 24]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene used, dehydration purification was performed with CaH ₂ . The styrene monomer and 2-vinylpyridine were each subjected to a dehydration reaction using triphenylmethyllithium. The styrene monomer and 2-vinylpyridine monomer were diluted with a purified benzene solution to prepare a 0.956N solution. A 0.01N solution was prepared from commercially available s-butyllithium and a purified benzene solution.
(Continuous diblock copolymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared styrene monomer / benzene solution and s-butyllithium solution were filled in pressure vessels, respectively, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flow meter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out continuous polymerization. Further, a 2-vinylpyridine monomer / benzene solution was introduced into the latter half of a static stirrer connected by a separate triple plunger pump, and additional block polymerization was carried out. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min. Moreover, each raw material monomer and the maximum flow rate fluctuation rate at this time were 0.4%. Regarding the raw material temperature, all solutions were controlled from -40 ° C to -30 ° C, and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. By performing continuous atmospheric distillation of the benzene solution, excess solvent is removed, and after preparing a polymerization solution of about 0.60 kg / L, a styrene-2-vinylpyridine copolymer represented by the following formula is prepared by a spray drying method. 17.3 kg of polymer was obtained. The yield was 96%. The styrene-2-vinylpyridine copolymer had a molecular weight (Mw) of 19,900 and a dispersity (Mw / Mn) of 1.03.

[Synthesis Example 25]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ . The styrene monomer and methyl methacrylate were dehydrated using triphenylmethyl lithium. The styrene monomer and methyl methacrylate monomer were diluted with a purified THF solution to prepare a 0.98N solution. A 0.01N solution was prepared from commercially available s-butyllithium and a purified THF solution.
(Continuous diblock copolymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared styrene monomer / THF solution and s-butyllithium solution was filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flow meter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out continuous polymerization. Further, a methyl methacrylate / THF solution was introduced into the latter half of a static stirrer connected by a separate triple plunger pump, and additional block polymerization was carried out. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min. Moreover, each raw material monomer and the maximum flow rate fluctuation rate at this time were 0.2%. Regarding the raw material temperature, all solutions were controlled from -20 ° C to -10 ° C, and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. The excess solvent is removed by continuously performing atmospheric distillation of the benzene solution, and after preparing a polymerization solution of about 0.60 kg / L, the styrene-methacrylic acid methyl ester copolymer represented by the following formula is spray-dried. 15.8 kg of polymer was obtained. The yield was 88%. The styrene-methacrylic acid methyl ester copolymer had a molecular weight (Mw) of 20700 and a dispersity (Mw / Mn) of 1.05.

[Synthesis Example 26]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ . The styrene monomer and acrylonitrile were dehydrated using triphenylmethyllithium. The styrene monomer and acrylonitrile monomer were diluted with a purified THF solution to prepare a 1.27N solution. A 0.01N solution was prepared from commercially available s-butyllithium and a purified THF solution.
(Continuous diblock copolymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, each of the prepared styrene monomer / THF solution and s-butyllithium solution was filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flow meter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out continuous polymerization. Further, an acrylonitrile / THF solution was introduced into the latter half of a static stirrer connected by another triple plunger pump, and additional block polymerization was carried out. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.3 L / min. Moreover, each raw material monomer and the maximum flow rate fluctuation rate at this time were 0.4%. Regarding the raw material temperature, all solutions were controlled from -20 ° C to -10 ° C, and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. By performing continuous atmospheric distillation of the benzene solution, the excess solvent is removed, and after preparing a polymerization solution of about 0.60 kg / L, a styrene-acrylonitrile copolymer represented by the following formula is obtained by a spray drying method. 12.6 kg was obtained. The yield was 90%. The styrene-acrylonitrile copolymer had a molecular weight (Mw) of 20400 and a dispersity (Mw / Mn) of 1.03.

[Synthesis Example 27]
(Preparation of raw material reagents)
In order to reduce the amount of water in the tetrahydrofuran (THF) used, dehydration purification was performed with CaH ₂ . The 4-t-butoxystyrene monomer and methacrylic acid t-butyl ester were each subjected to a dehydration reaction using triphenylmethyllithium. The 4-t-butoxystyrene monomer and the methacrylic acid t-butyl ester monomer were diluted with a purified THF solution to prepare a 0.628N solution. A 0.01N solution was prepared from commercially available s-butyllithium and a purified THF solution.
(Continuous diblock copolymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared 4-t-butoxystyrene monomer / THF solution and s-butyllithium solution were filled in a pressure vessel, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flow meter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out continuous polymerization. Furthermore, the methacrylic acid t-butyl ester / THF solution was introduced into the latter half of a static stirrer connected by another triple plunger pump feeding solution to carry out additional block polymerization. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw material solutions were adjusted to 0.2 L / min. Moreover, each raw material monomer and the maximum flow rate fluctuation rate at this time were 0.5%. Regarding the raw material temperature, all the solutions were controlled from -30 ° C to -20 ° C, and this continuous reaction was performed for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. 4-t-Butoxystyrene represented by the following formula is obtained by spray drying method after removing excess solvent by continuously performing atmospheric distillation of benzene solution to prepare a polymerization solution of about 0.60 kg / L. -10.2 kg of methacrylic acid t-butyl ester copolymer was obtained. The yield was 85%. The 4-t-butoxystyrene-methacrylic acid t-butyl ester copolymer had a molecular weight (Mw) of 20700 and a dispersity (Mw / Mn) of 1.07.

[Synthesis Example 28]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene used, dehydration purification was performed with CaH ₂ . The styrene monomer and t-butoxystyrene monomer were dehydrated using triphenylmethyllithium. The styrene monomer and t-butoxystyrene monomer were diluted with a purified benzene solution to prepare 0.43N and 0.58N solutions, respectively. Further, a 0.95N solution of butadiene / benzene cooled and liquefied was prepared separately, and a 0.01N solution was prepared from commercially available s-butyllithium and a purified benzene solution.
(Continuous triblock copolymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared styrene monomer / benzene solution (1 step) and s-butyllithium solution were filled in a pressure vessel, respectively, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flow meter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out continuous polymerization. Furthermore, the t-butoxystyrene / benzene solution was introduced into the latter half of the static stirrer connected by a separate triple plunger pump feed, and finally the styrene monomer / benzene solution (two steps) was fed to the static stirrer. Block polymerization was performed. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw materials and the initiator solution were adjusted to 0.2 L / min. Moreover, each raw material monomer at this time and the maximum flow rate fluctuation rate were 0.3%. Regarding the raw material temperature, all solutions were controlled from -20 ° C to -10 ° C, and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. By continuously performing atmospheric distillation of the benzene solution, excess solvent is removed, and after preparing a polymerization solution of about 0.60 kg / L, styrene-t-butoxystyrene represented by the following formula by a spray drying method 22.6 kg of styrene copolymer was obtained. The yield was 94%. The styrene-t-butoxystyrene-styrene copolymer had a molecular weight (Mw) of 20400 and a dispersity (Mw / Mn) of 1.08.

[Synthesis Example 29]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene used, dehydration purification was performed with CaH ₂ . The styrene monomer and 4-chlorostyrene were dehydrated using triphenylmethyllithium. The styrene monomer and 4-chlorostyrene monomer were diluted with a purified benzene solution to prepare 0.51N and 0.68N solutions, respectively. Further, a similarly purified isoprene / benzene 0.67N solution was prepared separately, and a 0.01N solution was prepared from commercially available s-butyllithium and a purified benzene solution.
(Continuous triblock copolymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared styrene monomer / benzene solution (1 step) and s-butyllithium solution were filled in a pressure vessel, respectively, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flow meter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out continuous polymerization. In addition, the 4-chlorostyrene / benzene solution was introduced into the latter half of the static stirrer connected by another triple plunger pump feed, and finally the styrene monomer / benzene solution (two steps) was fed to the static stirrer, Block polymerization was performed. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw materials and the initiator solution were adjusted to 0.2 L / min. Moreover, each raw material monomer and the maximum flow rate fluctuation rate at this time were 0.5%. Regarding the raw material temperature, all solutions were controlled from -20 ° C to -10 ° C, and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. By continuously performing atmospheric distillation of the benzene solution, the excess solvent is removed, and after preparing a polymerization solution of about 0.60 kg / L, styrene-4-chlorostyrene- 22.8 kg of styrene copolymer was obtained. The yield was 95%. The styrene-4-chlorostyrene-styrene copolymer had a molecular weight (Mw) of 20100 and a dispersity (Mw / Mn) of 1.04.

[Synthesis Example 30]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene used, dehydration purification was performed with CaH ₂ . The styrene monomer and t-butoxystyrene monomer were dehydrated using triphenylmethyllithium. The styrene monomer and t-butoxystyrene monomer were diluted with a purified benzene solution to prepare 0.725N and 0.544N solutions, respectively. Furthermore, an acrylonitrile / benzene 0.544N solution was prepared separately, and a 0.01N solution was also prepared from commercially available s-butyllithium and a purified benzene solution.
(Continuous triblock copolymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared styrene monomer / benzene solution (1 step) and s-butyllithium solution were filled in a pressure vessel, respectively, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flow meter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out continuous polymerization. In addition, t-butoxystyrene monomer / benzene solution (2 steps) was introduced into the latter half of the static stirrer connected by another triple plunger pump, and finally acrylonitrile monomer / benzene solution (3 steps) was static. Liquid feeding to the stirrer and triblock polymerization were performed. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw materials and the initiator solution were adjusted to 0.2 L / min. Moreover, each raw material monomer and the maximum flow rate fluctuation rate at this time were 0.4%. Regarding the raw material temperature, all solutions were controlled from -20 ° C to -10 ° C, and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. By performing continuous atmospheric distillation of the benzene solution, the excess solvent is removed, and after preparing a polymerization solution of about 0.60 kg / L, styrene-t-butoxystyrene-acrylonitrile represented by the following formula by a spray drying method. 23.0 kg of copolymer (ABS resin) was obtained. The yield was 96%. The styrene-t-butoxystyrene-acrylonitrile copolymer (ABS resin) had a molecular weight (Mw) of 20500 and a dispersity (Mw / Mn) of 1.07.

[Synthesis Example 31]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene used, dehydration purification was performed with CaH ₂ . The styrene monomer and t-butoxystyrene monomer were dehydrated using triphenylmethyllithium. The styrene monomer and t-butoxystyrene monomer were diluted with a purified benzene solution to prepare 0.643N and 0.482N solutions, respectively. Further, a methacrylic acid methyl ester / benzene 0.683N solution was separately prepared, and a 0.01N solution was also prepared from commercially available s-butyllithium and a purified benzene solution.
(Continuous triblock copolymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared styrene monomer / benzene solution (1 step) and s-butyllithium solution were filled in a pressure vessel, respectively, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flow meter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out continuous polymerization. In addition, t-butoxystyrene monomer / benzene solution (2 steps) was introduced into the latter half of the static stirrer connected by another triple plunger pump, and finally, methacrylic acid methyl ester monomer / benzene solution (3 steps). Was fed to a static stirrer and triblock polymerization was performed. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw materials and the initiator solution were adjusted to 0.2 L / min. Moreover, each raw material monomer and the maximum flow rate fluctuation rate at this time were 0.5%. Regarding the raw material temperature, all solutions were controlled from -20 ° C to -10 ° C, and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. By continuously performing atmospheric distillation of the benzene solution, excess solvent is removed, and after preparing a polymerization solution of about 0.60 kg / L, styrene-t-butoxystyrene-methacrylic acid represented by the following formula by a spray drying method. 21.4 kg of acid methyl ester copolymer was obtained. The yield was 89%. The styrene-t-butoxystyrene-methacrylic acid methyl ester copolymer had a molecular weight (Mw) of 20900 and a dispersity (Mw / Mn) of 1.06.

[Synthesis Example 32]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene used, dehydration purification was performed with CaH ₂ . The styrene monomer was subjected to a dehydration reaction using triphenylmethyllithium. The styrene monomer was diluted with a purified benzene solution to prepare a 0.914N solution. Further, similarly purified acrylonitrile / benzene 0.685N solution and methacrylic acid methyl ester / benzene 0.685N solution were prepared separately, and 0.01N solution was also prepared from commercially available s-butyllithium and purified benzene solution.
(Continuous triblock copolymerization)
First, after the entire system in the apparatus was vacuum-dried, the reaction was performed in a high-purity argon atmosphere. Next, the prepared styrene monomer / benzene solution (1 step) and s-butyllithium solution were filled in a pressure vessel, respectively, and the solution was fed to a static stirrer using two triple plunger pumps. The flow rate of the raw material solution was measured with a Coriolis flow meter, the pre-reaction solution was cooled with a cooling spiral tube, and then fed to a static stirrer and mixed to carry out continuous polymerization. In addition, the acrylonitrile monomer / benzene solution (2 stages) was introduced into the latter half of the static stirrer connected by a separate triple plunger pump, and finally the methacrylic acid methyl ester monomer / benzene solution (3 stages) was a static stirrer. Liquid feeding and triblock polymerization. Moreover, the temperature control of the raw material was performed using the temperature sensor with which the upstream side of a static stirrer and the connected static stirrer were equipped. The flow rates of both raw materials and the initiator solution were adjusted to 0.2 L / min. Moreover, each raw material monomer and the maximum flow rate fluctuation rate at this time were 0.2%. Regarding the raw material temperature, all solutions were controlled from -20 ° C to -10 ° C, and this continuous reaction was carried out for 10 hours.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel in the apparatus, and the polymerization was stopped using methanol. By continuously performing atmospheric distillation of the benzene solution, the excess solvent is removed, and after preparing a polymerization solution of about 0.60 kg / L, styrene-acrylonitrile-methyl methacrylate represented by the following formula by a spray drying method. 20.4 kg of (ester copolymer) was obtained. The yield was 85%. Styrene-acrylonitrile-methyl methacrylate (ester copolymer) had a molecular weight (Mw) of 19700 and a dispersity (Mw / Mn) of 1.04.

[Comparative Synthesis Example 11]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene used, dehydration purification was performed with CaH ₂ . The styrene monomer and t-butoxystyrene monomer were dehydrated using triphenylmethyllithium. A 1.0N solution was prepared from commercially available s-butyllithium and purified benzene solution.
(Batch polymerization)
A 10 L reaction vessel corresponding to the same volume as that required for installing the continuous reaction apparatus of this example was vacuum dried, and then the reaction was performed in a high purity argon atmosphere. Next, 25 ml of the prepared s-butyllithium / benzene solution and 5 L of purified benzene were charged into the reaction vessel, the internal temperature was cooled to −70 ° C., 185.5 g of styrene monomer was injected over 3 hours, and − After the temperature was raised to 20 ° C., 314.5 g of t-butoxystyrene monomer was introduced over 3 hours, the reaction was further performed for 2 hours, and the reaction was stopped using 20 ml of methanol. Thereafter, the internal temperature of the reaction was heated to 25 ° C.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel, and the benzene solution was subjected to atmospheric distillation to remove excess solvent. After preparing a polymerization solution of about 0.65 kg / L, styrene-t was prepared by spray drying. -0.485 kg of butoxystyrene copolymer was obtained. The yield was 97%. The styrene-t-butoxystyrene copolymer had a molecular weight (Mw) of 21,200 and a dispersity (Mw / Mn) of 1.07.

[Comparative Synthesis Example 12]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene used, dehydration purification was performed with CaH ₂ . The styrene monomer and methacrylic acid methyl ester monomer were subjected to a dehydration reaction using triphenylmethyl lithium. A 1.0N solution was prepared from commercially available s-butyllithium and purified benzene solution.
(Batch polymerization)
A 10 L reaction vessel corresponding to the same volume as that required for installing the continuous reaction apparatus of this example was vacuum dried, and then the reaction was performed in a high purity argon atmosphere. Next, 25 ml of the prepared s-butyllithium / benzene solution and 5 L of purified benzene were charged into the reaction vessel, the internal temperature was cooled to -70 ° C., and 255 g of styrene monomer was injected over 3 hours, and further −20 ° C. After the temperature was raised to 245 g, 245 g of methacrylic acid methyl ester monomer was introduced over 3 hours, the reaction was further continued for 2 hours, and the reaction was stopped using 20 ml of methanol. Thereafter, the internal temperature of the reaction was heated to 25 ° C.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel, and the benzene solution was subjected to atmospheric distillation to remove excess solvent. After preparing a polymerization solution of about 0.65 kg / L, styrene-methacrylic was prepared by spray drying. 0.45 kg of acid methyl ester copolymer was obtained. The yield was 90%. The styrene-methacrylic acid methyl ester copolymer had a molecular weight (Mw) of 21,500 and a dispersity (Mw / Mn) of 1.12.

[Comparative Synthesis Example 13]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene used, dehydration purification was performed with CaH ₂ . The styrene monomer and t-butoxystyrene monomer were dehydrated using triphenylmethyllithium. A 1.0N solution was prepared from commercially available s-butyllithium and purified benzene solution.
(Batch polymerization)
A 10 L reaction vessel corresponding to the same volume as that required for installing the continuous reaction apparatus of this example was vacuum dried, and then the reaction was performed in a high purity argon atmosphere. Next, 25 ml of the prepared s-butyllithium / benzene solution and 5 L of purified benzene were charged into the reaction vessel, the internal temperature was cooled to -70 ° C, and 117 g of styrene monomer was injected over 2 hours. 265 g of t-butoxystyrene monomer was introduced over 3 hours, reacted for another 2 hours, cooled again to -70 ° C., and 174 g of styrene monomer was injected over 2 hours, followed by polymerization for 1 hour. After the run, the reaction was stopped with 20 ml of methanol. Thereafter, the internal temperature of the reaction was heated to 25 ° C.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel, and the benzene solution was subjected to atmospheric distillation to remove excess solvent. After preparing a polymerization solution of about 0.65 kg / L, styrene-t was prepared by spray drying. 0.43 kg of -butoxystyrene-styrene copolymer was obtained. The yield was 85%. The styrene-t-butoxystyrene-styrene copolymer had a molecular weight (Mw) of 21,700 and a dispersity (Mw / Mn) of 1.14.

[Comparative Synthesis Example 14]
(Preparation of raw material reagents)
In order to reduce the amount of water in the benzene used, dehydration purification was performed with CaH ₂ . The styrene monomer, t-butoxystyrene monomer, and methacrylic acid methyl ester monomer were subjected to a dehydration reaction using triphenylmethyllithium. A 1.0N solution was prepared from commercially available s-butyllithium and purified benzene solution.
(Batch polymerization)
A 10 L reaction vessel corresponding to the same volume as that required for installing the continuous reaction apparatus of this example was vacuum dried, and then the reaction was performed in a high purity argon atmosphere. Next, 25 ml of the prepared s-butyllithium / benzene solution and 5 L of purified benzene were filled in each reaction vessel, the internal temperature was cooled to -70 ° C, and 167 g of styrene monomer was injected over 2 hours, and further -60 ° C Then, 212 g of t-butoxystyrene monomer was introduced over 3 hours and further reacted for 2 hours. After the temperature was raised to −10, 121 g of methacrylic acid methyl ester monomer was injected over 2 hours. After time polymerization, the reaction was stopped using 20 ml of methanol. Thereafter, the internal temperature of the reaction was heated to 25 ° C.
(Post-processing)
The obtained polymerization solution was sent to a distillation vessel, and the benzene solution was subjected to atmospheric distillation to remove excess solvent. After preparing a polymerization solution of about 0.65 kg / L, styrene-t was prepared by spray drying. 0.41 kg of a butoxystyrene-methacrylic acid methyl ester copolymer was obtained. The yield was 82%. The styrene-t-butoxystyrene-methacrylic acid methyl ester copolymer resin had a molecular weight (Mw) of 20900 and a dispersity (Mw / Mn) of 1.08.

The comparison results are shown in Table 3 below. The comparison magnification in the following table is the continuous synthesis amount / batch synthesis amount.

  As shown in Table 3, the continuous reaction apparatus of this embodiment measures the introduction flow rates of two or more raw material monomer solutions and the polymerization initiator solution using a flow meter, performs stable control of each flow rate, and introduces them. By controlling the temperature and the polymerization temperature, the block corresponding to several tens of times compared to the case of using the conventional batch polymerization synthesizer of the apparatus volume equipment corresponding to the continuous reaction apparatus of this embodiment The copolymer can be mass-produced. Therefore, the continuous reaction apparatus of this embodiment can produce many block copolymers with a small apparatus scale. From the above, the continuous reaction apparatus of the present embodiment can dramatically improve mass production efficiency and dramatically improve block polymerization controllability. Moreover, since the apparatus can be miniaturized and can be manufactured efficiently in a short time, the cost of required facility investment can be drastically reduced.

10, 10a, 10b, 110, 110a Continuous reactor 12, 112, 112a First raw material supply unit 14, 113, 113a Second raw material supply unit 114, 114a Third raw material supply unit 115, 115a Fourth raw material supply unit 16, 116 Pressure adjusting unit 18, 118 Reaction unit 20, 120 Recovery unit 22 Control unit 30a First raw material container 30b Second raw material container 30c Third raw material container 30d Fourth raw material container 31a, 31b, 31c, 31d Control valve 32a, 32b, 32c, 32d metering pump
34a, 34b, 34c, 34d Heat exchanger 35a, 35b, 35c, 35d Mass meter 36a, 36b, 36c, 36d Upstream pressure sensor 38a, 38b, 38c, 38d Flow meter 40a, 40b, 40c, 40d Downstream pressure sensor
42a, 42b Upstream temperature sensor 44a, 44b Downstream temperature sensor 46a, 46b, 46c, 46d Dip tube 50 High pressure cylinder 51 Gas supply pipe 52 Pressure reducing valve 54 Pressure regulator 55a, 55b, 55c, 55d Branch pipe 56a, 56b, 56c, 56d Gas control valve 60, 60a, 60b, 60c Static stirrer 62, 62a, 62b, 62c Temperature control mechanism 64 Upstream temperature sensor 66 Downstream temperature sensor 70 Recovery container 80a, 80b, 80c, 80d Flow control device ( Mass flow controller)
La 1st supply line Lb 2nd supply line Lc 3rd supply line Ld 4th supply line L1 Reaction line

Claims (31)

Heat exchange is performed between a first raw material container that stores the first raw material, a first supply line that distributes the first raw material stored in the first raw material container, and the first raw material that flows through the first supply line. A first raw material supply unit that includes the first heat exchanger to perform, and supplies the first raw material heat-exchanged by the heat exchanger;
Heat exchange is performed between a second raw material container that stores the second raw material, a second supply line that distributes the second raw material stored in the second raw material container, and the second raw material that flows through the second supply line. A second raw material supply unit that includes the second heat exchanger to perform, and supplies the second raw material heat-exchanged by the heat exchanger;
The first raw material is continuously supplied from the first raw material supply unit, and the second raw material is continuously supplied from the second raw material supply unit. The reaction line is installed in the reaction line and supplied to the reaction line. A static stirrer that statically stirs the first raw material and the second raw material, and the first raw material and the second raw material are stirred by the static stirrer. A reaction part for continuously producing a reaction product with
Control for controlling the amount and temperature of the first raw material supplied from the first raw material supply unit to the reaction unit, and the amount and temperature of the second raw material supplied from the second material supply unit to the reaction unit A continuous reaction apparatus.   2. The continuous reaction apparatus according to claim 1, wherein one of the first raw material and the second raw material is one of organic magnesium halide, organic lithium, and organic aluminum.   The continuous reaction apparatus according to claim 1, wherein the static stirrer reacts a plurality of the raw materials from which salts are precipitated by a reaction by stirring. The continuous reaction apparatus according to any one of claims 1 to 3, wherein the reactant is represented by the following general formula (A).
(R ^A ) ₃ M _A Formula (A)
(In the formula (A), R ^A represents a linear or branched substituted alkyl group or alkoxyalkyl group having 1 to 10 carbon atoms, and M _A represents a Group III metal.) 4. The continuous reaction apparatus according to claim 1, wherein one of the first raw material and the second raw material is represented by the following general formula (B), and the other is represented by the following general formula (C). .
R ^B -Y Formula (B)
M _B (X _A ) Formula ₃ (C)
(In the formulas (B) and (C), R ^B represents a linear or branched substituted alkyl group or alkoxyalkyl group having 1 to 10 carbon atoms, and Y represents lithium or magnesium halide. M _B represents a Group III metal, and X _A represents a halogen atom. One of the first raw material and the second raw material is represented by the following general formula (D), the other is represented by the following general formula (E), and the reactant is represented by the following general formula (F). To 4. The continuous reaction apparatus according to any one of 3 to 4.
R ^C Li Formula (D)
M _C Cl Formula ₃ (E)
(R ^D ) ₃ M _D formula (F)
(In the formulas (D) to (F), R ^C and R ^D each independently represent a methyl group, an ethyl group, a propyl group or a butyl group, and M _C and M _D are each independently a gallium atom or Represents an indium atom.) The first heat exchanger cools the first raw material,
The continuous reaction apparatus according to any one of claims 1 to 6, wherein the second heat exchanger cools the first raw material.   The continuous reaction apparatus according to any one of 1 to 7, further comprising: a recovery unit that recovers the reaction product continuously generated in the reaction unit. The reaction unit further includes a temperature control mechanism for controlling the temperature in the static stirrer,
The continuous reaction apparatus according to any one of claims 1 to 8, wherein the control unit controls a temperature in the static stirrer. The first raw material supply unit has a metering pump that is installed in the first supply line and conveys the first raw material toward the reaction unit,
The continuous reaction apparatus according to any one of claims 1 to 9, wherein the second raw material supply unit includes a metering pump that is installed in the second supply line and conveys the second raw material toward the reaction unit. . The first raw material supply unit has a flow rate control device that is installed in the first supply line and controls the flow rate of the first raw material conveyed toward the reaction unit,
The said 2nd raw material supply part is installed in the said 2nd supply line, and has a flow volume control apparatus which controls the flow volume of the said 2nd raw material conveyed toward the said reaction part. A continuous reaction apparatus according to 1. The first raw material supply unit has a mass meter for measuring the mass of the first raw material container,
The continuous reaction apparatus according to any one of claims 1 to 11, wherein the second raw material supply unit includes a mass meter that measures a mass of the second raw material container.   The control unit is configured to supply the first raw material supply unit and the second raw material supply based on a measurement result of the mass meter of the first raw material supply unit and a measurement result of the mass meter of the second raw material supply unit. The continuous reaction apparatus of Claim 12 which controls operation | movement of a part. The first raw material supply unit has a first flow meter for measuring a flow rate of the first raw material flowing through the first supply line,
The continuous reaction apparatus according to any one of claims 1 to 13, wherein the second raw material supply unit includes a second flowmeter that measures a flow rate of the second raw material flowing through the second supply line.   The control unit is configured to supply the first raw material supply unit and the second raw material supply based on a measurement result of the flow meter of the first raw material supply unit and a measurement result of the flow meter of the second raw material supply unit. The continuous reaction apparatus of Claim 14 which controls operation | movement of a part. The first raw material supply unit has a pressure sensor that measures the pressure of the first raw material flowing through the first supply line,
The continuous reaction apparatus according to any one of claims 1 to 15, wherein the second raw material supply unit includes a pressure sensor that measures a pressure of the second raw material flowing through the second supply line.   The control unit includes the first raw material supply unit and the second raw material supply based on the measurement result of the pressure sensor of the first raw material supply unit and the measurement result of the pressure sensor of the second raw material supply unit. The continuous reaction apparatus of Claim 16 which controls operation | movement of a part. The first raw material supply unit has a temperature sensor that measures the temperature of the first raw material flowing through the first supply line,
The second raw material supply unit has a temperature sensor that measures the temperature of the second raw material flowing through the second supply line,
The control unit controls a cooling operation using a heat exchanger of the first raw material supply unit based on a measurement result of the temperature sensor of the first raw material supply unit,
The continuous reaction according to any one of claims 1 to 17, wherein a cooling operation using a heat exchanger of the second raw material supply unit is controlled based on a measurement result of the temperature sensor of the second raw material supply unit. apparatus. The reaction unit has a temperature sensor that measures the temperature of the compound flowing through the reaction line,
The continuous reaction device according to any one of claims 1 to 18, wherein the control unit controls an operation of the temperature control mechanism of the reaction unit based on a measurement result of the temperature sensor of the reaction unit.   A pressure adjusting unit that pressurizes the first raw material container and the second raw material container and transports the first raw material of the first raw material container and the second raw material of the second raw material container to the downstream side in the transport direction; The continuous reaction apparatus according to any one of claims 1 to 19. Another raw material container for storing another raw material different from at least one of the first raw material and the second raw material, another supply line for distributing the other raw material stored in the other raw material container, and the other supply A heat exchanger that exchanges heat with the other raw material flowing through the line, and having at least one other raw material supply unit that supplies the other raw material heat-exchanged by the heat exchanger;
The reaction section includes a plurality of the static stirrers, a plurality of the static stirrers are connected in series to the reaction line, and the temperature control mechanism is the most upstream of the plurality of the static stirrers. Placed against a static stirrer,
In the other raw material supply unit, the other supply line is connected to the reaction line between the static stirrer on the upstream side and the static stirrer on the downstream side, and is discharged from the static stirrer on the upstream side. Supplying the other raw material flowing through the other supply line to the reaction line through which the reactant flows.
The reaction section statically stirs the reactant discharged from the static stirrer on the upstream side with the static stirrer on the downstream side and the other raw material to react the reactant with the other raw material. Is generated continuously,
The continuous reaction apparatus according to any one of claims 1 to 18, wherein the control unit controls an amount and a temperature of the other raw material supplied from the other raw material supply unit to the reaction unit. The reaction unit has a plurality of temperature control mechanisms for controlling the temperature in the static stirrer, and a plurality of the temperature control mechanisms are arranged in each of the plurality of static stirrers,
The continuous reaction apparatus according to claim 21, wherein the control unit controls operations of the temperature control mechanisms. Two or more kinds of raw materials including at least a first raw material and a second raw material are supplied, and a static stirrer for statically stirring the two or more kinds of the supplied raw materials is provided,
A continuous reaction apparatus for controlling the flow rate and temperature at which the raw material is introduced into the static stirrer and the reaction temperature of the static stirrer. Two or more liquid raw materials including at least a first raw material and a second raw material are supplied, and a static stirrer that statically stirs the supplied two or more liquid raw materials;
A mechanism for supplying two or more kinds of liquid raw materials individually and continuously to the static stirrer;
And a mechanism for continuously discharging the reaction product generated by the static stirrer out of the system.   The continuous reaction apparatus according to claim 23 or 24, wherein one of the first raw material and the second raw material is any one of organic magnesium halide, organic lithium, and organic aluminum.   The continuous reaction apparatus according to any one of claims 23 to 25, wherein the static stirrer reacts a plurality of the raw materials from which salts are precipitated by a reaction by stirring. The continuous reaction apparatus according to any one of claims 23 to 26, wherein the reactant is represented by the following general formula (A).
(R ^A ) ₃ M _A Formula (A)
(In the formula (A), R ^A represents a linear or branched substituted alkyl group or alkoxyalkyl group having 1 to 10 carbon atoms, and M _A represents a Group III metal.) The continuous reaction apparatus according to any one of claims 23 to 27, wherein one of the first raw material and the second raw material is represented by the following general formula (B), and the other is represented by the following general formula (C). .
R ^B -Y Formula (B)
M _B (X _A ) Formula ₃ (C)
(In the formulas (B) and (C), R ^B represents a linear or branched substituted alkyl group or alkoxyalkyl group having 1 to 10 carbon atoms, and Y represents lithium or magnesium halide. M _B represents a Group III metal, and X _A represents a halogen atom. 24. One of the first raw material and the second raw material is represented by the following general formula (D), the other is represented by the following general formula (E), and the reactant is represented by the following general formula (F). The continuous reaction apparatus according to any one of 28 to 28.
R ^C Li Formula (D)
M _C Cl Formula ₃ (E)
(R ^D ) ₃ M _D formula (F)
(In the formulas (D) to (F), R ^C and R ^D each independently represent a methyl group, an ethyl group, a propyl group or a butyl group, and M _C and M _D are each independently a gallium atom or Represents an indium atom.) Using the continuous reaction apparatus according to any one of claims 1 to 20,
While adjusting the amount and temperature of the first raw material supplied from the first raw material supply unit to the reaction unit, and the amount and temperature of the second raw material supplied from the second material supply unit to the reaction unit, Continuously supplying the first raw material and the second raw material to the reaction section;
A step of stirring and synthesizing the first raw material and the second raw material supplied to the reaction section with the static stirrer, and discharging the obtained reaction product from the static stirrer to the downstream side; A continuous synthesis method comprising: Using the continuous reaction apparatus according to claim 21 or 22,
While adjusting the amount and temperature of the first raw material supplied from the first raw material supply unit to the reaction unit, and the amount and temperature of the second raw material supplied from the second material supply unit to the reaction unit, Continuously supplying the first raw material and the second raw material to the reaction section;
Stirring the first raw material and the second raw material supplied to the reaction section with the static stirrer, and discharging the obtained reaction product from the upstream static stirrer to the downstream side;
While adjusting the amount and temperature of the other raw material supplied from the other raw material supply unit to the reaction unit, the other raw material is continuously supplied to the reaction unit, and is downstream from the upstream static stirrer. The reaction product discharged to the side and the other raw materials are mixed with the downstream static stirrer to cause a synthesis reaction, and the obtained reaction product is discharged from the downstream static stirrer to the downstream side. Carrying out at least once.

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