JP6017204B2 - Nanoparticle manufacturing method, manufacturing apparatus, and automatic manufacturing apparatus - Google Patents

Description

  The present invention relates to a method for producing nanoparticles from a solvent and a raw material, and more particularly to a method for producing nanoparticles having a uniform fine diameter, a production apparatus, and an automatic production apparatus.

  In recent years, composite nano metal particles in which organic coating layers made of various organic materials are formed around a metal core of 100 nm or less as metal nanoparticles for bonding or metal pattern formation have been developed. For example, as the composite nanometal particle, Example 1 of JP-A-10-183207 (Patent Document 1) describes ultrafine particles having a stearic acid group organic coating layer around a metal silver core. . The present inventor has disclosed composite nano silver particles in which an organic coating layer such as alcohol molecules or alcohol derivatives is formed around silver nuclei in International Publication No. WO2009 / 090846 (Patent Document 2). . These nanoparticles are kneaded with a resin or a solvent to form a paste, and this paste is used for semiconductor bonding or printing ink. The degree of the particle size of the nanoparticles and the uniformity of the particle size of the nanoparticles greatly contribute to the quality of the paste. Therefore, it is extremely important to develop an apparatus for mass-producing fine nanoparticles with good uniformity.

  The methods for producing nanoparticles are roughly classified into a solid phase method, a liquid phase method, and a gas phase method. In the solid-phase method, the solid is melted to produce nanoparticles, so the amount of nanoparticles is large due to the large amount of material, but the particle size is large or the aggregation is severe, and the uniformity of particle size is difficult There are many. In the gas phase method, since nanoparticles are produced by a gas reaction, the amount of the substance is reduced and it is not suitable for mass production of nanoparticles. Therefore, the liquid phase method has been developed. In the liquid phase method, since the raw material is dispersed and dissolved in a solvent to form a solution and nanoparticles are produced as a solution reaction, the amount of the substance is increased and the mass productivity of the nanoparticles is improved. Moreover, if the concentration is adjusted, there is an advantage that it is easy to achieve uniformity of the particle diameter of the nanoparticles.

  As liquid phase methods for producing nanoparticles, JP 2005-264199 A (Patent Document 3), JP 2006-503790 A (Patent Document 4) and JP 2008-28549 A (Patent Document 5) are known. It has been.

The nanoparticle production apparatus of Patent Document 3 is shown in FIG. 20 of the present patent application. In FIG. 20, 101 is a microreactor, 102 is an ultrasonic generator, 103 is a water bath, 104 is a reactor, 105 is a bottom plate, 106 is an intermediate laminated thin plate, 107 is a top plate, 108 is an inflow channel, 109 is a microchannel. , 110 is an outlet, 124 is a connecting bolt, 126 is an ultrasonic wave, 126 a is a portion that is strengthened by ultrasonic interference, and 126 b is a portion that is weakened by ultrasonic interference.
The function of the microreactor 101 is to use ultrasonic energy in a microchannel 109 (109a, 109b) having a diameter of several μm to several hundreds of μm that is irradiated with ultrasonic waves by flowing an aqueous metal salt solution into the inflow path 108. Then, metal ultrafine particles (nanoparticles) are produced from the metal salt in an aqueous solution.

The nanoparticle production apparatus of Patent Document 4 is shown in FIG. 21 of the present patent application. (21A) is a straight tube type nanoparticle production apparatus, 201 is a reactor, 202 is a reaction tube, 203a is a zirconium salt aqueous solution (raw material aqueous solution), 203b is a suspension, 204 is a precipitated particle, 205 is a reaction mixture ( (Precipitation solution), 206 is a zirconia hydrate sol, 207 is a heating medium, 207a is an inlet, 207b is an outlet, 208 is a velocity gradient formed inside the reaction tube, 212 is a pH adjuster, and 213 is a mixer.
The function of the reactor 201 is to flow the heating medium 207 from the inlet 207a to the outlet 207b to heat the raw material aqueous solution 203a in the reaction tube 202 to generate precipitated particles 204 (zirconia hydrate nanoparticles). The Japanese sol 206 is sent out. However, as a nanoparticle generation condition, in [0052], the cross-sectional diameter of the reaction tube is preferably 0.01 cm to 5 cm, and in [0041], the zirconium salt aqueous solution has no vortex in the reaction tube, that is, a laminar flow. In [0049], it is described that the average flow rate u of the zirconium salt aqueous solution should be determined so that the average residence time in the reaction tube is 1 to 60 seconds. However, it is difficult to mass-produce nanoparticles because the collision probability is low in a laminar flow state, and it is difficult to control the production apparatus because the nanoparticles are produced in an extremely short time of 1 to 60 seconds in the reaction tube. Have

  Furthermore, (21B) is a helical tube type nanoparticle production apparatus, but the reaction tube 202 is merely a helical tube in order to lengthen the reaction time, and the other conditions are the same as (21A). That is, it is desired to flow in a laminar flow state in the reaction tube, and the residence time within the entire length of the helical tube is as short as 1 to 60 seconds. Therefore, the mass production of nanoparticles is inadequate, and the difficulty of production control is a weak point.

The nanoparticle production apparatus of Patent Document 5 is shown in FIG. 22 of the present patent application. In FIG. 22, 310 is a precursor supply unit, 320 is a first heating unit, 321 is a first circulator, 330 is a second heating unit, 331 is a second circulator, 340 is a cooling unit, and 350 is a transfer device. . In addition, as seen in claims 8 and 9, the first heating unit 320 and the second heating unit 330 incorporate a helical reactor-type reactor channel having a diameter of 1 to 50 mm, and the heating unit The coil tube (spiral tube) of the reactor channel is heated by the amount of heat.
In this nanoparticle manufacturing apparatus, first, a precursor solution of metal nanoparticles is supplied to the first heating unit 320 from the precursor supply unit 310 via the transfer device 350, and the first heating unit kept warm by the first circulator 321. The precursor solution is preheated to a temperature within 320 where no nanoparticle formation occurs. Next, the preheated precursor solution is transferred to the second heating unit 330, and in the second heating unit that is kept at a temperature at which nanoparticle generation occurs by the second circulator 331, the nanoparticles are reacted in the reaction channel. Generated. And the produced | generated nanoparticle solution is transferred to the cooling part 340, is cooled, and nanoparticle production | generation is stopped.

JP-A-10-183207 International Publication No. WO2009 / 090846 JP 2005-264199 A JP-T-2006-503790 JP 2008-285749 A

  In the nanoparticle manufacturing apparatus of Patent Document 3, the size of the microchannel 9 is extremely narrow, such as a diameter of several μm to several hundreds of μm, and there is a defect that clogging is likely to occur due to the generated nanoparticles. Even if the metal salt aqueous solution can be continuously supplied, once clogging occurs, the metal salt aqueous solution cannot be passed, and the production of nanoparticles is stopped.

  In the nanoparticle production apparatus of Patent Document 4, since the reaction liquid is in a laminar flow state, it is difficult to mass-produce nanoparticles because the collision probability between particles that generate nanoparticles is small, and 1 to 60 in the reaction tube. Since it is necessary to produce nanoparticles in an extremely short time of seconds, it is difficult to control the flow rate and temperature in such a short time, and the control performance of the entire apparatus is weak.

  In the nanoparticle production apparatus of Patent Document 5, a reaction channel composed of a straight tube or a coiled tube is arranged inside the second heating unit 330, and a method of generating nanoparticles by circulating a precursor solution in the reaction channel is adopted. ing. Therefore, it is structurally very similar to Patent Document 2, and is not suitable for mass production of nanoparticles because the collision probability is low when the flow in the channel is laminar, as in Patent Document 2, and the channel is not suitable. Since it circulates in a short time, the reaction time is short and it is difficult to mass-produce nanoparticles.

  Therefore, the present invention can not only produce nanoparticles having a small diameter, but can simultaneously mass-produce nanoparticles at the same time, and can also shorten or shorten the generation time of nanoparticles. The first object of the present invention is to provide an automatic manufacturing apparatus that performs integrated processing by computer control from raw material liquid production, nanoparticle generation, concentration of the produced liquid, and drying of the concentrated liquid. Objective.

  The present invention has been completed in order to solve the above-mentioned problems. In the first embodiment of the present invention, a raw material liquid for preparing nanoparticles in which a raw material is mixed in a solvent is prepared, and the raw material liquid is distributed. A reaction tube is arranged, the inside of the reaction tube is filled with the same solvent as the raw material liquid and / or the raw material liquid, the temperature of the solvent in the reaction tube is controlled to the nanoparticle synthesis temperature, and the raw material liquid is Supplied to the inflow end of the reaction tube and circulates along the circumferential direction of the inner surface of the outer peripheral wall of the reaction tube while mixing the supplied raw material solution and the solvent of the reaction tube or stirring the raw material solution. While forming a spiral flow that flows from the inflow end to the outflow end, forming nanoparticles from the source material in the spiral flow, and delivering the product liquid containing the nanoparticles from the outflow end of the reaction tube This is a method for producing nanoparticles.

  According to a second aspect of the present invention, in the first aspect, the reaction tube is divided into one or more sections along a flow direction of the raw material liquid, and the inlet side of the section is along the inner surface of the outer peripheral wall. An annular opening that is open in the circumferential direction is formed, and the spiral flow passes through the annular opening to become an annular spiral flow and flows through one or more of the compartments. It is a manufacturing method of the nanoparticle in which the said nanoparticle is formed.

  A third aspect of the present invention is the method for producing nanoparticles according to the first or second aspect, wherein the raw material liquid is preheated within a temperature range where nanoparticles are not synthesized.

  According to a fourth aspect of the present invention, in the first, second, or third aspect, one or more stages of the reaction tubes are configured in series and / or in parallel, and the spiral flow inside each reaction tube is lowered. It is a method for producing nanoparticles selected from a flow, an upward flow, a gradient flow or a horizontal flow.

  According to a fifth aspect of the present invention, in any one of the first to fourth aspects, the nanoparticle is produced by reacting the solvent and the raw material at the synthesis temperature.

  According to a sixth aspect of the present invention, in any one of the first to fourth aspects, the raw material includes a direct raw material and a reducing agent, and the direct raw material is contained in the solvent by the reducing agent. This is a method for producing nanoparticles in which the nanoparticles are produced by reduction.

  According to a seventh aspect of the present invention, in any one of the first to sixth aspects, the raw material liquid manufacturing step, after the production liquid is produced, the production liquid is concentrated to increase the concentration of the nanoparticles. It is a method for producing nanoparticles by adding at least one of a concentrated liquid manufacturing process and a concentrated liquid drying process for further drying the concentrated liquid.

  According to an eighth aspect of the present invention, in the seventh aspect, in the manufacturing step of the concentrated liquid, the product liquid is sprayed into a vacuum container to evaporate the solvent from the product liquid, and the nanoparticles that have flowed down are used. This is a method for producing nanoparticles in which a concentrated liquid having an increased concentration is recovered.

  In a ninth aspect of the present invention, in the seventh or eighth aspect, in the drying step of the concentrated liquid, the concentrated liquid is vacuum-dried in a container and is dried to an extent that at least nanoparticles are not scattered. This is a method for producing nanoparticles.

The tenth aspect of the present invention is a reaction tube filled with a raw material liquid for nanoparticle production in which a raw material substance is mixed in a solvent and / or the raw material liquid, and the solvent and / or the reaction tube. While mixing the temperature controller for controlling the temperature of the raw material liquid to the synthesis temperature of the nanoparticles, the inflow end of the reaction tube to which the raw material liquid is supplied, and the supplied raw material liquid and the solvent of the reaction tube Or a rotor that forms a spiral flow along the inner surface of the outer peripheral wall of the reaction tube while stirring the raw material liquid, and a nanoparticle is formed from the raw material in the spiral flow and includes the nanoparticles. It is a manufacturing apparatus of the nanoparticle comprised from the outflow end of the said reaction tube which discharges a liquid.

  According to an eleventh aspect of the present invention, in the tenth aspect, a rotating shaft arranged at an axial center position of the reaction tube, one or more separators fixed to the rotating shaft so as to be spaced apart from each other, A partition formed between the matching separators or between the separator and the tube end of the reaction tube, the rotor fixed to the rotating shaft in the partition, the outer peripheral edge of the separator, and the reaction tube An annular opening formed between the inner surface of the outer peripheral wall and the spiral flow passes through the annular opening to form an annular spiral flow and flows through the compartment. In the apparatus for producing nanoparticles, the nanoparticles are formed.

  A twelfth aspect of the present invention is the nanoparticle manufacturing apparatus according to the eleventh aspect, wherein the separator has one or more gas vent holes opened in the top plate portion.

  According to a thirteenth aspect of the present invention, in the tenth, eleventh or twelfth aspect, the preheating apparatus preheats the raw material liquid in a temperature range in which nanoparticles are not synthesized before being supplied to the reaction tube. Is an apparatus for producing nanoparticles.

  In a fourteenth aspect of the present invention, in any one of the tenth to thirteenth aspects, one or more stages of the reaction tubes are configured in series and / or in parallel, and the spiral flow inside each reaction tube is a downward flow , A nanoparticle production device selected for upward flow, inclined flow or horizontal flow.

  According to a fifteenth aspect of the present invention, in any one of the tenth to fourteenth aspects, the raw material liquid manufacturing apparatus, the concentration that increases the concentration of the nanoparticles by concentrating the generated liquid after manufacturing the generated liquid A nanoparticle production apparatus to which at least one of a liquid production apparatus and a concentrated liquid drying apparatus for further drying the concentrated liquid is added.

A sixteenth aspect of the present invention is stored in the nanoparticle production apparatus according to any one of the tenth to fifteenth aspects, a computer control apparatus that controls the nanoparticle production apparatus using an electrical signal, and the computer control apparatus. The automatic nanoparticle production apparatus operates according to a program and automatically controls the nanoparticle production apparatus.

According to the first aspect of the present invention, since a raw material solution for producing nanoparticles in which a raw material is mixed in a solvent is prepared, the solvent is simply a solvent for dissolving and dispersing the raw material, and the raw materials are mixed in the solvent. The case where the nanoparticles are synthesized from the above and the case where the solvent is a kind of liquid raw material and the solvent and the raw material react to synthesize the nanoparticles are included. As an example of the former, when the solvent is water and the raw material is a nitrate metal salt / organic substance / reducing agent, there is metal nanoparticles in which the nitrate metal salt is reduced with the reducing agent and organically coated with the organic substance. As an example of the latter, as disclosed in Patent Document 2, when the solvent is alcohol and the raw material is silver carbonate, the alcohol is the solvent and simultaneously acts as a reducing agent / organic substance. There are metal nanoparticles in which the fine silver particles have an organic coating derived from alcohol. Thus, the invention provides a liquid phase production method for a wide range of nanoparticles.
In addition, a reaction tube through which the raw material liquid flows is arranged, the inside of the reaction tube is filled with the same solvent and / or the raw material liquid as the raw material liquid, and the solvent in the reaction tube is set to the nanoparticle synthesis temperature. The temperature is controlled, the raw material liquid is supplied to the inflow end of the reaction tube, and the supplied raw material liquid and the solvent of the reaction tube are mixed. Therefore, the solvent in the reaction tube and the solvent of the raw material liquid are the same solvent. There is no problem even if the raw material liquid and the solvent are mixed. In addition, when the raw material liquid is filled in the reaction tube, the raw material liquid can be stirred. Moreover, since the solvent and / or raw material liquid in the reaction tube is temperature controlled to the synthesis temperature (including heating, heating, constant temperature, and cooling), the supplied raw material liquid immediately transitions to the reaction state, and in the reaction tube Nanoparticle synthesis begins. The higher the synthesis temperature, the faster the nanoparticle synthesis rate, and the synthesis can be started immediately at the time of mixing if the temperature of the raw material liquid is set to a high temperature at which synthesis does not start.
Further, the mixed liquid or the raw material liquid forms a spiral flow that circulates along the circumferential direction of the inner surface of the outer peripheral wall of the reaction tube while flowing from the inflow end to the outflow end. Since the raw material is close to the inner surface of the outer peripheral wall and the heavy raw material is also close to the inner surface of the outer peripheral wall by centrifugal force, nanoparticles are easily synthesized near the inner surface of the outer peripheral wall. If temperature control means such as a tape heater (including heaters, heaters, thermostats, coolers, etc.) are placed on the outer surface of the outer peripheral wall of the reaction tube, the temperature is controlled near the inner surface of the outer peripheral wall with high synthesis efficiency. Nanoparticles can be efficiently synthesized. In addition, since the spiral flow is configured, the time to reach from the inflow end to the outflow end, that is, the reaction time can be adjusted, and the pitch of the spiral flow (distance to advance in one rotation) depends on the length of the reaction tube. By adjusting the reaction time, the reaction time can be variably adjusted from several seconds to several tens of minutes. Further, the spiral flow is close to turbulent flow or somewhat turbulent flow, the probability of collision between particles increases, and the nano reaction is activated, and various nano particle generation reactions can be efficiently realized. This is completely different from the laminar straight pipe system and laminar spiral pipe system as described in the prior art.
In addition, if the product liquid is pushed out from the outflow end by the amount that the raw material liquid is supplied and the raw material liquid is continuously supplied, there is an advantage that the product liquid can also be continuously purified, which realizes mass synthesis of nanoparticles. It is.

According to the second aspect of the present invention, the reaction tube is divided into one or more compartments along the flow direction of the raw material liquid, and the entrance side of the compartment is circumferentially along the inner surface of the outer peripheral wall. An open annular opening is formed, and the spiral flow passes through the annular opening to form an annular spiral flow and flows through one or more of the compartments. A part of the solvent in the reaction tube is mixed, but most of the raw material liquid passes through the annular opening and enters the first compartment, and enters the second compartment from the next annular opening. The raw material liquid flows in an annular spiral flow from the last section to the outflow end. Therefore, synthesis of nanoparticles occurs in a continuous annular spiral flow having a relatively small thickness, and diffusion of the raw material liquid can be suppressed, so that nanoparticles are generated almost according to the concentration of the raw material liquid.
In addition, when passing through the first annular opening, the spiral flow stays while temporarily rotating in the first section, and when passing through the next annular opening, the spiral flow temporarily rotates while rotating in the next section. Since the staying time is longer than that of the spiral flow without compartments, the staying time in the reaction tube becomes longer, and the reaction time for generating nanoparticles can be further extended. Accordingly, the reaction time is the shortest when there are no sections, and can be set longer as the number of sections installed increases.
Further, the heavy material material remains in the annular spiral flow by the helical centrifugal force, and the annular spiral flow located on the inner surface of the outer peripheral wall is efficiently heated by the temperature control means attached to the outer peripheral wall of the reaction tube. The nanoparticle reaction takes place actively in the annular spiral flow, enabling continuous mass synthesis of nanoparticles.

  According to the third aspect of the present invention, since the raw material liquid is preheated within a temperature range in which nanoparticles are not synthesized, it is slightly lower in temperature than the solvent in the reaction tube heated to the synthesis temperature. The raw material liquid set to a high temperature that does not synthesize particles is relatively small in temperature drop even if both liquids are mixed by supplying the raw material liquid, and nanoparticles are immediately generated in the mixed liquid. The production efficiency of nanoparticles increases. The preheating temperature depends on the nanoparticle reaction and can be adjusted according to the raw material liquid.

According to the fourth aspect of the present invention, one or more stages of the reaction tubes are configured in series and / or in parallel, and the spiral flow inside each reaction tube is a downward flow, an upward flow, an inclined flow, or a horizontal flow. You can choose from. When the synthesis density of the nanoparticles is not sufficient only with the first stage reaction tube, the second stage reaction tube can be connected in series to increase the number of series stages with the third and fourth stages. In mass synthesis of nanoparticles, multiple reaction tubes can be arranged in parallel in the first stage, nanoparticles can be produced in parallel in each reaction tube, and multiple reaction tubes can be connected in series in the second stage. is there. Thus, the number of parallel and the number of series can be adjusted according to the purpose of mass production. In one stage, the nanoparticle synthesis time can be shortened, and in multistage, the nanoparticle synthesis time can be lengthened, and the nanoparticle synthesis time can be adjusted freely.
Further, in the case of serial connection, it is possible to adopt a mode in which the downward flow and the upward flow are appropriately adjusted so that the first step is a downward flow and the second step is an upward flow so that the serial flow is easily adjusted. If the vertical direction is defined as the vertical type and the horizontal direction is defined as the horizontal type, the reaction tube has three types of a vertical reaction tube, a horizontal reaction tube, and an inclined reaction tube, and the arrangement can be adjusted as appropriate. .

  According to the fifth aspect of the present invention, there can be provided a method for producing nanoparticles in which the nanoparticles are produced by the reaction of the solvent and the raw material at the synthesis temperature. Nanoparticles as defined in the present invention are particles having a particle size in the range of 1 nm to 1000 nm, regardless of whether the surface of the particles is coated with a modifying substance (for example, an organic substance). In this embodiment, the case where a solvent and a raw material react with each other to produce nanoparticles in a heated state is claimed. For example, as shown in Patent Document 2, when alcohol and silver carbonate react in a heated state, silver nuclei are precipitated from the silver carbonate by the reducing power of the alcohol, and the alcohol-derived organic matter is coated around the silver nuclei. At this time, the alcohol is not only a solvent but also a reducing agent and an organic substance. In this embodiment, all cases where a solvent and a raw material react to generate nanoparticles are included.

  According to the sixth aspect of the present invention, the raw material includes a direct raw material and a reducing agent, and the direct raw material is reduced by the reducing agent in the solvent to produce the nanoparticles. A method for producing nanoparticles is provided. This form corresponds to the case where the solvent does not directly contribute to the nanoparticle formation reaction but only provides a reaction bath. There are many such reaction systems. For example, there is an example in which water is used as a solvent, silver nitrate and an organic substance are directly used as raw materials, and a reducing agent is included. Specifically, silver nitrate is dissolved in water, silver is precipitated by a reducing agent to form a silver nucleus, and nanoparticles in which organic substances are coated around the silver nucleus are generated. In this embodiment, all cases in which the raw material and the reducing agent react directly in the solvent to form nanoparticles are included. A dissolution promoting substance may be added to dissolve the organic substance in water.

  According to a seventh aspect of the present invention, a manufacturing process of the raw material liquid, a manufacturing process of the concentrated liquid that increases the concentration of the nanoparticles by concentrating the generated liquid after manufacturing the generated liquid, and the concentrated liquid The manufacturing method of the nanoparticle which adds any one or more process of the drying process of the concentrate which further dries can be provided. In the present invention, since the nanoparticles are produced by the liquid phase method, a production liquid in which the nanoparticles are dispersed is produced, and the nanoparticle production process means a production liquid production process. In order to obtain a form in which nanoparticles can be used in the liquid phase method, four steps of a raw material liquid production process → a production liquid production process → a production liquid concentration process → a concentrated liquid drying process must be performed. The gist of the present invention lies in the product liquid production process (that is, the nanoparticle production process). In this embodiment, the product liquid production process is continuously added with one or more from the raw material liquid production process, the product liquid concentration process, and the concentrate liquid drying process. A manufacturing method is provided.

  According to the eighth aspect of the present invention, in the manufacturing process of the concentrated liquid, the product liquid is sprayed into a vacuum container to evaporate the solvent from the product liquid, and the concentration of the flowing down nanoparticles increases. A method of producing nanoparticles for recovering a concentrate is provided. The concentrated liquid production process of this embodiment means a concentrated process of the product liquid in which nanoparticles are dispersed. Eventually, the solvent may be evaporated from the product solution to increase the concentration of nanoparticles in the product solution. In this embodiment, when the product liquid is sprayed into the decompression vessel, the solvent in the spray droplets evaporates due to the decompression, and the spray droplets having an increased concentration flow down, and when this is collected, a concentrated liquid is obtained. Increasing the concentration can be achieved not only by reducing the spray droplets but also by providing a plurality of spray operations.

  According to a ninth aspect of the present invention, there is provided a method for producing nanoparticles, wherein in the drying step of the concentrated solution, the concentrated solution is dried in a vacuum in a container and dried to a degree that at least nanoparticles do not scatter. Is done. If the concentrate is vacuum-dried, the solvent can be further removed, so that the concentration of the concentrate can be further increased. However, if the solvent is completely removed, the nanoparticles are scattered, which is not good for health. In this embodiment, the nanoparticles can be dried to the extent that they do not scatter and the nanoparticles can be provided in a wet state. If the slightly wet nanoparticles are stored in a sealed container, the nanoparticles do not scatter in the atmosphere, and care is required for handling, but they can be treated relatively safely.

According to the tenth aspect of the present invention, a reaction tube filled with a raw material liquid for nanoparticle production in which a raw material substance is mixed in a solvent and / or the raw material liquid is filled, the solvent in the reaction tube, and / Or a temperature controller for controlling the temperature of the raw material liquid to the nanoparticle synthesis temperature; an inflow end of the reaction tube to which the raw material liquid is supplied; and the supplied raw material liquid and the solvent of the reaction tube are mixed. A rotor that forms a spiral flow along the inner surface of the outer peripheral wall of the reaction tube while stirring the raw material liquid, and the nanoparticles are formed by forming nanoparticles from the raw material in the spiral flow. An apparatus for producing nanoparticles can be provided which is constituted from the outflow end of the reaction tube for discharging the product liquid.
The apparatus of this embodiment has been developed in order to realize the method for producing nanoparticles described in the first embodiment. First, a reaction tube filled with the same solvent as the raw material liquid for nanoparticle production in which the raw material is mixed in a solvent is provided, so even if the raw material liquid is supplied to the reaction tube, the combination of the solvent and the raw material does not change at all. First, nanoparticles can be produced. Moreover, when filling the said raw material liquid in the inside of the said reaction tube, the said raw material liquid can be stirred and a spiral flow can be formed and a nanoparticle can be manufactured. In this apparatus, the solvent is simply a solvent, and nanoparticles are synthesized from raw materials in the solvent, and the solvent becomes a kind of liquid raw material, and the solvent and the raw material react to synthesize nanoparticles. Both reactions can be realized. As an example of the former, when the solvent is water and the raw material is a nitrate metal salt / organic substance / reducing agent, there is metal nanoparticles in which the nitrate metal salt is reduced with the reducing agent and organically coated with the organic substance. As an example of the latter, as disclosed in Patent Document 2, when the solvent is alcohol and the raw material is silver carbonate, the alcohol is the solvent and simultaneously acts as a reducing agent / organic substance. There are metal nanoparticles in which the fine silver particles have an organic coating derived from alcohol. Thus, it is an invention of an apparatus that realizes a liquid phase production apparatus for a wide range of nanoparticles.
Moreover, since the temperature controller which heats the said solvent of the said reaction tube and / or the said raw material liquid to the synthesis temperature of a nanoparticle is provided, the temperature inside reaction tube has reached the synthesis temperature. Therefore, when the raw material liquid supplied from the inflow end and the solvent of the reaction tube are mixed, or when the raw material liquid is supplied from the inflow end, the raw material liquid immediately reaches the synthesis temperature, and the conditions under which nanoparticles are generated are To establish. The higher the synthesis temperature, the faster the nanoparticle synthesis rate. If the temperature of the raw material liquid is set to a high temperature at which synthesis does not start, synthesis can be started immediately at the time of mixing.
Further, by the rotation of the rotor, the mixed liquid forms a spiral flow that circulates from the inflow end to the outflow end while circling along the circumferential direction of the inner surface of the outer peripheral wall of the reaction tube. The raw material liquid is brought close to the inner surface of the outer peripheral wall of the reaction tube by the centrifugal force of the spiral flow, and the heavy raw material substance is also brought closer to the inner surface of the outer peripheral wall by the centrifugal force. If heating means such as a tape heater is arranged on the outer peripheral wall outer surface of the reaction tube, nanoparticles can be efficiently synthesized in the vicinity of the inner surface of the outer peripheral wall with high heating efficiency. In addition, since the spiral flow is configured, the time to reach from the inflow end to the outflow end, that is, the reaction time can be adjusted, and the pitch of the spiral flow (distance to advance in one rotation) depends on the length of the reaction tube. By adjusting the reaction time, the reaction time can be variably adjusted from several seconds to several tens of minutes. Further, the spiral flow is close to turbulent flow or somewhat turbulent flow, the probability of collision between substances is increased, and nanoreaction is activated, and various nanoparticle generation reactions can be efficiently realized. This is completely different from the laminar straight pipe system and laminar spiral pipe system as described in the prior art.
In addition, if the product liquid is pushed out from the outflow end by the amount that the raw material liquid is supplied and the raw material liquid is continuously supplied, there is an advantage that the product liquid can also be continuously purified, which realizes mass synthesis of nanoparticles. It is.

According to an eleventh aspect of the present invention, a rotating shaft disposed at the axial center position of the reaction tube, one or more separators fixed to the rotating shaft so as to be spaced apart from each other, and adjacent separators Or a partition formed between the separator and the tube end of the reaction tube, the rotor fixed to the rotating shaft in the partition, the outer peripheral edge of the separator, and the outer peripheral wall of the reaction tube An annular opening formed between the inner surface, the spiral flow passes through the annular opening to form an annular spiral flow and flows through the compartment, and the nanoparticles are included in the annular spiral flow. An apparatus for producing nanoparticles in which is formed is provided.
According to the eleventh embodiment, the reaction tube is divided into one or more compartments along the flow direction of the raw material liquid, and each compartment is a region extending from the separator to the next separator, and for each compartment A rotor is fixed to the rotation shaft. Since an annular opening is formed in the outer peripheral edge of the separator, the spiral flow driven by the rotor passes through the annular opening and becomes an annular spiral flow and flows through the compartment. That is, the raw material liquid and the solvent in the reaction tube partially mix on the input side of the first compartment, but most of the raw material liquid passes through the annular opening and enters the first compartment, and from the next annular opening. In the procedure of entering the second section, the raw material liquid becomes an annular spiral flow and travels from the last section to the outflow end. Therefore, synthesis of nanoparticles occurs in a continuous annular spiral flow having a relatively small thickness, and diffusion of the raw material liquid can be suppressed, so that nanoparticles are generated almost according to the concentration of the raw material liquid.
When passing through the first annular opening, the spiral flow stays while temporarily rotating in the first compartment, and when passing through the second annular opening, the spiral flow temporarily stays while rotating within the next compartment. The residence time in the reaction tube is longer than that of the spiral flow without compartments, and it is possible to further extend the nanoparticle production reaction time. Accordingly, the reaction time is the shortest when there are no sections, and can be set longer as the number of sections installed increases. Further, by driving the annular spiral flow, the heavy material material stays in the annular spiral flow by the helical centrifugal force, and the annular member located on the inner surface of the outer peripheral wall by the heating means attached to the outer peripheral wall outer surface of the reaction tube. The spiral flow is heated efficiently, and nanoparticle reactions occur actively in the annular spiral flow, allowing continuous mass synthesis of nanoparticles.

  According to the 12th form of this invention, the said separator can provide the manufacturing apparatus of the nanoparticle which opened the 1 or more gas vent hole in the top-plate part. When the reaction tube is a vertical reaction tube or an inclined reaction tube, when nanoparticles are generated in the spiral flow or the annular spiral flow, a generated gas may be generated or the solvent may be evaporated. When these product gas or evaporative gas rises, they are guided to the top plate, and the product gas or evaporative gas escapes upward from the gas vent hole and is finally liquefied by the cooling device at the top of the reaction tube and does not liquefy. Safe gas is exhausted to the outside by the exhaust device. If the top plate portion is formed in an umbrella shape and a gas vent hole is formed near the center of the top plate portion, the gas rises along the inner surface of the umbrella-shaped top plate portion, and the gas easily escapes upward from the gas vent hole. Become.

  According to a thirteenth aspect of the present invention, the nanoparticle manufacturing apparatus is provided with a preheating device that preheats the raw material liquid in advance within a temperature range in which the nanoparticles are not synthesized before being supplied to the reaction tube. Is provided. According to the third embodiment, since the raw material liquid is preheated within a temperature range in which nanoparticles are not synthesized, the solvent in the reaction tube heated to the synthesis temperature and the nanoparticles are slightly lower in temperature. The raw material liquid set at a high temperature that is not synthesized is relatively low in temperature even when both liquids are mixed due to the supply of the raw material liquid, and nanoparticles are generated immediately in the mixed liquid, Particle generation efficiency increases. The preheating temperature depends on the nanoparticle reaction and can be adjusted according to the raw material liquid.

  According to the fourteenth aspect of the present invention, one or more stages of the reaction tubes are configured in series and / or in parallel, and the spiral flow inside each reaction tube is a downward flow, an upward flow, an inclined flow, or a horizontal flow. An apparatus for producing nanoparticles selected from the above can be provided. When the synthesis density of the nanoparticles is not sufficient only with the first stage reaction tube, the second stage reaction tube can be connected in series to increase the number of series stages with the third and fourth stages. In mass synthesis of nanoparticles, multiple reaction tubes can be arranged in parallel in the first stage, nanoparticles can be produced in parallel in each reaction tube, and multiple reaction tubes can be connected in series in the second stage. is there. Thus, the number of parallel and the number of series can be adjusted according to the purpose of mass production. Further, in the case of serial connection, it is possible to adopt a mode in which the downward flow and the upward flow are appropriately adjusted so that the first step is a downward flow and the second step is an upward flow so that the serial flow is easily adjusted. If the vertical direction is defined as the vertical type and the horizontal direction is defined as the horizontal type, the reaction tube has three types of a vertical reaction tube, a horizontal reaction tube, and an inclined reaction tube, and the arrangement can be adjusted as appropriate. .

  According to a fifteenth aspect of the present invention, the raw material liquid manufacturing apparatus, the concentrated liquid manufacturing apparatus that concentrates the generated liquid and increases the concentration of the nanoparticles after manufacturing the generated liquid, and the concentrated liquid An apparatus for continuously producing nanoparticles can be provided to which any one or more of the apparatus for drying a concentrated solution for further drying is added. In the present invention, since the nanoparticles are produced by the liquid phase method, a production liquid in which the nanoparticles are dispersed is produced, and the nanoparticle synthesis apparatus means a production liquid production apparatus. In order to make nanoparticles usable in the liquid phase method, four devices of raw material liquid production apparatus → product liquid production apparatus → concentrated liquid production apparatus → concentrated liquid drying apparatus are required. The gist of the present invention resides in a product liquid production apparatus (that is, a nanoparticle production apparatus). In this embodiment, the production liquid production apparatus is continuously added with at least one of a raw material liquid production apparatus, a concentrate production apparatus, and a concentrated liquid drying apparatus. A manufacturing apparatus is provided.

  According to a sixteenth aspect of the present invention, the nanoparticle production apparatus according to any one of the tenth to fifteenth aspects, a computer control apparatus that controls the nanoparticle production apparatus using an electrical signal, and the computer control apparatus An automatic nanoparticle production apparatus that operates according to a stored program and automatically controls the nanoparticle production apparatus can be provided. As described in the fifteenth embodiment, the completed form of the present manufacturing apparatus is a four-device combination of raw material liquid manufacturing apparatus → product liquid manufacturing apparatus → concentrated liquid manufacturing apparatus → concentrated liquid drying apparatus. In addition to this, a raw material liquid manufacturing apparatus → product liquid manufacturing apparatus, product liquid manufacturing apparatus → concentrated liquid manufacturing apparatus, product liquid manufacturing apparatus → concentrated liquid drying apparatus, two device combination, raw material liquid manufacturing apparatus → product liquid manufacturing apparatus → concentration There are three device combinations: liquid production device, raw material liquid production device → product liquid production device → concentrated liquid drying device, product liquid production device → concentrated liquid production device → concentrated liquid drying device. Computer controllers are used to provide continuous electronic control of these device combinations.

FIG. 1 is a front view of a first embodiment of a nanoparticle production apparatus according to the present invention, and shows a series-type nanoparticle production apparatus having a first reaction tube (downflow) and a second reaction tube (upflow). FIG. 2 is a front view of a second embodiment of the nanoparticle production apparatus according to the present invention, and shows a single reaction tube (downflow) nanoparticle production apparatus. FIG. 3 is a front view of a third embodiment of the nanoparticle production apparatus according to the present invention, and shows a single reaction tube (upflow) nanoparticle production apparatus. FIG. 4 is a schematic view of a separator used in the nanoparticle production apparatus according to the present invention, in which (4A) is a longitudinal sectional view and (4B) is a plan view. FIG. 5 is a schematic view of a rotor used in the nanoparticle production apparatus according to the present invention, in which (5A) is a longitudinal sectional view and (5B) is a plan view. FIG. 6 is a block diagram of a fourth embodiment of the nanoparticle production apparatus according to the present invention, showing a computer-controlled automatic nanoparticle production apparatus in which a first reaction tube and a second reaction tube are connected in series. FIG. 7 is a block diagram of a fifth embodiment of the nanoparticle production apparatus according to the present invention, and shows a computer-controlled single-particle nanoparticle automatic production apparatus controlled by a computer. FIG. 8 shows a block diagram of an automatic nanoparticle production apparatus showing the first reaction tube and the second reaction tube of FIG. FIG. 9 is a block diagram of the automatic nanoparticle manufacturing apparatus showing the first reaction tube of FIG. FIG. 10 is a block diagram of the automatic nanoparticle manufacturing apparatus showing the second reaction tube of FIG. FIG. 11 is a schematic explanatory diagram of a raw material liquid production unit shown in the nanoparticle automatic production apparatus of FIGS. 6 and 7. FIG. 12 is a schematic explanatory diagram of a product liquid concentrating unit shown in the nanoparticle automatic manufacturing apparatus of FIGS. 6 and 7. FIG. 13 is a schematic explanatory diagram of the concentrated solution drying unit shown in the automatic nanoparticle production apparatus of FIGS. 6 and 7. FIG. 14 is a basic control flowchart of the computer control apparatus. FIG. 15 is a raw material liquid manufacturing subroutine flow chart showing the raw material liquid manufacturing process of the computer controller. FIG. 16 is a nanoparticle synthesis subroutine flow chart showing the nanoparticle synthesis process in the first reaction tube of the computer controller. FIG. 17 is a nanoparticle synthesis subroutine flow chart showing the nanoparticle synthesis process in the second reaction tube of the computer controller. FIG. 18 is a product solution concentration subroutine flow chart showing a product solution concentration process of the computer control device. FIG. 19 is a concentrate drying subroutine flowchart showing the concentrate drying process of the computer controller. FIG. 20 is a schematic explanatory diagram of Patent Document 1 which is a conventional device. FIGS. 21A and 21B are schematic explanatory diagrams of Patent Document 2 which is a conventional device. FIG. 22 is a schematic explanatory diagram of Patent Document 3 which is a conventional device.

<First embodiment>
FIG. 1 is a front view of a first embodiment of a nanoparticle production apparatus according to the present invention, in which a series of nanoparticle production of a first reaction tube 30 (downflow f) and a second reaction tube 40 (upflow k) is performed. Indicates the device. In the following description, after explaining the outline about the structure of 1st Example, the function of each member is demonstrated along the distribution | circulation process of the raw material liquid 18 in the raw material liquid storage tank 14. FIG. In addition, in the 1st reaction tube 30 and the 2nd reaction tube 40, the same code | symbol is attached | subjected to the same member or the member which has the same function, and a part description is abbreviate | omitted. Further, the nanoparticles include not only nanoparticles without a coating layer but also composite nanometal particles in which an organic coating layer is formed around a metal nucleus. Hereinafter, the composite nanometal particles are also simply referred to as “nanoparticles”. .
In the first embodiment shown in FIG. 1, a first reaction tube 30 and a second reaction tube 40 are connected in series, and a first reaction tube indicated by an arrow h via an outflow end 30f and an inflow end 40e communicating with each other. The first product liquid 25 containing the nanoparticles 26 flows in the direction from 30 to the second reaction tube 40. The first reaction tube 30 is composed of a reaction tube head portion 30a and a reaction tube body portion 30g, and one or more temperature controllers 22 are provided around the reaction tube body portion 30g, and a predetermined reaction temperature (synthesis temperature). The solvent 11 and the raw material liquid 18 which are supplied to the reaction tube body 30g can be heated. Furthermore, the raw material liquid storage tank 14 is connected to the upper part of the reaction tube body 30g via the electromagnetic valve 17, the pump 21 and the inflow end 30e, and the raw material liquid is supplied from the raw material liquid storage tank 14 to the direction of the arrow a by the pump 21. The liquid 18 is circulated, and the raw material liquid 18 is supplied into the reaction tube body 30g.
Similar to the first reaction tube 30, the second reaction tube 40 includes a reaction tube head portion 40a and a reaction tube body portion 40g, and one or more temperature controllers 22 are provided around the reaction tube body portion 40g. Thus, the first product liquid 25 supplied from the solvent 11 or the inflow end 40e can be heated to a predetermined reaction temperature (synthesis temperature). Furthermore, the reaction tube body portion 40g communicates with the product liquid storage tank 68 through an outflow end 40f connected to the upper portion thereof, and the product liquid 65 flows in the direction of the arrow n. The product liquid 65 generated in the second reaction tube 40 is stored in the product liquid storage tank 68. That is, in the nanoparticle production apparatus of the first embodiment, the raw material liquid 18 in the raw material liquid storage tank 14 reacts inside the first reaction tube 30 and the second reaction tube 40 connected in series, and the product liquid 65 is produced. The product liquid storage tank 68 is configured to be supplied and stored. In the first embodiment of the nanoparticle production apparatus according to the present invention, each of the first reaction tube 30 and the second reaction tube 40 includes a rotation shaft 52 connected to the rotation device 50 via a rotation connection portion 51. Yes. Each spiral of the raw material liquid 18 supplied to the first reaction tube 30 and the first product liquid 25 supplied to the second reaction tube 40 by the separators 31 and 41 and the rotors 35 and 45 attached to the rotary shaft 52. A feature is that the streams e and j are formed, which will be described later.

  Hereinafter, regarding the first embodiment of the nanoparticle production apparatus shown in FIG. 1, along with the explanation of other members such as the exhaust system, the function of each member is along the flow process of the raw material liquid 18 in the raw material liquid storage tank 14. explain. The raw material liquid 18 is made of a solvent in which the raw material is dispersed and / or dissolved, and before the raw material liquid 18 is supplied, the same solvent 11 as the solvent used for the raw material liquid 18 is the reaction tube of the first reaction tube 30. The body 30g and the reaction tube body 40g of the second reaction tube 40 are filled inside. The solvent 11 is heated and held up to a predetermined reaction temperature by the temperature controller 22. The synthesis temperature (heating temperature) by the temperature controller 22 may be different between the first reaction tube 30 and the second reaction tube 40. For example, in the first reaction tube 30, since the raw material liquid 18 is supplied, the heating temperature is set higher than in the second reaction tube 40, most of the raw material liquid 18 finishes the reaction, and nanoparticles 26 are generated, A first product liquid 25 containing unreacted raw material together with the nanoparticles 26 is supplied to the second reaction tube. Therefore, although the heating temperature by the temperature controller 22 of the second reaction tube 40 can be reacted, it is set lower than the first reaction tube 30, and a slight unreacted portion of the first product liquid 25 reacts to become nano. Set to generate particles. As described above, in the raw material liquid 18, the solvent for dissolving and dispersing the raw material is the same as the solvent 11. For example, when the raw material is composed of a metal nitrate, an organic substance, and a reducing agent, water is used as the solvent 11. Can be used. Further, as described in Patent Document 2, when the raw material is silver carbonate, alcohol is used as the solvent 11.

Next, the reaction process of the raw material liquid 18 in the first reaction tube 30 will be described in detail. First, as shown in FIG. 1, the solvent 11 is filled in the reaction tube body 30g of the first reaction tube 30, and a predetermined reaction is performed by the temperature controller 22 while being stirred by the blades 36 of the plurality of rotors 35. Heated uniformly to temperature. This reaction temperature only needs to be equal to or higher than the reaction start temperature at which the raw material starts to react with the solvent, and is appropriately adjusted according to the flow rate of the raw material liquid 18. The temperature controller 22 includes a band heater disposed around the reaction tube body 30g. The plurality of rotors 35 are attached to a rotating shaft 52 connected to a rotating device 50 via a rotation connecting portion 51, and are rotated in a direction indicated by an arrow d or a reverse direction at a predetermined rotational speed by driving the rotating device 50. be able to. The rotating shaft 50 is stably attached by a bearing 53 made of a bearing, a seal, and the like, and the rotary connecting portion 51 is also made of a bearing, a seal, etc., and the sealing performance in the rotating mechanism of the first reaction tube 30 is maintained. .
When the raw material liquid 18 is preheated to a preheating temperature lower than the reaction start temperature in the raw material liquid storage tank 14, as described above, the electromagnetic valve 17 is opened, and the pump 21 circulates the inflow end 30e in the direction of arrow a. The solvent 11 at the reaction temperature is supplied to the reaction tube body 30g to be stirred. In the reaction tube body 30g, a region between the separator 31 and the separator 31 below the partition 31 is referred to as a section 39. A plurality of rotors are provided inside the reaction tube body 30g, and each section 39 has one blade 36. 35 is disposed. The section 39 at the lowermost part of the reaction tube body 30g has a region 39 between the separator 31 and the bottom surface of the reaction tube body 30g. Therefore, the raw material contained in the raw material liquid 18 does not diffuse immediately below the reaction tube body 30g, and the raw material liquid 18 is formed between the outer peripheral edge 32b of the separator 31 and the inner surface of the reaction tube body 30g. Pass through the annular opening 32d. The raw material liquid 18 is stirred together with the solvent 11 and passes through the annular opening 32d by forming an annular spiral flow e while being mixed. Therefore, when the raw material liquid passes through the section 39, it is stirred and mixed by the rotor 35 to form an annular spiral flow e, and flows down while reacting with the solvent 11 at the reaction temperature as the downward flow f. . Since the annular spiral flow e is formed, a heavy raw material is brought close to the inner surface of the reaction tube body 30g by centrifugal force, and nanoparticles are synthesized with high efficiency in the vicinity of the inner surface. Furthermore, by forming the annular spiral flow e, the time to reach the outflow end 30f from the inflow end 30e, that is, the reaction time can be adjusted. Although depending on the length of the reaction tube body 30g, the reaction time can be set to several seconds by adjusting the pitch of the spiral flow e (distance to advance in one rotation) according to the number of sections 39, the rotation speed of the rotor 35, and the like. Variable adjustment up to several tens of minutes is possible. The raw material liquid 18 partially mixes with the solvent 11 on the input side of the first compartment 39, but most of the raw material liquid 18 enters the first compartment 18 and enters the second compartment 39 below, and the annular spiral flow While holding e, head toward the outflow end 30f. Therefore, the diffusion of the raw material liquid 18 can be suppressed, and nanoparticles are generated almost according to the concentration of the raw material liquid 18. The product gas g generated by the reaction between the raw material and the solvent rises through the gas vents 32a of the separator 35 in each section 39 of the reaction tube body 30g, and is cooled by the reaction tube head 30a. . The cooling mechanism will be described later.

In the first embodiment shown in FIG. 1, as described above, the first reaction liquid 25 is supplied from the inflow end 40e connected to the lower portion of the reaction tube body 40g of the second reaction tube 40. In the reaction of the first reaction tube 30, nanoparticles 26 are generated, but the unreacted raw material is contained in the first reaction liquid 25, and the reaction of the raw material is completely or almost completely performed in the second reaction tube 40. Then, the product liquid 65 containing the nanoparticles 26 is supplied from the second reaction tube 40 to the product liquid storage tank 68 and stored. Also in the reaction tube body 40g of the second reaction tube 40, a section 49 that is a region from the bottom surface of the reaction tube body 40g to the intermediate separator 41 is formed, and above that is a region from the separator 41 to the separator 41. A compartment 49 is formed. In the upper section 49, a rotor 45 having a stirring blade 46 is attached to a rotating shaft 52, and the rotating shaft 45 is rotated in the direction of arrow r or in the reverse direction. The first product liquid 25 is stirred and mixed. In the initial stage, the reaction tube body 40g is filled with the solvent 11 heated to the synthesis temperature (reaction temperature), and the first product liquid 25 is supplied from the inflow end 40e. Although not shown, an electromagnetic valve and a flow rate control device can be disposed between the outflow end 30f and the inflow end 40e, and a more appropriate amount of the first product liquid 25 can be appropriately supplied. . In the reaction tube body 40g of the second reaction tube 40, an upward flow k is formed, but an annular spiral flow j is formed by the same mechanism as that of the first reaction tube 30. The rotation mechanism of the rotor 45 in the second reaction tube 40 is the same as that of the first reaction tube 30, and detailed description thereof is omitted.
An annular opening 42d is provided between the inner surface of the reaction tube body 40g in the second reaction tube 40 and the outer peripheral edge of the separator 41 having the top plate 42, and passes through the annular opening 42d for the first reaction. Similar to the tube 30, the upward flow k is stirred and mixed in the section 49, thereby forming an annular spiral flow j. Therefore, it is close to the inner surface of the reaction tube body 40g where the heavy raw material is heated by centrifugal force, and the nanoparticles 26 are synthesized with high efficiency in the vicinity of the inner surface. In the first reaction tube 30 and the second reaction tube 40, The raw material liquid 18 reacts almost completely, and the generated liquid 65 in which the nanoparticles 26 are generated is supplied to the generated liquid storage tank 68.

Here, the cooling means in the reaction tube heads 30a and 40a will be described. In FIG. 1, as described above, in the first reaction tube 30 and the second reaction tube 40, the raw material liquid 18 and the first product liquid 25 containing the same solvent as the solvent 11 are heated. 30a and 40a are provided with a cooling means for the evaporated solvent 11. This cooling means is provided with a spiral tube 23b indicated by a dotted line that circulates cold water supplied from the product gas cooling device 23 through the input tube 23a and collects it from the output tube 23c to the product gas cooling device 23. The Since the cooling water circulates and the spiral tube 23b is cooled, the solvent 11 evaporated in the reaction tube barrels 30g and 40g reaches the periphery of the spiral tube 23b or the vicinity thereof, and a part of the solvent 11 is circularly received by heat exchange. It is liquefied and dripped at the parts 30b and 40b. The solvent 11 stored in the annular receiving portions 30b and 40b is appropriately discharged and collected from the drain valves 30c and 40c. From the reaction tube barrels 30g and 40g, the generated gases g and m generated with the reaction rise to the inside of the reaction tube heads 30a and 40a, and the generated gases g and m are also cooled. For example, when the raw material is silver carbonate and the solvent 11 is alcohol, carbon dioxide gas is generated as the product gas g and m and rises to the inside of the reaction tube heads 30a and 40a.
In each reaction tube head 30a, 40a of the first reaction tube 30 and the second reaction tube 40, each pressure P1, P2 is monitored by a pressure gauge (not shown), and an exhaust device 24 connected to the exhaust tube 24a. Thus, the pressures P1 and P2 can be adjusted independently. The first reaction tube 30 and the second reaction tube 40 are each provided with a liquid level gauge 64, and the height of the liquid level is controlled by the pressures P1 and P2. That is, the distances to the liquid level gauges 64 indicated by arrows b are measured, and the pressures P1 and P2 are independently adjusted by the exhaust device 24 so as to keep the predetermined liquid level, and applied in the direction of the arrow c. Pressed. An ultrasonic liquid level gauge or the like is used as the liquid level gauge 64, and a pressure holding valve or the like that can control the pressure is used as the exhaust device 24. The gas exhausted from the exhaust device 24 may contain a small amount of the vapor of the solvent 11 together with the product gas g, and is preferably completely liquefied and removed by a heat exchanger or the like.

<Second embodiment>
FIG. 2 is a front view of a second embodiment of the nanoparticle production apparatus according to the present invention, and shows a single reaction tube (downflow) nanoparticle production apparatus. In the second embodiment, the reaction tube is composed only of the first reaction tube 30 shown in FIG. 1, and the difference from the first embodiment is that the product liquid storage tank 68 is connected to the outflow end 30f, and the product liquid 65 is It is in the point where it is stored. Therefore, the same reference numerals are given to the same members, and detailed description is omitted unless there is a special difference.
In the second example of FIG. 2, the reaction between the raw material and the solvent 11 in the raw material liquid 18 is completed or almost completed in the first reaction tube 30, and nanoparticles 26 are generated. The reaction time is appropriately determined by adjusting the supply flow rate of the raw material liquid 18 by the pump 21, adjusting the stirring state by the rotation speed of the rotating device 50, adjusting the synthesis temperature (heating temperature) by the temperature controller 22, adjusting the pressure P 1 by the exhaust device 24, etc. The nanoparticles 26 are generated from the raw material liquid 18 only by the first reaction tube 30, and the product liquid 65 is stored in the product liquid storage tank 68. It is the same as that of the first reaction tube 30 shown in FIG. 1 that the downward flow of the raw material liquid 18 is stirred and mixed as an annular spiral flow e (also referred to as a downward spiral flow) and flows down. Description of is omitted.

<Third embodiment>
FIG. 3 is a front view of a third embodiment of the nanoparticle production apparatus according to the present invention, and shows a single reaction tube (upflow) nanoparticle production apparatus. In the third embodiment, the reaction tube is composed only of the second reaction tube 40 shown in FIG. 1, and the difference from the first embodiment is that the bottom of the second reaction tube 40 is connected to the bottom of the second reaction tube 40 via the electromagnetic valve 17 and the pump 21. The raw material liquid storage tank 14 is connected, and the raw material liquid 18 is supplied from the lower part of the second reaction tube 40 from the raw material liquid storage tank 14. Similarly, the same members are denoted by the same reference numerals, and detailed description thereof is omitted.
In the third embodiment of FIG. 3, the raw material liquid 18 is directly supplied to the second reaction tube 40, and an upward flow k (also referred to as an upward annular spiral flow) is formed by the pump. As in the case of the two reaction tubes 40, an annular spiral flow j (ascending spiral flow) that rises in each section 49 is formed. In the third embodiment, the reaction between the raw material and the solvent 11 in the raw material liquid 18 is completed or almost completed in the second reaction tube 40, and the nanoparticles 26 are generated. Similar to the second embodiment, the supply flow rate of the raw material liquid 18 by the pump 21, the adjustment of the stirring state by the rotation speed of the rotating device 50, the adjustment of the synthesis temperature (heating temperature) by the temperature controller 22, the pressure P1 by the exhaust device 24 The reaction time can be appropriately set by adjusting the amount of the liquid, and the nanoparticles 26 are generated from the raw material contained in the raw material liquid 18 only by the first reaction tube 30, and the generated liquid 65 containing the nanoparticles 26 is generated as the generated liquid. It is supplied to the storage tank and stored. It is the same as the second reaction tube 40 shown in FIG. 1 that the upward flow k of the raw material liquid 18 is stirred and mixed as an annular spiral flow j (also referred to as upward spiral flow) and reacted while rising. The above description is omitted.

  FIG. 4 is a schematic view of a separator 31 (41) used in the nanoparticle production apparatus according to the present invention, (4A) is a longitudinal sectional view, and (4B) is a plan view. The separators 31 and 41 shown in FIGS. 1 to 3 have the same structure, and the “separator” is denoted by reference numeral 31 (41). Similarly, the first reaction tube 30 and the second reaction tube in FIG. 40, the symbol of the second reaction tube 40 is shown in parentheses. The separator 31 (41) includes a top plate portion 32 (42) and an annular portion 33 (43). The annular portion 33 (43) is fixed to the rotating shaft 52 by a fastening bolt 34 (44), and the separator 31 (41). Rotates together with the rotating shaft 52 in the direction of the arrow d (r). As described above, the top plate portion 32 is provided with the gas vent holes 32a (42a), and the generated gas generated in the reaction can be discharged upward. The size and number of the gas vent holes 32a (42a) are adjusted according to the amount of generated gas generated and the raw material liquid to be supplied. An annular opening 32d (42d) is formed between the outer peripheral edge 32b (42b) of the top plate 32 (42) and the outer peripheral wall 30h (40h) of the reaction tube 30 (40). The upward flow k (or ascending annular spiral flow) or the downward flow f (or downward annular spiral flow) flows through the portion 32d (42d).

  FIG. 5 is a schematic view of a rotor 35 (45) used in the nanoparticle production apparatus according to the present invention, in which (5A) is a longitudinal sectional view and (5B) is a plan view. 4, the rotors 35 and 45 have the same structure in the first reaction tube 30 and the second reaction tube 40 shown in FIGS. 1 to 3, and the reference numerals of the second reaction tube 40 are shown in parentheses. Yes. The rotor 35 (45) includes a blade 36 (46) and an annular portion 37 (47). The annular portion 37 (47) is fixed to the rotating shaft 52 by a fastening bolt 38 (48), and the blade 36 (46) is provided. It rotates with the rotating shaft 52, and a solvent, a raw material liquid, etc. are stirred and mixed.

<Fourth embodiment>
FIG. 6 is a block diagram of a fourth embodiment of the nanoparticle production apparatus according to the present invention, and shows a nanoparticle automatic production apparatus 1 in which a computer-controlled first reaction tube 30 and second reaction tube 40 are connected in series. The nanoparticle automatic manufacturing apparatus 1 includes a computer control device 2, a raw material liquid manufacturing unit 10, a nanoparticle manufacturing unit 20, a product liquid concentrating unit 70, and a concentrated liquid drying unit 90, and is connected to the computer control device 2 by terminals Q1 to Q4. Has been. That is, the terminals Q1 to Q4 of the raw material liquid production unit 10, the nanoparticle production unit 20, the product liquid concentration unit 70, and the concentrated liquid drying unit 90 correspond to the terminals Q1 to Q4 of the I / O port 8, respectively. Connected and automatically controlled by the computer controller 2, the nanoparticles can be manufactured automatically and continuously or intermittently.
The computer control device 2 includes a ROM 3 in which a program is recorded, a CPU 4 that performs calculation, a RAM 5 that inputs and outputs a calculation result, an INPUT 6 that inputs a set value and an operation mode from the outside, and an OUTPUT 7 that outputs measurement data and an operation state. And an I / O port 8 that inputs / outputs data to / from the CPU 4, converts INPUT 6 data into digital signals, and outputs each measurement data to the OUTPUT 7. Via the terminals Q1 to Q4 connected to the I / O port 8, the terminals Q1 to Q4 of the computer control device 2 are generated as a terminal Q1 of the raw material liquid manufacturing unit 10 and a terminal Q2 of the nanoparticle manufacturing unit 20, respectively. It is connected to the terminal Q3 of the liquid concentrating unit 70 and the terminal Q4 of the concentrated liquid drying unit 90. When a set value or operation mode is input from the OUTPUT 7 from the outside, a command is output from the I / O port 8 via the terminals Q1 to Q4 by calculation of the CPU 4, and from each part the I / O port via the terminals Q1 to Q4 Is fed back to 8 and output to the CPU 4. Therefore, if a set value or an operation mode is input from INPUT 6, nanoparticles are automatically manufactured, and the operation status of the automatic nanoparticle manufacturing apparatus 1 can be monitored by OUTPUT 7. The computer control device 2 can be a commercially available personal computer, an I / O port, a PID control device, or a combination thereof.

The raw material liquid production unit 10 in FIG. 6 is supplied with a solvent 11 and a raw material substance 12 to produce a raw material liquid, a raw material liquid production machine 13, a cooling device 15 that cools the raw material liquid of the raw material liquid production apparatus 13, The raw material liquid is stored, and is constituted by a raw material liquid storage tank 14 in which the raw material liquid is preheated to a predetermined temperature not higher than the reaction start temperature by the preheating device 16. This raw material liquid storage tank 14 is described in FIGS. 1 to 3 and has a similar function. The raw material liquid production machine 13 disperses, mixes and dissolves the raw material 12 in the solvent 11. The raw material liquid production machine 13 includes a bead mill device, a mixer, and the like. For example, in the bead mill device, the aggregated raw material is uniformly pulverized with fine bead particles in a solvent and dispersed in the solvent.
In response to a command from the computer control device 2, the raw material liquid production machine 13 is driven, and the solvent 11 and the raw material substance 12 are automatically supplied to the raw material liquid production machine 13 at a predetermined flow rate, and the raw material substance 12 is supplied to the solvent 11. Dispersed / mixed / dissolved raw material liquid is produced. At the same time, the cooling device 15 is driven, and the raw material liquid is manufactured while being cooled so that the raw material liquid does not react. The raw material liquid generated in a predetermined time is supplied to the raw material storage tank 18 and is held at a predetermined temperature below the reaction start temperature by the preheating device 16. For example, when the raw material is silver carbonate and the solvent is alcohol, the temperature is maintained at about 60 ° C. A predetermined amount of a raw material liquid having a predetermined preheating temperature is stored, and the fact that the raw material liquid can be supplied is transmitted to the computer control device 2.

In FIG. 6, the nanoparticle production unit 20 includes most of the configuration of the first embodiment shown in FIG. 1, and includes the first reaction tube 30, the second reaction tube 40, the product liquid storage tank 68, and the like. The attached pump 21, heating device (temperature controller) 22, generated gas cooling device 23, exhaust device 24, rotating device 50 and electromagnetic valve 69 are described in FIG. 1, and the details thereof are described. Omitted.
The first reaction tube 30 and the second reaction tube 40 are filled with the solvent 11 in advance, and the heating device (temperature controller) 22, the product gas cooling device 23, the exhaust device 24, and the rotating device 50 are driven. The temperature of the solvent 11 in the first reaction tube 30 and the second reaction tube 40 reaches the reaction temperature, the liquid level is at a predetermined height, and the pressure is kept below a predetermined value by the exhaust device 24 having a pressure holding valve. Is transmitted from Q2 to the computer controller 2. That is, the fact that it is possible to supply the raw material liquid to the nanoparticle manufacturing unit 20 is transmitted to the computer control device 2, and the pump 21 is driven to generate a signal for opening the electromagnetic valve 17 of the raw material liquid manufacturing unit 10. Sent. In the continuous operation, since the raw material liquid is continuously manufactured and the same amount of raw material liquid as the amount supplied to the first reaction tank 30 is manufactured, the electromagnetic valve 17 is kept almost always open in the continuous operation. The supply amount of the raw material liquid is maintained at a predetermined value by the pump 21. As described in the explanation of FIG. 1, the reaction process in the nanoparticle manufacturing unit 20 is formed by forming an annular spiral flow in the first reaction tube 30 and the second reaction tube and heating, thereby generating nanoparticles. A product liquid composed of a solvent containing nanoparticles is stored in the product liquid storage tank 68.
Here, the temperature, vapor pressure, and liquid level of the first reaction tube and the second reaction tube are measured and transmitted to the computer control device 2 via Q2, and the heating device 22 and product gas cooling are performed by feedback control. A control signal is transmitted to the device 23 and the exhaust device 24, and the temperature, vapor pressure, and liquid level are automatically adjusted, and the administrator can always monitor by the OUTPUT7.
Further, the nanoparticle manufacturing unit 20 is provided with a liquefaction device 60, which is controlled by the computer control device 2. The gas exhausted from the exhaust device 24 contains the vapor of the solvent 11 that has not been completely removed by the product gas cooling device 23 together with the product gas generated by the reaction, and this vapor is liquefied by a heat exchanger or the like. It is liquefied by the device 60. For example, the solvent 11 is made of alcohol or water, and these substances can be completely liquefied. Accordingly, the gas exhausted from the exhaust device 34 is separated into the solvent 11 and the product gas, the product gas is released by the safety gas atmospheric release 66, and the solvent 11 is recovered by the solvent recovery 67.

The product liquid concentrating unit 70 in FIG. 6 includes a product liquid concentrating device 80, a concentrating liquid storage tank 75, an exhaust device 71, a liquefying device 72, a solvent recovery 73, a safety gas atmospheric discharge 74, and an electromagnetic valve 76, and a terminal Q3 A control signal is transmitted from the computer control device 2 via this, and a measured value and an operating state are fed back. In the nanoparticle manufacturing unit 20, when a predetermined amount of product liquid is stored in the product liquid storage tank 68, the electromagnetic valve 69 is opened, and the product liquid is supplied to the product liquid concentrating device 80. At this stage, the product liquid concentrating device 80 is set in a state in which the product liquid can be supplied, and the solvent 11 is removed from the product liquid to concentrate the product liquid and increase the nanoparticle concentration. Is obtained. This concentrated liquid is supplied and stored from the product liquid concentrating device 80 to the concentrated liquid storage tank 75, and when a predetermined amount is stored, the electromagnetic valve 76 is opened and supplied to the concentrated liquid drying unit 90. A specific example of the product liquid concentrating device 80 will be described later. By the exhaust device 71 connected to the product liquid concentrating device 80, the product gas containing the solvent 11 flows to the liquefying device 72, and the solvent 11 is liquefied by the liquefying device 72. The solvent 11 is recovered by the solvent recovery 11, and the product gas from which the solvent 11 has been removed is released into the atmosphere by a safe gas release 74.
The concentrate drying unit 90 includes a concentrate drying device 91, a solvent recovery 92, and a nanoparticle recovery 93, and is controlled by the computer control device 2 via a terminal Q4. In the concentration drying apparatus 91, the solvent 11 contained in the concentrate is further removed to form a dry state, and the nanoparticles are recovered by the nanoparticle recovery 93. The solvent 11 removed by drying is recovered by a solvent recovery 92.

<Fifth embodiment>
FIG. 7 is a block diagram of a fifth embodiment of the nanoparticle production apparatus according to the present invention, showing a computer-controlled automatic nanoparticle production apparatus for a single reaction tube 30 (40). In FIG. 7, the same members as those in FIG. 6 are denoted by the same reference numerals, and a part of the description is omitted. Furthermore, since the fifth embodiment of FIG. 7 is the same as the fourth embodiment of FIG. 6 except for the nanoparticle manufacturing section 20, the nanoparticle manufacturing section 20 will be described.
In the nanoparticle production unit 20 of FIG. 7, as shown in FIGS. 2 and 3, the reaction tank 30 (40) is single, and the first reaction tank 30 of FIG. 2 or the second reaction tank 40 of FIG. Is disposed. Therefore, the operations other than the reaction process and the reaction tank 30 (40) are the same as those in the fourth embodiment shown in FIG. In the nanoparticle production unit 20 of FIG. 7, since the reaction basket 30 (40) is single, as described with respect to the embodiment of FIGS. 2 and 3, the single reaction basket 30 (40) Generation takes place. Accordingly, the synthesis temperature (ie, heating temperature) by the temperature controller 22, the supply amount from the raw material liquid storage tank 14 by the pump 21, and the stirring speed by the rotating device 50 are adjusted, and a single reaction tank 30 (40) is used. The reaction rate and reaction time are controlled by the computer controller 2 so that the production of nanoparticles is completed.

  FIG. 8 shows a block diagram of an automatic nanoparticle production apparatus showing the first reaction tube and the second reaction tube of FIG. FIG. 8 is substantially the same as the block diagram of the automatic nanoparticle production apparatus of FIG. 6 based on the first embodiment shown in FIG. The description of the configuration and its operation is substantially the same as the description of FIGS. To explain in part, the raw material liquid storage tank 14 is provided with a preheating device 16 and a raw material liquid production machine 13, and the raw material liquid production machine 13 is supplied with the solvent 11 and the raw material substance 12. The exhaust device 24 is provided with a liquefying device 60, which separates the solvent 11 and the generated gas, releases the generated gas to the atmosphere by the safety gas atmospheric release 66, and recovers the solvent 11 by the solvent recovery 67. A product liquid concentrating device 80 is attached to the product liquid storage tank 68 via an electromagnetic valve 69, from which the concentrate is supplied to the concentrate storage tank 75, and the concentrated liquid is concentrated liquid dried. It is dried by the apparatus 91 and recovered by the nanoparticle recovery 91. The solvent 11 removed by the concentrated liquid drying device 91 is recovered by a solvent recovery 92.

  FIG. 9 is a block diagram of the automatic nanoparticle manufacturing apparatus showing the first reaction tube of FIG. FIG. 9 is substantially the same as the block diagram of the automatic nanoparticle manufacturing apparatus of FIG. 7 based on the second embodiment shown in FIG. The description of the configuration and the operation thereof is substantially the same as the description of FIG. 2, FIG. 7, and FIG. To explain in part, on the inflow side of the first reaction tank 30 in FIG. 2, the preheating device 16 and the raw material liquid production machine 13 are attached to the raw material liquid storage tank 14, and on the outflow side of the first reaction tank 30, A product liquid concentrating device 80 is attached to the product liquid storage tank 68 via an electromagnetic valve 69. Further, the exhaust device 24 is provided with a liquefying device 60, which separates the solvent 11 and the generated gas, releases the generated gas from the safe gas atmospheric release 66, and recovers the solvent 11 by the solvent recovery 67. Other configurations and operations are the same as those in FIG. 8, and thus further description is omitted.

  FIG. 10 is a block diagram of the automatic nanoparticle manufacturing apparatus showing the second reaction tube of FIG. FIG. 10 is substantially the same as the block diagram of the automatic nanoparticle manufacturing apparatus of FIG. 7 based on the third embodiment shown in FIG. The description of the configuration and its operation is substantially the same as the description of FIG. 3, FIG. 7, and FIG. To explain in part, on the inflow side of the second reaction tank 30 of FIG. 3, the preheating device 16 and the raw material liquid production machine 13 are attached to the raw material liquid storage tank 14, and on the outflow side of the second reaction tank 30, A product liquid concentrating device 80 is attached to the product liquid storage tank 68 via an electromagnetic valve 69. Further, the exhaust device 24 is provided with a liquefying device 60, which separates the solvent 11 and the generated gas, releases the generated gas from the safe gas atmospheric release 66, and recovers the solvent 11 by the solvent recovery 67. Other configurations and operations are the same as those in FIG. 9, and thus further description is omitted.

FIG. 11 is a schematic explanatory diagram of the raw material liquid production unit 10 shown in the automatic nanoparticle production apparatus of FIGS. 6 and 7. The raw material liquid production unit 10 includes a mixer 18 a that mixes the solvent 11 and the raw material substance 12, a three-way valve 18 b that sends the mixed liquid aa to the raw material liquid storage tank 14 or the bead mill 19, and a motor M that drives the bead mill 19. It has. When the raw material 12 or the direct raw material / reducing agent contained in the raw material 12 is easily dispersed / dissolved by the mixer 18a, the three-way valve 18a causes the raw material liquid to flow in the direction of the arrow cc and the raw material liquid storage tank 14 To be stored. For example, when the raw material is silver nitrate directly, it is easily dissolved in water as the solvent 11.
When the raw material 12 is agglomerated into relatively large particles, after mixing with the solvent 11 by the mixer 18a, the three-way valve 18b is opened to flow to the bead mill 19 side, and the mixing is performed by the mixer 18a. The liquid aa is supplied to the bead mill 19. The bead mill 19 includes a dispersion unit 13a, a centrifuge unit 13b, and a chilled water pipe 13c. The dispersion unit 13a and the centrifuge unit 13b are rotated in the direction of the arrow rr or in the reverse direction by driving the motor M. When the mixed liquid aa is supplied to the bead mill 19 and the dispersion unit 13b rotates, the bead particles collide, and the aggregated raw material 12 is pulverized and dispersed in the solvent 11 to produce a suitable dispersion. The aggregated raw material 12 is pulverized to a size of about several tens of microns to submicrons. This dispersion contains bead particles, circulates in the direction of the arrow bb, and is supplied to the centrifugal separator 13b. Here, the bead particles are collected by centrifugation and fed back to the dispersion unit 13a as indicated by an arrow dd. While the bead mill 19 is in operation, cooling water is supplied from the cooling device 15 to the chilled water pipe 13c so that the reaction between the solvent 11 and the raw material 12 does not proceed, and the bead particles are dispersed in the dispersion unit 13b or the centrifuge unit 13b. Continue to cool the raw material liquid from which water is removed. The raw material liquid flows from the centrifugal separator 13b in the direction of the arrow cc, is supplied to the raw material liquid storage tank 14, and is stored in a predetermined amount. As described above, the raw material liquid stored in the raw material liquid storage tank 14 is heated and controlled by the preheating device 16 to a preheating temperature lower than the reaction start temperature. Further, when the preparation for the reaction of the nanoparticle production unit is completed, the electromagnetic valve 17 is opened, and the raw material liquid is supplied to the nanoparticle production unit by a pump.

FIG. 12 is a schematic explanatory diagram of the product liquid concentrating unit 80 shown in the automatic nanoparticle manufacturing apparatus of FIGS. 6 and 7. The product liquid concentrating unit 80 includes a spray tube 81, a decompression large container 85, and a support member 89 that supports the decompression large container 85. A spray device 83 having a spray hole 83a is provided at the outlet end 81b of the spray tube. Installed. The spray pipe 81 is supplied with the product liquid 65 containing the nanoparticles 26 from the inlet end 81 a, and the inlet end 81 a is connected to the product liquid storage tank 68 via the pump P and the electromagnetic valve 69. Accordingly, the electromagnetic valve 69 is opened, and the pump 65 is driven, so that the generated liquid 65 is pumped and supplied in the direction of the arrow s. A large container taper portion 87 is provided at the bottom of the decompression large container 85, and a discharge port 88 is provided in the large container taper portion 87. If this discharge port 88 is closed by an electromagnetic valve or the like, the large pressure reduction container 85 can be kept sealed except for the discharge port 86 provided in the upper part of the pressure reduction large container 85. The spray tube 81 and the large decompression container 85 can be circulated through the outlet end 81b and the spray hole 83a of the spray device 83. However, when the spray tube 81 and the decompression large container 85 are closed by an electromagnetic valve or the like (not shown), The distribution of 85 is blocked. Therefore, when the outlet end 81b of the spray pipe 81 and the discharge port 88 of the decompression large container 85 are in the closed state, if the exhaust device 71 composed of a vacuum pump exhausts from the discharge port 86, the inside of the large container 85 becomes a vacuum state. Become.
Further, when the outlet end 81 b of the spray pipe 81 and the discharge port 88 of the large container 85 are closed, the product liquid 65 is not supplied into the spray pipe 81 by the pump P. When the degree of vacuum inside the decompression large container 85 reaches a predetermined value or less, the outlet end 81b is opened and the pump P is activated. Accordingly, the product liquid 65 from the spray pipe 81 is sprayed from the spray hole 83a of the sprayer 83 into the vacuum large container 81 which is a vacuum. At this time, the solvent is volatilized inside the decompression large container 81 and is exhausted to the liquefying device 72 by the exhaust device 71. In the liquefying device 72, the solvent volatilized by a heat exchanger or the like is liquefied and the solvent is recovered by the solvent recovery 73. Further, the product gas from which the solvent has been removed by liquefaction is released into the atmosphere by a safe gas atmosphere release 74. Therefore, the product liquid 65 is concentrated, collected in the direction of the arrow w by the large container taper 87, and the concentrated liquid 78 is stored. When the concentrated liquid 78 reaches a predetermined amount, the outlet end 81b of the spray tube 81 is closed, the exhaust device 71 stops, and the concentrated liquid 78 flows from the discharge port 88 of the decompression large container 85 in the direction of the arrow X to concentrate. It is stored in the liquid storage tank 75. In this concentrated liquid 78, the nanoparticles are present at a higher density than in the produced liquid.

FIG. 13 is a schematic explanatory view of the concentrated solution drying unit 90 shown in the nanoparticle automatic manufacturing apparatus of FIGS. 6 and 7. As described above, the concentrate drying unit 90 includes the concentrate drying device 91, the solvent recovery 92, and the nanoparticle recovery 93, and further, a vacuum exhaust device 98 is provided between the concentrate drying device 91 and the solvent recovery 92. A liquefaction device 99 and a safe gas atmosphere release 99a are provided. The concentrated liquid 78 is supplied from the concentrated liquid storage tank 75 to the hopper 94 of the concentrated liquid drying apparatus 91 by the pump P through the electromagnetic valve 76. The concentrated liquid drying device 91 is provided with a rotary table 95 and a temperature control device 96 for heating the rotary table 95. The concentrated liquid 78 dropped on the turntable 95 by a predetermined amount from the hopper 94 is dried on the heated turntable 95 to form dry nanoparticles 97. The dried nanoparticles 97 are automatically recovered by the nanoparticle recovery 93 by suction or the like.
The solvent evaporated by drying is exhausted by the vacuum exhaust device 98, cooled and liquefied by the liquefying device 99, the solvent is recovered in the solvent recovery 92, and the product gas from which the solvent has been removed is discharged by the safe gas atmospheric release 99a. Released into the atmosphere.

  FIG. 14 is a basic control flowchart of the computer control apparatus. Hereinafter, in the basic flowchart, the same reference numerals are given to the same devices and members as those shown in the above-described device description and block diagram. 14 to 19, N means “No” and Y means “Yes”. When the basic control flow starts, it is determined in step S1 whether or not initial settings such as reaction temperature, reaction amount, and operation time have been set. If N, the process returns to the previous stage of step S1. In step S1, in the case of Y, the process proceeds to step S2, and it is determined whether or not the raw material liquid is manufactured. If the predetermined amount of the raw material liquid is already present, the answer is No and the process proceeds to step S3. When there is no raw material liquid or when the predetermined amount is not reached, Step S2 becomes Yes, the process proceeds to a subroutine SUB1, and the process proceeds to the raw material liquid manufacturing process. When a predetermined amount of the raw material liquid is manufactured in this raw material liquid manufacturing process, the process proceeds to step S3. In step S3, it is determined whether or not nanoparticles are to be manufactured. Similarly, if a predetermined amount of product liquid containing nanoparticles already exists, N is determined, and the process proceeds to step S4. If step S3 is Y, the process proceeds to subroutine SUB2. In the subroutine SUB2, the process proceeds to the nanoparticle synthesis process, a predetermined amount of a production liquid containing nanoparticles is generated, and the process proceeds to step S4. In step S4, it is determined whether or not the product liquid is to be concentrated. If a predetermined amount of the concentrated liquid already exists, N is determined and the process proceeds to step S5. If step S4 is Y, the process proceeds to a subroutine SUB3, where the process proceeds to the production liquid concentration process to produce a predetermined amount of the concentrated liquid, and the process proceeds to step S5. In step S5, it is determined whether or not the concentrate is to be dried. If a predetermined amount of dry nanoparticles has already been produced, the result is N, and the process proceeds to step S6. If the predetermined amount of dry nanoparticles has not been produced, step S5 becomes Y, and the process proceeds to subroutine SUB4 where the concentrated liquid drying process is performed to dry the concentrated liquid, and after drying, the process proceeds to step S6. In step S6, it is determined whether or not to end the production of nanoparticles. When the predetermined amount of nanoparticles is not manufactured, the value is N, and the process returns to step S2. When a predetermined amount of nanoparticles are produced, the production is finished as Y, and the flow is finished at END.

  FIG. 15 is a raw material liquid manufacturing subroutine flow chart showing the raw material liquid manufacturing process of the computer controller. FIG. 15 is a flowchart of the subroutine SUB1 shown in FIG. When the subroutine SUB1 starts, in step S10, initial conditions regarding the amount of solvent, the amount of raw material, and the mixing temperature are set. The initial conditions can be changed for each operation, but when the same nanoparticles are manufactured, the initial conditions are automatically set according to the values input in advance, and the process proceeds to step S11. In step S11, it is instructed to mix the solvent 11 and the raw material 12 with the mixer 18a. When the mixing in step S11 ends, the process proceeds to step S12. In step S12, it is determined whether or not the bead mill 19 is used. When the raw material 12 is insoluble in the solvent 11 or when it is difficult to aggregate and disperse suitably, a bead mill is used, step S12 becomes Y, and the process proceeds to step S13. If the source material 12 is easily dispersed / dissolved in the solvent 11, the result is N, and the process proceeds to step S 18. In step S18, the mixed liquid (mixer mixed liquid) mixed by the mixer is used as the raw material liquid 18, and the process proceeds to step S19. In step S19, the raw material liquid which consists of a mixer liquid mixture is sent to the raw material liquid storage tank 14 by the three-way valve 18b, and it progresses to step S16. In step S13, the mixer mixed solution is sent from the three-way valve to the bead mill, and the process proceeds to step S14. In step S14, the raw material 12 is pulverized and refined by the bead particles in the dispersion unit 13a, and the process proceeds to step S15. In step S15, the bead particles are separated from the raw material liquid 18 in the centrifugal separator 13b and fed back to the dispersion unit 13a, and the raw material liquid 18 is sent to the raw material liquid storage tank 14, and the process proceeds to step S16. In step S16, the raw material liquid 18 is preheated to a temperature at which nanoparticles are not generated by the preheating device 16, and the process proceeds to step S17. In step S17, it is determined whether or not the raw material liquid production is completed. When a predetermined amount of the raw material liquid is stored, Y is set and Return is set. In the case of N, the process returns to step S11, the solvent 11 and the raw material 12 are mixed, and the steps so far are repeated.

  FIG. 16 is a nanoparticle synthesis subroutine flow chart showing the nanoparticle synthesis process in the first reaction tube of the computer controller. FIG. 16 is a flowchart of the subroutine SUB2 shown in FIG. In step S20, initial conditions for the nanoparticle synthesis process are set. The initial conditions to be set are the raw material liquid supply rate, the synthesis temperature, the first reaction tube flow rate, the second reaction tube rise rate, and the like. When the initial condition setting is completed, the process proceeds to step S21, where nanoparticles are generated in the first reaction tube 30, and the process proceeds to step S22. In step S22, it is determined whether or not the solvent 11 is filled in the first reaction tube 30, and if the solvent 11 is not filled, the result is N, and the process returns to step S22. When the solvent 11 is filled, step S22 becomes Y and the process proceeds to step S23 to determine whether the product gas cooling device 23 is in operation. In step S23, if the product gas cooling device 23 is in operation, the result is Y, and the process proceeds to step S24. If the product gas cooling device 23 is not in operation, the process returns to N, and the process returns to step S23 to generate the product gas cooling device 23. Step S23 is repeated until. In step S24, it is determined whether the exhaust device 24 is in operation. If Y, the process proceeds to step S25. In the case of N, the process returns to step S24, and step S24 is repeated until the exhaust device 24 operates. In step S25, it is determined whether the rotor 35 of the first reaction tube 30 is being stirred. If Y, the process proceeds to step S26. When not stirring, it becomes N and returns to step S25, and step S25 is repeated until it agitates at the predetermined rotational speed by the rotor 35. In step S26, it is determined whether or not the first reaction tube 30 is appropriate for the synthesis temperature. If Y, the process proceeds to step S27. When the 1st reaction tube 30 is not heated to the appropriate synthesis temperature, it returns to N and returns to step S26, and step S26 is repeated until it reaches an appropriate synthesis temperature. In step S27, the raw material liquid 18 is supplied to the 1st reaction tube 30 with the pump 21, and it progresses to step S28. In this step S28, it is determined whether or not the flow rate of the raw material liquid 18 in the first reaction tube 30 is appropriate. If Y, the process proceeds to step S29. If the flow-down speed is not appropriate, N is returned to Step S28, the rotation speed of the rotor 35, the flow rate of the raw material liquid 18 and the like are adjusted, and Step S28 is repeated until the flow-down speed is appropriate. In step S29, it is determined whether or not the color of the nanoparticle generation liquid in the lowermost section 39 is appropriate. If Y, the process proceeds to step S30 shown in FIG. 16 and 17 are subroutines that proceed together. The nanoparticle production liquid color is obtained by sampling a part of the first production liquid flowing out from the first reaction tube 30 or by flowing a small amount of the first production liquid into the transparent tube for confirming the nanoparticle production liquid color. Observed. If the nanoparticle production liquid color is not appropriate, it means that there is a large amount of unreacted, and the process returns to step S29 and this step is repeated. At this time, the outflow of the first product liquid may be blocked by an electromagnetic valve or the like provided in the outflow path, and the supply of the raw material liquid 18 may be temporarily stopped.

  FIG. 17 is a flowchart of a nanoparticle synthesis subroutine showing a nanoparticle synthesis process in the second reaction tube of the computer control device in a flow integrally connected to FIG. 16 by “R”. In step S30, nanoparticle generation in the second reaction tube 40 is started, and the process proceeds to step S31. In step S31, it is determined whether or not the second reaction tube 40 is filled with the solvent 11. If Y, the process proceeds to step S32. In the case of N, the process returns to Step S31, and Step S31 is repeated until the solvent 11 is filled in the second reaction tube 40. In step S32, it is determined whether or not the product gas cooling device 23 is in operation. If Y, the process proceeds to step S33. In the case of N, the process returns to step S32, and step S32 is repeated until the product gas cooling device 23 is operated, similarly to the first reaction tube 30. In step S33, it is determined whether the exhaust device 24 is in operation. If Y, the process proceeds to step S34. In the case of N, the process returns to step S33, and step S33 is repeated until the exhaust device 24 operates. Similarly, in step S34, it is determined whether the rotor 45 of the second reaction tube 40 is being stirred. If Y, the process proceeds to step S35. In the case of N, the process returns to step S34, and step S34 is repeated until the rotor 45 is stirred at a predetermined rotation speed. In step S35, it is determined whether the liquid temperature in the second reaction tube 40 is appropriate for the synthesis temperature. If Y, the process proceeds to step S36. Similarly, when the liquid temperature of the second reaction tube 40 is not heated to an appropriate synthesis temperature, the process returns to step S35, and step S35 is repeated until the appropriate synthesis temperature is reached. In step S36, the first product solution in the first reaction tube 30 is supplied to the second reaction tube 40, and the process proceeds to step S37. In this step S37, it is determined whether or not the rising speed of the first product liquid in the second reaction tube 40 is appropriate. If Y, the process proceeds to step S38. In the case of N, the process returns to step S37, and the flow rate of the first product liquid and the like are adjusted by the pressure of the second reaction tube 40 and the first reaction tube 30 and the supply amount of the product liquid, etc. Step S37 is repeated until the speed is appropriate. In step S38, it is determined whether or not the nanoparticle production liquid color in the uppermost section 49 is appropriate. If Y, the process proceeds to step S39. Similar to the first reaction tube 30, the nanoparticle production liquid color is observed by sampling a part of the outflowing production liquid or by allowing a small amount of production liquid to flow into the transparent tube for confirming the nanoparticle production liquid color. The If the nanoparticle generation liquid color is not appropriate, it indicates that the reaction amount has not reached the predetermined amount that causes a complete reaction, and the process returns to step S38 and this step is repeated. At this time, the outflow of the product liquid may be blocked by an electromagnetic valve or the like provided in the outflow path, and the supply of the first product liquid from the first reaction tube 30 may be temporarily stopped. In step S39, it is determined whether or not the production of the product liquid is finished. If the result is Y, “Return” is set and the subroutine SUB2 is finished. If the production amount of the product liquid has not reached the predetermined amount, the result is N, and the process returns to step S31.

  FIG. 18 is a product solution concentration subroutine flow chart showing a product solution concentration process of the computer control device. In the subroutine SUB3, in step S40, initial conditions of the product liquid concentration process including a vacuum drying method are set, and the initial conditions include the product liquid supply speed and the degree of vacuum. When the initial condition setting is completed, the process proceeds to step S41, the exhaust device 71 (vacuum pump) is driven, and the process proceeds to step S42. In step S42, the reduced pressure large container 85 is maintained at a predetermined degree of vacuum, and in the next step S43, the product liquid 65 is supplied from the product liquid storage tank 68 into the small container 81 by the pump P, and the process proceeds to step S44. In step S44, the generated liquid 68 is sprayed from the spray container 83 into the vacuum large container 85, and in the next step S45, the solvent is vaporized and exhausted by the exhaust device 71, and the solvent contained in the exhaust (gas) is removed. The safe gas which has been liquefied by the liquefier 72, recovered by the solvent recovery 73 and from which the solvent 11 has been removed is released into the atmosphere 74, and the process proceeds to step S47. In step S47, the concentrate 78 is stored in the concentrate storage tank 75, and in the next step S48, it is determined whether or not the concentrate production is completed. In the case of Y in step S48, “Return” is set, and the subroutine SUB3 ends. If the concentrated liquid production is less than the predetermined amount, the result is N, and the process returns to step S41.

  FIG. 19 is a concentrate drying subroutine flowchart showing the concentrate drying process of the computer controller. In the subroutine SUB4, in step S50, initial conditions of the concentrated liquid drying process including the vacuum drying method are set, and the initial conditions include the concentrated liquid supply speed and the degree of vacuum. In the next step S51, the vacuum exhaust device 98 (vacuum pump) is driven, and the process proceeds to step S52. In step S52, the concentrated liquid drying device 91 is maintained at a predetermined degree of vacuum. In the next step S53, the concentrated liquid 78 is supplied from the concentrated liquid storage tank 75 to the hopper 94 by the pump P, and the process proceeds to step S54. In step S54, the concentrated liquid 78 is discharged from the hopper 94 onto the rotary table 95. In the next step S55, the solvent is vaporized from the concentrated liquid 78 and exhausted by the exhaust device 98, and the gas is liquefied by the liquefier 99. The solvent 11 is recovered by the solvent recovery 92, and a safe gas is released into the atmosphere 99a, that is, into the atmosphere. In the next step S56, the temperature control device 96 adjusts the temperature of the turntable 95. In the next step S57, the concentrated solution 78 is dried on the turntable 95 to become dry nanoparticles 97. In the next step S58, the dried nanoparticles 97 are appropriately recovered outside the apparatus (93), and the process proceeds to step S59. In step S59, it is determined whether or not the drying process is completed. If “Y”, “Return” is set, and the subroutine SUB4 is completed. If “N”, the process returns to step S51.

[Production Experiments 1-5 of Silver Carbonate / n-Hexanol: C6AgAL-MP Nanoparticles]
In the production experiments 1 to 5, n-hexanol (C number is 6) is used. The meaning of C6AgAL-MP means that C6 has a C number of 6, Ag means a silver nucleus, and AL means an alcohol. MP is a notation for using the mass production continuous production system including the nanoparticle production apparatus shown in FIGS. 1 and 2, for example, and is distinguished from the description C6AgAL by the conventional pot method. The alcohol having 6 carbon atoms is n-hexanol.
First, 2 kg of silver carbonate (Ag2CO3) was mixed with 12.7 L (showing a liter) of n-hexanol to prepare a dilute dispersion having a mixing ratio of 14 mol of n-hexanol to 1 mol of silver carbonate. Hereinafter, the liter is indicated by L, and the milliliter is indicated by mL. This dilute dispersion was supplied to a bead mill 19 shown in FIG. 11, and silver carbonate was made into fine particles using beads. This bead mill treatment was repeated 20 times to produce a raw material liquid 18 by converting silver carbonate into uniform fine particles, and the raw material liquid was stored in the raw material liquid storage tank 14.

  Next, when using the nanoparticle production apparatus having the first reaction tube 30 and the second reaction tube 40 as shown in FIG. 1, the electromagnetic valve 17 is opened, and the first reaction tube 30 and the second reaction tube 40 are connected. A total of 15 L of n-hexanol was charged at a rate of 0.4 L / min, the electromagnetic valve 17 was closed, and the first reaction tube 30 was further charged with 1.5 L of n-hexanol. Experiments using the nanoparticle production apparatus shown in FIG. In a preliminary experiment using only the first reaction tube 30 as shown in FIG. 2, 8.5 L of n-hexanol is charged while the electromagnetic valve is closed. Experiments using only the first reaction tube 30 are referred to as generation experiments 1 and 2. Further, in the generation experiments 1 and 2, the set temperature was adjusted to 110 ° C. by the heating device 22. In the generation experiments 3 to 4, the n-hexanol in the first reaction tube 30 is adjusted to 100 ° C., and the n-hexanol in the second reaction tube 40 is adjusted to 90 ° C. In the production experiment 5, both n-hexanol in the first reaction tube 30 and the second reaction tube 40 were set to 90 ° C. The pump 21 continuously feeds the raw material liquid 18 in the raw material liquid storage tank 14 at a flow rate of 400 mL / min (generation experiments 1 to 3), 450 mL / min (generation experiment 4), and 500 mL / min (generation experiment 5). The reaction tube 30 was supplied. In the first reaction tube 30, the rotator 35 was rotated at 150 rpm by the rotating device 50, and the second reaction tube was set to 100 rpm, and an annular spiral flow was caused inside the first and second reaction tubes 30 and 40. In the annular spiral flow, silver carbonate is reduced by n-hexanol, and n-hexanol-derived organic-coated silver nanoparticles (C6AgAL) are generated around the silver core. When the nanoparticles are generated, the liquid turns slightly black, and the black liquid reaches the lower part of the first reaction tube 30 in about 10 minutes. The time to reach the outlet of the second reaction tube 40 is about 15 minutes or more. The time for the 100% reacted solution to appear is described as the reaction time in Table 1 described later from the thermal analysis result of the sampling solution. The liquid is continuously withdrawn from the first or second reaction tube at a flow rate equivalent to the supply amount, and the liquid in each reaction tube is stirred so that the reaction always proceeds under a constant temperature distribution. It is controlled. Since it is not black for the first 10 minutes, it is n-hexanol itself, which is delivered to another container. A black liquid is generated after 20 minutes, and this reacted black liquid is a generated liquid 65 in which nanoparticles are generated and is stored in the generated liquid storage tank 68. Carbon dioxide gas is generated, and the inside of the first reaction tube 30 is adjusted by a back pressure valve so that the gauge pressure is constant at 0.3 atm. The second reaction tube 40 uses a variable pressure back pressure valve, and the gauge pressure is slightly increased to 0.32 atm.

  The black product liquid 65 was sampled for the purpose of knowing the characteristics of the produced nanoparticles, 0.001 kg was taken out for thermal analysis, the same amount was taken out after 10 minutes, the same amount was taken out after 10 minutes, and the same amount was taken out after 10 minutes. . The product liquid 65 was extracted from the product liquid storage tank 68 every 10 minutes, n-hexanol was removed by centrifugation and vacuum filtration, and only nanoparticles were extracted. At that time, the yield of the nanoparticles extracted at each stage was measured for each stage, thermal analysis was performed to examine the yield and characteristics of the nanoparticles, and the results are shown in Tables 1 and 2 as described later. When the supply liquid runs out, n-hexanol is supplied instead, and the reacted liquid continues to be withdrawn for 10 minutes, but after that it dilutes and is transferred to a separate container. The remaining liquid in the container was washed to finish the reaction.

Table 1 shows the detailed analysis results for each reaction liquid extraction elapsed time of the reaction results in the generation experiment 5. In the reaction solution samplings # 1 and # 2, the particle size of the initial produced nanoparticles is smaller, and the DTA peak temperature and the silvering temperature are slightly lower, and the coating amount is higher. It is difficult to directly compare the characteristics of thermal analysis of sampling liquid and extraction / recovery nanoparticles because extraction conditions are different. The nanoparticle yield of extraction recovery was 1.9 kg in total, and the characteristics of the nanoparticles were almost the same. The average coating amount was 9.2%, and the estimated average particle size was 11 nm.
The maximum amount of nanoparticles produced per unit time in Production Experiment 5 using this reaction system is 3.5 Kg / h by dividing the total yield by the time required from the reaction solution removal to the completion of the reaction of 0.55 hours. Is required. Table 2 shows a summary of the reaction results of C6AgAL-MP in production experiments 1-5. From these results, when the reaction set temperature is high and the flow rate is small, the average coating amount is low, and therefore the nanoparticle diameter is large. The temperature of the reaction solution is about 10 ° C. higher than the set temperature because of the generation of reaction heat.

[Silver carbonate / butanol: C4AgAL-MP nanoparticle production experiment 6]
A production experiment of butanol-derived organic-coated silver nanoparticles (referred to as C4AgAL-MP) was performed using the nanoparticle production apparatus in which the first reaction tube 30 and the second reaction tube 40 shown in FIG. 1 were combined. The meaning of C4AgAL-MP means that C4 has a C number of 4, Ag means a silver nucleus, and AL means an alcohol. An alcohol having 4 carbon atoms is butanol. MP is a notation for using the mass production continuous production system as shown in FIG. 1, and is distinguished from the description C4AgAL by the conventional pot method.
First, 2 kg of silver carbonate was mixed with 9.4 L of normal butanol (hereinafter referred to as n-butanol) to prepare a dilute dispersion having a mixing ratio of 14 mol of n-butanol with respect to 1 mol of silver carbonate. This diluted dispersion was supplied to a bead mill 19 shown in FIG. 11, and silver carbonate was made into fine particles by using beads. This bead mill treatment was repeated 15 times to produce a raw material liquid 18 in which the average particle size of silver carbonate was refined and uniformly dispersed to about 100 nm, and stored in the raw material liquid storage tank 14.

Next, the electromagnetic valve 17 is opened, the first reaction tube 30 and the second reaction tube 40 are filled with a total of 15 L of n-butanol at a rate of 0.5 L / min, the electromagnetic valve 17 is closed, and the first reaction tube An additional 1.5 L of n-butanol was charged. Further, the set temperature was set to 85 ° C. for each of the first reaction tube 30 and the second reaction tube 40 in the production experiment 6 by the heating device 22. The electromagnetic valve 17 was opened and the raw material liquid 18 in the raw material liquid storage tank 14 was continuously supplied to the first reaction tube 30 at a flow rate of 500 mL / min by the pump 21. In the first reaction tube 30, the rotator 35 was rotated at 150 rpm by the rotating device 50, and in the second reaction tube 40, the rotation was set to 100 rpm, and an annular spiral flow was caused inside each reaction tube. In the circular spiral flow, silver carbonate is reduced by n-butanol, and organic-coated silver nanoparticles (C4AgAL) derived from n-butanol are produced around the silver core.
When nanoparticles are produced, the liquid turns blackish brown. The dark brown liquid reaches the lower part of the first reaction tube 30 in about 10 minutes. The time to reach the second reaction tube outlet is about 15 minutes or more. The time for the 100% reacted solution to appear is described as the reaction time in Table 3 to be described later from the thermal analysis result of the sampling solution. The liquid is continuously withdrawn from the reaction tube at a flow rate equivalent to the supply amount, and the liquid in the reaction tube is controlled so that the reaction always proceeds under a constant temperature distribution upon stirring. Since it is not black-brown for the first 10 minutes, it is n-butanol itself, which is sent to another container by opening and closing the valve. A black-brown liquid is generated after 20 minutes, and this reacted black-brown liquid is a generated liquid 65 in which nanoparticles are generated, and is stored in the generated liquid storage tank 68. Carbon dioxide gas is generated, and the pressure in the first reaction tube 30 is adjusted by a back pressure valve so that the gauge pressure is constant at 0.3 atm. The second reaction tube 40 uses a variable pressure back pressure valve, and the gauge pressure is slightly increased to 0.32 atm.

The samplings # 1 to # 4 shown in Table 3 will be described. The reaction solution was sampled and analyzed by thermal analysis for the purpose of knowing the properties of the produced nanoparticles. The product liquid 65 was extracted from the product liquid storage tank 68 every 10 minutes, subjected to centrifugal filtration and vacuum filtration to remove n-butanol, and only nanoparticles were extracted. At that time, the amount of nanoparticles extracted at each stage was measured for each stage, and thermal analysis was performed to examine the yield and characteristics of the nanoparticles. The results are shown in Table 3.
When the supply liquid runs out, n-butanol is supplied instead, and the reacted liquid continues to be withdrawn for 10 minutes. However, after that, it becomes diluted, so it is transferred to a separate container, and n-butanol is added until a clear liquid comes out. The remaining liquid in the container was washed to finish the reaction. Then, the nanoparticles for each reaction time were analyzed, and the average particle diameter of the silver nuclei and the weight percentage of the amount of the organic coating were measured.

  The maximum amount of nanoparticles produced per unit time in Production Experiment 6 using this reaction system is 5.4 kg / h by dividing the total yield by the time required from the reaction solution removal to the end of the reaction of 0.35 hours. Is required. When the results of the generation experiment 6 are summarized, the results shown in Table 4 are obtained.

When these results are compared with the results of C6AgAL-MP, which is the reaction with n-hexanol in Production Experiment 5, the boiling point of n-butanol is lower than that of n-hexanol, but the reducing power is strong and the coating amount is larger at lower temperatures. Thus, nanoparticles with a small particle size are produced. In addition, since the DTA peak temperature and silvering temperature are low and a small particle size distribution is important for bonding applications, the results of the n-butanol reaction are superior to the n-hexanol reaction in all aspects in the application development of nanoparticles. I understand that

  By using the method and apparatus of the present invention, it is possible to produce a large amount of nanoparticles having a uniform particle size by a liquid phase reaction and to produce nanoparticles in a spiral flow, particularly an annular spiral flow. The production speed is high, and it is possible to mass-produce nanoparticles having a uniform particle size. Since the method and apparatus of the present invention can produce any kind of nanoparticles by a liquid phase method, it is possible to efficiently produce nano metal particles, nano inorganic particles, nano organic particles, and the like. Therefore, the method and apparatus of the present invention can contribute to various industrial fields such as the bonding field, printing field, cosmetic field, and chemical industry field.

1 Nanoparticle automatic manufacturing equipment 2 Computer control equipment 3 ROM
4 CPU
5 RAM
6 Input device (INPUT)
7 Output device (OUTPUT)
8 I / O port 10 Raw material liquid production unit 11 Solvent 12 Raw material substance 13 Raw material liquid production device 13a Dispersion unit 13b Centrifugal separation unit 13c Cold water pipe 14 Raw material liquid storage tank 15 Cooling device 16 Preheating device 17 Electromagnetic valve 18 Raw material liquid 18a Mixer 18b Three-way valve 19 Bead mill 20 Nanoparticle production unit 21 Pump 22 Heating device 23 Generated gas cooling device 23a Input tube 23b Spiral tube 23c Output tube 24 Exhaust device 24a Exhaust tube 25 First product liquid 26 Nanoparticle 30 First reaction tube 30a Reaction tube Head portion 30b Annular receiving portion 30c Drain valve 30d Projection tube portion 30e Inlet end 30f Outlet end 30g Reaction tube body portion 30h Outer peripheral wall 31 Separator 32 Top plate portion 32a Gas vent hole 32b Outer peripheral edge 32d Annular opening 33 Annular portion 34 Tightening bolt 35 Rotor 36 Blade 37 Annular portion 38 Tightening bolt 39 Section 40 Second Reaction tube 40a Reaction tube head portion 40b Drain valve 40d Drain valve 40d Projection tube portion 40e Inflow end 40f Outflow end 40g Reaction tube body portion 40h Outer wall 41 Separator 42 Top plate portion 42a Gas vent hole 42b Outer peripheral edge 42d Annular opening 43 Annular Part 44 Clamping bolt 45 Rotor 46 Blade 47 Annular part 48 Clamping bolt 49 Compartment 50 Rotating device 51 Rotating connecting part 52 Rotating shaft 53 Bearing 60 Liquefaction device 64 Liquid level meter 65 Product liquid 66 Safety gas atmospheric release 67 Solvent recovery 68 Product solution reservoir 69 Electromagnetic valve 70 Product solution concentrator 71 Exhaust device (vacuum pump)
72 Liquefaction device 73 Solvent recovery 74 Safety gas release to atmosphere 75 Concentrated liquid storage tank 76 Solenoid valve 78 Concentrated liquid 80 Product liquid concentrating device 81 Spray pipe 81a Inlet end 81b Outlet end 83 Sprayer 83a Spray hole 85 Depressurized large container 86 Exhaust port 87 Large container taper section 88 Discharge port 89 Support member 90 Concentrated liquid drying section 91 Concentrated liquid drying apparatus 92 Solvent recovery 93 Nanoparticle recovery 94 Hopper 95 Rotary table 96 Temperature control apparatus 97 Dry nanoparticle 98 Vacuum exhaust apparatus 99 Liquefaction apparatus 99a Safety gas Atmospheric discharge aa Liquid mixture e Spiral flow (downward spiral flow)
f Downflow (also called down annular spiral flow)
g Generated gas j Spiral flow (upward spiral flow)
k Ascending flow (also called ascending annular spiral flow)
m Product gas M Motor P Pump Q1 Terminal Q2 Terminal Q3 Terminal Q4 Terminal 101 Microreactor 102 Ultrasonic generator 103 Water bath 104 Reactor 105 Bottom plate 106 Intermediate laminated thin plate 107 Top plate 108 Inflow path 109 Microchannel 109a Microchannel 109b Microchannel 110 Outlet 124 Connecting bolt 126 Ultrasonic wave 126a Part that strengthens by ultrasonic interference 126b Part that weakens by ultrasonic interference 201 Reactor 202 Reaction tube 203a Zirconium salt aqueous solution (raw material aqueous solution)
203b Suspension 204 Precipitated particles 205 Reaction mixture (precipitation solution)
206 Zirconia hydrate sol 207 Heating medium 207a Inlet 207b Outlet 208 Velocity gradient 212 formed in the reaction tube 212 pH adjuster 213 Mixer 310 Precursor supply unit 320 First heating unit 321 First circulator 330 Second heating unit 331 Second circulator 340 Cooling unit 350 Transfer device

Claims (13)

A raw material solution for producing nanoparticles in which a raw material is mixed in a solvent is prepared, a reaction tube through which the raw material solution flows is arranged, and the same solvent and / or the raw material solution as the raw material solution is placed inside the reaction tube. And the temperature of the solvent in the reaction tube is controlled to the nanoparticle synthesis temperature, the raw material liquid is supplied to the inflow end of the reaction tube, and the supplied raw material liquid and the solvent in the reaction tube are mixed. forming a Nagato or annular helical flow which flows to the outlet end from the inlet end while orbiting along the circumferential direction of the outer peripheral wall inner surface of the reaction tube wherein the raw material solution while being stirred, the in the annular spiral flow Nanoparticles are formed from the raw material, and the product liquid containing the nanoparticles is sent out from the outflow end of the reaction tube, where the reaction tube is placed in one or more compartments along the flow direction of the raw material liquid. The inlet side of the compartment is along the inner surface of the outer peripheral wall. An annular opening that is open in the circumferential direction is formed, the annular spiral flow passes through the annular opening and flows through one or more of the compartments, and the nanoparticles are formed in the annular spiral flow The partition is a region extending from a separator to the next separator, and one or more gas vent holes are opened in the top plate portion of the separator, and the generated gas is allowed to escape upward from the gas vent holes. A method for producing nanoparticles. The method for producing nanoparticles according to claim 1 , wherein the raw material liquid is preheated within a temperature range in which the nanoparticles are not synthesized. One or more stages of the reaction tube is configured in series and / or parallel to, said annular helical flow downward flow inside of each reaction tube, an upward flow, to claim 1 or 2 is selected from the inclined flow or horizontal flow The manufacturing method of the nanoparticle of description. The method for producing nanoparticles according to any one of claims 1 to 3 , wherein the nanoparticles are produced by the reaction of the solvent and the raw material at the synthesis temperature. Any of a manufacturing process of the raw material liquid, a manufacturing process of a concentrated liquid that increases the concentration of the nanoparticles after the manufacturing of the generating liquid, and a drying process of the concentrated liquid that further dries the concentrated liquid The method for producing nanoparticles according to any one of claims 1 to 4 , wherein one or more steps are added. 6. The process for producing the concentrate according to claim 5 , wherein in the step of producing the concentrate, the product liquid is sprayed into a vacuum container to evaporate the solvent from the product liquid, and the concentrate having an increased concentration of the flowing down nanoparticles is recovered. A method for producing nanoparticles. The method for producing nanoparticles according to claim 5 or 6 , wherein in the drying step of the concentrated liquid, the concentrated liquid is vacuum-dried in a container and dried to an extent that at least the nanoparticles are not scattered. The same solvent as the nanoparticle manufacturing raw material liquid in which the raw material is mixed in the solvent and / or the reaction tube filled with the raw material liquid, and the synthesis temperature of the nanoparticles in the solvent and / or the raw material liquid in the reaction tube A temperature controller for controlling the temperature, an inflow end of the reaction tube to which the raw material liquid is supplied, the mixing of the supplied raw material liquid and the solvent of the reaction tube, or stirring the raw material liquid A rotor that forms an annular spiral flow along the inner surface of the outer peripheral wall of the reaction tube, and the reaction tube that discharges the product liquid containing the nanoparticles by forming nanoparticles from the source material in the annular spiral flow An outlet end of the reaction tube, a rotating shaft disposed at the axial center of the reaction tube, one or more separators fixed to the rotating shaft so as to be spaced apart from each other, between adjacent separators, or between the separator and the Formed between the tube ends of the reaction tube And an annular opening formed between an outer peripheral edge of the separator and an inner surface of the outer peripheral wall of the reaction tube. wherein through the annular opening so on are flowing through the compartment, the manufacturing apparatus of the annular said nanoparticles in the spiral flow is formed nanoparticles, wherein Rukoto is. The said separator is a manufacturing apparatus of the nanoparticle of Claim 8 which opened the 1 or more gas vent hole in the top-plate part. The nanoparticle production apparatus according to claim 8 or 9 , wherein a preheating device for preheating the raw material liquid in advance within a temperature range in which nanoparticles are not synthesized is arranged before being supplied to the reaction tube. One or more stages of the reaction tube is configured in series and / or parallel to, said annular helical flow downward flow inside the respective reaction tubes, upflow of claims 8-10 which is selected on the inclined flow or horizontal flow The nanoparticle production apparatus according to any one of the above. An apparatus for producing the raw material liquid, an apparatus for producing a concentrate in which the production liquid is concentrated after the production liquid is produced to increase the concentration of the nanoparticles, and a liquid drying apparatus for further drying the liquid concentrate The nanoparticle production apparatus according to any one of claims 8 to 11 , wherein any one or more apparatuses are added. The nanoparticle production apparatus according to any one of claims 8 to 12 , a computer control apparatus that controls the nanoparticle production apparatus using an electrical signal, and a program stored in the computer control apparatus, An automatic nanoparticle production apparatus characterized by automatically controlling a particle production apparatus.

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