WO2013022126A1

WO2013022126A1 - Heterogeneous phase reaction accelerating apparatus and method for a fluid

Info

Publication number: WO2013022126A1
Application number: PCT/KR2011/005757
Authority: WO
Inventors: 문광순; 윤승규
Original assignee: 재단법인 한국계면공학연구소
Priority date: 2011-08-08
Filing date: 2011-08-08
Publication date: 2013-02-14
Also published as: KR101580583B1; KR20140088856A

Abstract

The present invention relates to a heterogeneous phase reaction accelerating apparatus, and to a method using same to produce a mixed fluid, the apparatus comprising: a reaction tube containing a first fluid to produce a mixed fluid using an ester interchange reaction of the first fluid and a second fluid; and a spraying unit having a nozzle for spraying the second fluid into the reaction tube in the form of fine particles to expand the interface of the second fluid. According to the present invention, by spraying the second fluid into the first fluid in the reaction tube by means of the nozzle, a mixed reaction product of a hydrophobic material and a hydrophilic material can be highly efficiently produced in a short time. Here, an ester interchange reaction is performed at a desired optimal reaction speed using at least one of: an interface expansion effect due to an increase in the specific surface area of the fine particles; an effect of the fine particles preventing the occurrence of fatty acid metal salts inside the reaction tube; a chemical effect caused by heating the first fluid; or a physical mixing effect caused by a turbulent flow within the reaction tube or by a mixer unit.

Description

Reaction promoting device and reaction promoting method of non-homogeneous fluid

The present invention relates to a reaction promoting device for non-homogeneous fluids and a method for promoting a reaction of non-homogeneous fluids that promote the reaction of non-homogeneous fluids that do not dissolve together.

Generally, a phase is a critical phase such as a solid phase, a liquid phase, a gas phase, or a plasma, depending on the state of a substance, and is divided into a homogeneous phase and a heterogeneous phase according to whether two phases have the same phase. Can be. For example, hydrophilicity liquids that mix well with water and hydrophobisity liquids that do not mix well with water can be regarded as non-homogeneous fluids.

In many chemical reactions, even if the phases of the two components are in the same liquid state, if the non-homogeneous phases are not mixed with each other, even if the reaction does not proceed or the reaction proceeds, the reaction rate is slow and the reaction yield is greatly reduced.

The present invention is to provide a reaction promoting device and a reaction promoting method for promoting the reaction rate of a non-homogeneous liquid having very low reactivity since they are not dissolved in each other. To this end, the present invention focuses on the interface of the non-homogeneous fluid and provides a means for greatly accelerating the reaction rate of the non-homogeneous fluid.

In order to achieve the above object, the reaction promotion apparatus of the non-homogeneous fluid of the present invention includes a reaction tube in which the first fluid is accommodated to produce a mixed fluid by ester reaction of a first fluid and a second fluid, and the reaction. And a spraying unit provided with a nozzle extending the interface of the second fluid by injecting the second fluid into fine particles inside the tube.

In one embodiment, the mixed fluid production method according to the present invention, by driving the pump to supply a first fluid to the supply, the heater to heat the first fluid, the reaction tube with the first fluid supplied through the supply And spraying the second fluid into the reaction tube with fine particles through a nozzle installed inside the reaction tube, and interfacial expansion effect due to an increase in the specific surface area of the fine particles, and suppresses the occurrence of fatty acid metal salts in the reaction tube. At least one of the effect of the fine particles, the chemical effect of the first fluid heating, the physical mixing effect of the turbulent flow inside the reaction tube to cause a transesterification reaction inside the reaction tube at a desired reaction rate and the mixed fluid Is generated, and the mixed fluid inside the reaction tube is discharged to the outside via the first discharge pipe at the outlet side of the reaction tube.

In another embodiment, the mixed fluid production method according to the present invention, by driving the pump to supply a first fluid to the supply, the heater to heat the first fluid, the reaction tube with the first fluid supplied through the supply Of the fine particles to spray the second fluid into the reaction tube through the nozzles installed inside the reaction tube, and to suppress the interface expansion effect by the fine particles and the generation of fatty acid metal salts in the reaction tube. At least one of an effect, a chemical effect by heating the first fluid, and a physical mixing effect by turbulent flow inside the reaction tube, causes a transesterification reaction inside the reaction tube at a desired reaction rate, and a mixed fluid is produced. The mixed fluid inside the reaction tube is supplied to the inline mixer of the mixer unit, and the inline mixer is rotated by external power. Mixing the mixed fluid by a zigzag shape in a wing or fixed state, and the mixed fluid passing through the reaction tube or through the mixer unit is disposed in the first discharge pipe or the mixer unit outlet side disposed at the outlet of the reaction tube. It is discharged to the outside through the second discharge pipe disposed in the.

According to the present invention, a mixed reaction product of a hydrophobic substance and a hydrophilic substance can be produced in a short time and with high efficiency by injecting a second fluid into the first fluid supplied into the reaction tube with a nozzle. At this time, the interfacial expansion effect due to the increase of the specific surface area of the fine particles, the effect of the fine particles to suppress the generation of fatty acid metal salt in the reaction tube, the chemical effect by the first fluid heating, the turbulent flow inside the reaction tube or physical mixing by the mixer unit At least one of the effects has the advantage that the transesterification reaction proceeds at the desired optimum reaction rate.

[Brief Description of Drawings]

1 is a scheme representing a transesterification reaction.

FIG. 2 shows one embodiment of the reaction promotion apparatus of the non-homogeneous fluid of the present invention which improves the reaction rate and the reaction yield by expanding the surface area of the interface by fine particle spraying.

FIG. 3 shows an embodiment in which the embodiment of FIG. 2 is optimized for mass production.

4 to 6 are photographs taken inside the reaction tube. FIG. 4 shows before injection, FIG. 5 immediately after injection, and FIG. 6 shows a maximum injection state.

7 is a graph comparing productivity of mixed fluids with and without nozzles.

[Technical Challenges]

Hereinafter, exemplary embodiments of the present invention will be described in detail with reference to the accompanying drawings.

Representative non-homogeneous fluids for the purposes of the present invention include oil and methoxide. Oil and methoxide are transesterified to biodiesel, and the mixed fluid of oil and methoxide becomes biodiesel.

1 is a scheme representing a transesterification reaction. Referring to this, a mixed fluid is prepared through a transesterification reaction in which glycerol is separated using methanol from triglycerides in which glycerol is bound to trivalent fatty acids, and then produced fatty acid esters.

In general, factors affecting the reaction rate of a chemical reaction include, for example, the physicochemical properties of the reactants, concentration, temperature, pressure, catalyst, and the ability of the reactants to contact each other. Maximizing the contact area between the reactants among the factors affecting the chemical reaction rate is a common requirement in all chemical reactions, and maximizes the contact area at the interface between the reactants and the retention time through the contact. Is an important factor in determining reaction rate and reaction yield.

And if a substance of atomized automized particles in the order of several micrometers between the reaction mixture can be provided just before the initiation of the reaction between the reaction mixtures, the aspect of the reaction goes beyond the range of simple physical mixing properties. Even change is possible.

One of the important factors for maximizing the contact area between the reaction mixtures is the phase and phase equilibrium of the reaction mixtures.

Generally, a phase is a critical phase such as a solid phase, a liquid phase, a gas phase, or a plasma depending on the state of a substance. When a phase has the same properties as a polar fluid such as water and ethanol, it can be regarded as a homogeneous phase fluid. Since they do not mix with each other like methanol, they can be regarded as heterogeneous phase fluids if they have different properties.

Homogeneous fluids are easily dissolved or mixed with each other so that no interface exists. For example, if a container is filled with water and ethanol is added to it, water and ethanol are easily mixed with the same polarity so that no distinct interface is formed.

On the other hand, non-homogeneous fluids do not dissolve or mix with each other, so there is a distinct interface due to the difference in density. For example, filling the vessel with oil and adding methanol to it does not easily mix the oil and the methanol with different polarities, so that the distinction between the bottom and the top of the vessel results in distinct densities, depending on the density difference.

Thus, chemical reactions between non-homogeneous fluids can occur only at the interface, and if no interface exists or two non-homogeneous fluids are isolated from each other at the interface location, the chemical reaction of the non-homogeneous fluid cannot occur. Thus, non-homologous

Increasing the area of the interface becomes important to facilitate the chemical and physical reactions of the fluid.

As exemplified below, when a biofluid of a mixed fluid is prepared by reacting hydrophobic oil with hydrophilic methanol as a representative example of a non-homogeneous fluid, the rate of transesterification can be increased by expanding the interface between oil and methanol. As a result, it is possible to accelerate the production rate of biodiesel.

Reactions, generally called two-phase reactions, refer to the reaction of two reactants with different phases of matter, such as solid-liquid and gas-liquid reactions. However, when a reactant having a hydrophobisity group and a reactant having a hydrophilicity group do not mix well with each other, as in the transesterification reaction, they are reactions between the same liquid state but a heterogeneous phase fluid, so it is like a two-phase reaction. It can be seen that the reaction proceeds. In this case, the reaction rate drops significantly.

Biodiesel is a mixed fluid by alcohol decomposition in which alcohol is added to triglyceride which is a main component of fats and oils. Biodiesel is prepared through transesterfication of alcohols and fats and oils using base or acid catalysts.

However, the main raw material of the biodiesel animal or vegetable oils and oils and fats and oils maintain the hydrophobic group of the triglyceride (triglyceride) and the alcohol in general has a hydrophilic group, the oil and alcohol are not easily dissolved at room temperature, atmospheric pressure.

The present invention is to increase the reaction rate and the reaction yield by injecting triglyceride or methanol as fine particles having a size of several to several tens of micrometers as a non-homogeneous fluid, thereby increasing the reaction area of the interface formed by the non-homogeneous fluid. It features.

That is, the reaction rate of the transesterification reaction by spraying a non-homogeneous fluid including triglyceride corresponding to the first fluid or methanol or methoxide corresponding to the second fluid in a mist state using the nozzle 120 inside the reaction tube and The reaction yield can be increased.

A specific embodiment of the reaction promoting device for a non-homogeneous fluid will be described taking a biodiesel production device as an example.

As a representative example, one of the 'mixed fluids' is biodiesel, one of the 'first fluids' is triglyceride, and one of the 'second fluids' is methanol or methoxide. Methoxide refers to a mixture of methanol and a catalyst (eg caustic soda).

FIG. 2 shows one embodiment of the reaction promotion apparatus of the non-homogeneous fluid of the present invention which improves the reaction rate and the reaction yield by expanding the surface area of the interface by fine particle spraying. FIG. 3 shows an embodiment in which the embodiment of FIG. 2 is optimized for mass production. 2 and 3 are the same in their fundamental operating principle, so they will be described together.

Referring to FIG. 2, the apparatus for promoting reaction of a non-homogeneous fluid of the present invention includes a reaction tube 110 for increasing a transesterification reaction rate by interfacial expansion by spraying fine particles of a nozzle 120. It may further include a mixer unit 200 for increasing the rate of transesterification by physical mixing.

In one embodiment, the reaction unit 100 includes a reaction tube 110, a fixing plate 111, a fixing rod 112, a nozzle 120, a first discharge pipe 190, and a first valve 195. .

The second fluid supplied through the second fluid supply part 320 is injected into the fine particles by the nozzle 120. The nozzle 120 injects the second fluid into the reaction tube 110 at a predetermined injection angle θ. The length L and the diameter D of the reaction tube 110 are constant levels depending on the injection angle θ of the nozzle 120, the injection pressure, the size of the fine particles, and the diameter of the reaction tube 110 inlet and outlet. It is optimized to obtain the above transesterification rate.

In the reaction tube 110, since the second fluid injected from the nozzle 120 is mixed with the first fluid at a high pressure, both ends of the reaction tube 110 may be fixed to a plate to stably support the reaction tube 110. 111) is sandwiched between and supported. The fixing plate 111 is coupled by the fixing rod 112 and the fixing plate 111 and the reaction tube 110 are firmly coupled by the tensile force of the fixing rod 112.

The first fluid is accommodated in the reaction tube 110. When the second fluid is injected into the fine particle state by the nozzle 120 installed inside the reaction tube 110, the reaction rate is accelerated by the interface expansion effect because the second fluid is injected in the atomized or automized phase state.

On the other hand, since the foamed fatty acid metal salt generated by the transesterification reaction is crushed by fine particles sprayed at high speed and high pressure, the reaction yield and reaction rate are improved.

In addition, fine particles of methanol or methoxide, which is a second fluid, are uniformly mixed in an emulsion state with oil, which is the first fluid, by kinetic energy supply by injection of the nozzle 120. That is, the esterification reaction rate is dramatically increased according to the interfacial engineering physicochemical effect by the fine particle injection, the physical effect by the injection force of the nozzle 120, and the chemical effect by the temperature heating of the heater 390.

A supply part 310 for supplying a first fluid is connected to an inlet side of the reaction tube 110, and the first fluid is supplied with a supply pressure by the pump 380. The outlet side of the reaction tube 110 is connected to the first discharge pipe 190 for discharging the mixed fluid inside the reaction tube 110.

The diameter of the reaction tube 110 is preferably larger than the diameter of the supply unit 310 and the first discharge tube 190.

When the fluid inside the reaction tube 110 causes irregular turbulent flow in the reaction tube 110 due to the injection pressure of the nozzle 120, the rate of transesterification reaction is increased. Due to the nature of the incompressible continuous fluid, the flow rate per unit time of the fluid is the same at the inlet and outlet of the reaction tube 110. Therefore, the reaction rate is increased when the fluid stays inside the large reaction tube 110 longer than the fluid stays in the small diameter supply unit 310 or the first discharge pipe 190. Since the second fluid injection angle of the nozzle 120, the diameter and the length of the reaction tube 110 are optimally designed, the transesterification reaction rate is enhanced.

The mixer unit 200 physically remixes the mixed fluid discharged from the reaction unit 100 to double the transesterification reaction rate, and includes an inline mixer 210.

The inline mixer 210 may have a blade that rotates by external power therein. In addition, in the embodiment shown in FIG. 2, a zigzag static blade 212 is provided which triggers turbulent flow of the fluid by the shape feature in a fixed state, and another embodiment of the inline mixer 210 is provided. Yes. In the embodiment shown in Figure 3 is shown a wing that is rotated by external power.

The first bypass pipe 201 is connected to the inlet side of the inline mixer 210 and the second discharge pipe 290 is connected to the outlet side. The first bypass pipe 201 is connected to the first discharge pipe 190 corresponding to the outlet of the reaction unit 100. When the first valve 195 is opened, the mixed fluid supplied through the first discharge pipe 190 flows into the inlet side of the inline mixer 210 through the first bypass pipe 201. When the first valve 195 is closed, the mixed fluid is produced by the ester reaction by the reaction unit 100 alone without the action of the mixer unit 200.

Whether to close the first valve 195 to produce a mixed fluid with the reaction unit 100 alone, or to open the first valve 195 to produce the mixed fluid by the combined action of the reaction unit 100 and the mixer unit 200. Whether or not is determined by several factors listed below.

That is, the supply pressure of the first fluid, the supply flow rate of the first fluid, the supply temperature of the first fluid, the injection pressure of the second fluid, the injection flow rate of the second fluid, the injection angle of the second fluid, the fine particles of the second fluid The size, the length of the reaction tube 110, the diameter of the reaction tube 110 is determined according to the optimum response value according to various variables.

On the other hand, the method is not limited to one cycle of the reaction unit 100 and the mixer unit 200, and according to the method of repeatedly circulating the reaction unit 100 and the mixer unit 200 several times, the amount of mixed fluid decreases but the mixing is performed. The purity of the fluid can be improved. In the case of repetitive circulation, the outlet side of the mixer unit 200 and the inlet side of the reaction unit 100 are connected. That is, the second discharge pipe 290 corresponding to the outlet side of the mixer unit 200 is connected to the second bypass pipe 301 corresponding to the inlet side of the reaction unit 100. The second bypass pipe 301 is connected to the supply unit 310 via the tank 330.

The tank 330 is a storage space for accommodating the mixed fluid and the first fluid, and serves as a buffer. In addition, the tank 330 becomes a space for providing a time for the first fluid to be heated by the heater 390.

3 is a reaction promoting device for a non-homogeneous fluid in a continuous production mode suitable for mass production. As a comparative example, in contrast to the present invention, there is a batch reaction promoting device. The batch reaction promoting device injects a second fluid into a large container containing the first fluid, while rotating the stirring blade inside the container to mix the first fluid and the second fluid, and then discharge the mixed fluid in the container when the reaction is completed. And a batch manner of filling a new first fluid inside the vessel.

However, this arrangement method has a fixed supply and discharge timing of the fluid, so that continuous operation is impossible and intermittent operation, and the reaction speed is much slower than the reaction promoting device of the present invention.

In the continuous operation reaction promoter of FIG. 3, the first fluid is continuously supplied to the reaction tube, and the nozzle installed inside the reaction tube continuously supplies the second fluid, and the reaction tube is capable of sufficiently reacting these non-homogeneous fluids. It extends with a sufficient length so that the injection angle of the nozzle, the injection pressure and the size of the nozzle hole cause sufficient turbulent flow inside the reaction tube, and the area of the interface of the second fluid by the nozzle injection can be maximized. It is optimized to ensure fast and consistent reactivity.

In FIG. 3, the mixer unit 200 may have a rotary blade or a fixed blade installed therein to add mechanical stirring, but may be used as a setler without installing the blade or blade. Here the settler functions as a separating funnel.

As shown in Figure 2 triglyceride (triglyceride), methanol, methoxide as a reactant of a large specific gravity glycerol and a small specific gravity methyl ester is obtained. At this time, the glycerol and methyl ester are separated from each other by the difference in specific gravity in the stopped state if left still without any stirring action inside the mixer unit 200 that functions as a settler. The methyl ester separated at the top of the mixer unit 200 is discharged as biodiesel, and the glycerol separated at the bottom is discharged separately.

The production method for various reaction modes for the reaction promotion apparatus of the non-homogeneous fluid illustrated in FIGS. 2 and 3 is as follows.

(1) Production method by the reaction unit 100 only (first mode):

The pump 380 is driven to supply the first fluid to the supply unit 310. Here, the first fluid is heated by the heater 390 to adjust the temperature of the first fluid that is optimal for increasing the reaction rate. A tank 390 is installed between the pump 380 and the supply part 310 to be used as a temporary storage space and a heating space of the heater 390.

The first fluid supplied through the supply unit 310 fills the reaction tube 110. The second fluid is injected into the fine particles through the nozzle 120 installed inside the reaction tube 110. At the desired reaction rate by the interfacial expansion effect by the fine particles, the effect of the fine particles to suppress the generation of fatty acid metal salts on the foam, the chemical effect by the first fluid heating, the physical mixing effect by the turbulent flow inside the reaction tube 110 The transesterification reaction takes place inside the reaction tube (110).

The mixed fluid inside the reaction tube 110 is discharged to the outside via the first discharge pipe 190 and the first valve 195. At this time, the first valve 195 is in an open state, and the second valve 295 connecting the reaction unit 100 and the mixer unit 200 is in a closed state.

(2) Production method by the circulation of reaction unit 100 and mixer unit 200 (second mode):

The pump 380 is driven to supply the first fluid into the tank 330, and the first fluid is heated by the heater 390.

When the first fluid is filled in the reaction tube 110, the second fluid is injected through the nozzle 120. The mixed fluid having the first transesterification reaction is supplied to the mixer unit 200 via the first discharge pipe 190 and the first bypass pipe 201. Here, since the first valve 195 is in a closed state, the mixed fluid cannot be discharged to the outside.

The mixed fluid flows inside the in-line mixer 210 due to the continuity of the fluid, and the transesterification reaction is secondarily performed by the physical mixing force caused by friction and collision with the static blade 212.

The mixed fluid passing through the in-line mixer 210 is discharged to the outside via the second discharge pipe 290 and the second valve 295. At this time, the third valve 395 located between the mixer unit 200 and the tank 330 is in a closed state.

(3) Production method by repeated circulation of reaction unit 100 and mixer unit 200 (third mode):

The operation of the pump 380, the heating of the heater 390, the spraying of the nozzle 120, and the operation of the inline mixer 210 are the same as described above.

The mixed fluid that has passed through the inline mixer 210 is resupplied to the tank 330 and the reaction unit 100 through the second discharge pipe 290 and the second bypass pipe 301. The transesterification reaction proceeds repeatedly while repeatedly cycling the reaction unit 100 and the mixer unit 200. When the reaction is completed, the driving of the pump 380 is stopped and the mixed fluid contained in the tank 330 is discharged to the outside.

During the reaction, the first valve 195 and the second valve 295 are in a closed state, and the third valve 395 connecting the second discharge pipe 290 and the second bypass pipe 301 is in an open state.

4 to 6 are photographs taken inside the reaction unit 100. FIG. 4 shows before the injection, FIG. 5 immediately after the injection, and FIG. 6 shows the maximum injection state. Depending on the degree of injection, it is possible to visually see a dramatic increase in reactivity due to the turbulent flow state inside the reaction tube 110 and the effect of interfacial expansion of the fine particles.

7 is a graph comparing the productivity of the mixed fluid with or without the nozzle 120.

Referring to this, in the case of the reaction using the nozzle 120, it can be seen that the methylester content reached a maximum value in a shorter time than when the nozzle 120 was not provided. As a result of confirming, it can be seen that the yield of the reaction using the nozzle 120 is much higher than otherwise.

[Description of the code]

100: reaction unit 110: reaction tube

111: fixing plate 112: fixing rod

120: nozzle 190: first discharge pipe

195: first valve 200: mixer unit

201: first bypass pipe 210: inline mixer

212: static blade 290: second discharge pipe

295: 2nd valve 301: 2nd bypass pipe

310: supply part 320: second fluid supply part

330 tank 380 pump

381: pump connector 390: heater

395: third valve

1 is a scheme representing a transesterification reaction.

7 is a graph comparing productivity of mixed fluids with and without nozzles.

Claims

In order to promote the reaction of a heterogeneous phase fluid including a first fluid and a second fluid that do not dissolve together, a reaction tube in which the first fluid is accommodated, and the second fluid in the reaction tube as fine particles. In the reaction promoting device for a non-homogeneous fluid comprising a nozzle for injecting,

The reaction tube extends along the spray direction of the nozzle,

A supply unit for supplying the first fluid is connected to the inlet side of the reaction tube,

The first fluid is supplied with a supply pressure by a pump,

A first discharge pipe for discharging the mixed fluid inside the reaction tube is connected to the outlet side of the reaction tube,

The diameter of the reaction tube is greater than the diameter of the supply portion and the first discharge tube, the reaction promoter of the non-homogeneous fluid, characterized in that.
The method of claim 1,

Reaction of the first fluid and the second fluid is promoted by the interface expansion effect of the second fluid according to the nozzle injection,

Wherein said first fluid and said second fluid are continuously reacted while said nozzle is being injected.
The method of claim 1,

And a mixer unit for physically mixing the mixed fluid of the first fluid and the second fluid discharged from the reaction tube to increase the reaction rate.
The method of claim 3,

The mixer unit includes an inline mixer for mixing the mixed fluid of the first fluid and the second fluid,

The in-line mixer has a zigzag static blade for mixing the fluid,

The first fluid is passed through the reaction tube once, and then in a first mode of obtaining the mixed fluid at the outlet side of the reaction tube, and the first fluid is passed through the reaction tube and the mixer unit once, respectively. A second mode of receiving the mixed fluid at the outlet side of the mixer unit, repeatedly passing the first fluid through the reaction tube and the mixer unit a plurality of times, and then at the outlet side of the reaction tube or at the outlet side of the mixer unit And / or to produce the mixed fluid in any one of the third modes of obtaining the mixed fluid.
The method of claim 3,

A pump for pressurizing the first fluid,

A tank disposed between the pump and the reaction tube to become a temporary receiving space of the first fluid,

Supply unit for supplying the first fluid at the inlet side of the reaction tube,

A first discharge pipe on the reaction tube outlet side through which the mixed fluid inside the reaction pipe is discharged;

A first bypass pipe connecting the first discharge pipe and the inlet side of the mixer unit,

A first valve for opening and closing a connection state between the first bypass pipe and the first discharge pipe,

A second discharge pipe connected to an outlet side of the mixer unit,

A second bypass pipe connecting the second discharge pipe to an inlet side of the reaction unit,

A second valve for opening and closing a connection state between the second discharge pipe and the second bypass pipe,

A pump connecting pipe connecting the second bypass pipe to the pump;

When producing the mixed fluid by passing the first fluid through the reaction tube once, the second valve is closed and the first valve is opened to obtain the mixed fluid through the first discharge pipe,

When the mixed fluid is produced by passing the first fluid through the reaction tube and the mixer unit once, the first valve is closed and the second valve is opened to obtain the mixed fluid through the second discharge pipe. ,

When the mixed fluid is produced by repeatedly passing the first fluid through the reaction tube and the mixer unit a plurality of the mixed fluid through the first discharge pipe with the second valve closed and the first valve opened. The apparatus for accelerating the reaction of a non-homogeneous fluid, wherein the mixed fluid is obtained through the second discharge pipe in a state of obtaining or closing the first valve and opening the second valve.
Driving the pump to supply the first fluid to the supply,

Heating the first fluid with a heater,

Filling the reaction tube with the first fluid supplied through the supply,

The second fluid is injected into the reaction tube with fine particles through a nozzle installed inside the reaction tube,

At least one of an interfacial expansion effect by the fine particles, an effect of the fine particles suppressing the generation of fatty acid metal salts in the reaction tube, a chemical effect by heating the first fluid, and a physical mixing effect by the turbulent flow inside the reaction tube By one, a mixed fluid is produced inside the reaction tube at a desired reaction rate,

The mixed fluid inside the reaction tube is discharged to the outside via the first discharge pipe of the reaction tube outlet side, characterized in that for promoting the reaction of the homogeneous fluid.
Driving the pump to supply the first fluid to the supply,

Heating the first fluid with a heater,

Filling the reaction tube with the first fluid supplied through the supply,

The second fluid is injected into the reaction tube with fine particles through a nozzle installed inside the reaction tube,

At least one of an interfacial expansion effect by the fine particles, an effect of the fine particles suppressing the generation of fatty acid metal salts in the reaction tube, a chemical effect by heating the first fluid, and a physical mixing effect by the turbulent flow inside the reaction tube By one, a mixed fluid is produced inside the reaction tube at a desired reaction rate,

The mixed fluid inside the reaction tube is supplied to the in-line mixer of the mixer unit,

The in-line mixer mixes the mixed fluid by a blade rotating in the external power or in a fixed state in a zigzag shape,

The mixed fluid passing through the reaction tube inside or through the mixer unit is discharged to the outside through a first discharge pipe disposed at the reaction tube outlet side or a second discharge pipe disposed at the mixer unit outlet side. Method of promoting the reaction of a fluid.