Method and reaction device for preparing brazitame protein by adopting micro-flow field reactor
By mixing the fermentation broth with methanol solution in a microfluidic reactor, the problem of low mixing efficiency in the fermenter was solved, enabling the efficient production of Brazilian sweet protein, increasing yield and production efficiency, and meeting industrial needs.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-12-31
- Publication Date
- 2026-04-10
AI Technical Summary
In existing technologies, the mixing efficiency in fermenters is limited, and the methanol is not evenly dispersed, resulting in poor mass transfer and affecting the utilization efficiency of methanol by microorganisms. This limits the yield and production cycle of Brazil sweet protein, making it difficult to achieve high efficiency and economy in industrial production.
A microfluidic reactor was used to mix the fermentation broth with a methanol solution. By achieving efficient mixing and mass transfer within the microfluidic reactor and controlling the methanol concentration below a safe threshold, the activity of microorganisms and the efficiency of product generation were improved by utilizing the high specific surface area and controllable flow state of the microfluidic reactor.
It significantly increased the yield of Brazilian sweet protein, shortened the production cycle, improved the equipment utilization rate of fermenters, achieved higher methanol conversion rate and lower methanol residue, and increased the yield by 20% to 30%.
Smart Images
Figure CN121826089A_ABST
Abstract
Description
Technical Field
[0001] This invention belongs to the field of bioengineering technology, and in particular relates to a method and reaction apparatus for preparing Brazilian sweet protein using a microfluidic reactor. Background Technology
[0002] Brazil protein is a naturally sweet protein with high sweetness and has broad application prospects in the food and beverage industries. Currently, the preparation of Brazil protein mainly relies on microbial fermentation. This method typically involves directly adding methanol into a fermenter, utilizing the fermenter's own stirring and mass transfer capabilities to allow microorganisms to contact and metabolize the methanol, thereby generating the target product.
[0003] However, this method has significant limitations: due to the limited mixing efficiency within the fermenter, methanol is unevenly dispersed in the fermentation broth, resulting in locally excessively high or low concentrations and poor mass transfer, which in turn affects the full utilization of methanol by microorganisms. Low methanol mass transfer efficiency not only limits the reaction rate but also easily leads to excessive methanol residue, inhibiting cell growth and product synthesis. Ultimately, this results in low yields and long production cycles for Brazil gluten, hindering the efficiency and economic viability of its industrial production.
[0004] In recent years, microfluidic reactor technology has demonstrated significant advantages in the biochemical field as an important means of process intensification. This technology, by conducting reactions within channels at the micrometer or submillimeter scale, leverages the large specific surface area, high mass and heat transfer efficiency, and controllable flow state to achieve rapid and uniform mixing of reactants, significantly improving reaction rates and product selectivity. Furthermore, microfluidic reactors feature continuous flow operation, easy process control, and high safety, making them particularly suitable for biocatalysis and fermentation processes with stringent mass transfer and reaction conditions.
[0005] Although microfluidic technology has been successfully applied in many chemical processes, there are few studies on its use in the fermentation of Brazilian sweet protein to improve methanol feeding efficiency and enhance the interaction between microorganisms and substrates. Summary of the Invention
[0006] The purpose of this invention is to overcome the shortcomings of the prior art by providing a method and device for preparing Brazil brittle protein using a microfluidic reactor, which has a short production cycle, high equipment utilization of the fermenter, and high yield of Brazil brittle protein.
[0007] To achieve the above objectives, the technical solution adopted by the present invention is: a method for preparing Brazil protein using a microfluidic reactor, comprising the following steps:
[0008] The fermentation broth in the fermenter is continuously fed to the microfluidic reactor at a first flow rate;
[0009] The methanol-containing substrate is continuously fed into the microfluidic reactor at a second flow rate;
[0010] The fermentation broth and the substrate methanol solution are mixed and reacted in the microfluidic reactor for a predetermined residence time.
[0011] The mixture treated by the microfluidic reactor is returned to the fermenter, whereby Brazil protein is generated and accumulated.
[0012] Furthermore, the methanol-containing substrate is a methanol solution with a concentration of 50%-100% (V / V).
[0013] Furthermore, the first flow rate is 5-30 ml / min.
[0014] Furthermore, the second flow rate is 0.05-0.3 ml / min.
[0015] Furthermore, the reaction temperature within the microfluidic reactor is controlled between 20°C and 35°C.
[0016] Furthermore, the reaction time between the fermentation broth and the methanol-containing substrate in the microfluidic reactor is 2-5 minutes.
[0017] A reaction apparatus for carrying out a method for preparing brassinolide using a microfluidic reactor, comprising:
[0018] Fermentation tank;
[0019] A microfluidic reactor, the outlet of which is connected to the fermenter via a pipeline;
[0020] The first conveying unit is used to convey the fermentation liquid in the fermenter to the microflow field reactor at a first flow rate;
[0021] The second conveying unit is used to convey the methanol-containing substrate to the microfluidic reactor at a second flow rate;
[0022] A mixing unit is disposed between the first conveying unit, the second conveying unit and the microfluidic reactor, and is used to mix the fermentation broth conveyed by the first conveying unit and the methanol-containing substrate conveyed by the second conveying unit.
[0023] Furthermore, the first conveying unit and the second conveying unit are peristaltic pumps.
[0024] Furthermore, the mixing unit is a Y-type mixer.
[0025] Furthermore, the microflow reactor is a tubular reactor made of perfluoroalkoxyalkane material.
[0026] Due to the application of the above technical solution, the present invention has the following advantages compared with the prior art:
[0027] This invention moves the mixing reaction of fermentation broth and methanol to a microfluidic reactor. Through the synergistic reaction of extremely high fermentation broth circulation rate and extremely low methanol flow rate, instantaneous and uniform dilution of methanol is achieved in the microfluidic reactor, keeping its concentration below a safe threshold and maintaining high cell activity and density. This allows operation at a higher average methanol replenishment rate, increases total methanol consumption, and allows more substrate to be efficiently converted into product. Compared with traditional fermentation methods, the unit yield of Brazil gluten can be increased by 20% to 30%.
[0028] Secondly, the huge specific surface area of the micron-level channels in the microfluidic reactor improves the contact efficiency between methanol and microorganisms, greatly accelerates the reaction rate, and increases the yield. Attached Figure Description
[0029] The technical solution of the present invention will be further described below with reference to the accompanying drawings:
[0030] Figure 1 This is a schematic flowchart of the method for preparing Brazilian sweet protein using a microfluidic reactor in this invention;
[0031] Figure 2 This is a schematic diagram of the reaction apparatus in this invention;
[0032] Figure 3 This is a graph showing the formation curve of Brazil protein in Embodiment 1 of the present invention;
[0033] Figure 4 This is a graph showing the methanol replenishment acceleration rate in Example 1 of the present invention;
[0034] Figure 5 This is a graph showing the change in OD600 of bacterial biomass in Example 1 of the present invention.
[0035] Figure 6 This is a methanol residue curve from Example 1 of the present invention;
[0036] Figure 7 This is a comparison chart of the formation curves of Brazilin in Examples 1 and 2 of the present invention;
[0037] Figure 8 This is a graph showing the methanol replenishment acceleration rate in Example 2 of the present invention;
[0038] Figure 9 This is a comparison curve of the changes in bacterial biomass OD600 in Examples 1 and 2 of the present invention;
[0039] Figure 10 This is a comparison curve of methanol residue in Examples 1 and 2 of the present invention;
[0040] Figure 11 This is a comparison chart of the formation curves of Brazil protein in Examples 1 and 3 of the present invention;
[0041] Figure 12 This is a comparison curve of the changes in OD600 of bacterial biomass in Examples 1 and 3 of the present invention;
[0042] Figure 13 This is a comparison curve of methanol residue in Examples 1 and 3 of the present invention;
[0043] Figure 14 This is a comparison chart of the formation curves of Brazil protein in Examples 1 and 4 of the present invention;
[0044] Figure 15 This is a comparison chart of the formation curves of Brazil protein in Examples 1 and 5 of the present invention;
[0045] Figure 16 This is a comparison chart of the formation curves of Brazil protein in Examples 1 and 6 of the present invention;
[0046] Figure 17 This is a comparison chart of the formation curves of Brazilin in Examples 1 and 7 of the present invention;
[0047] Figure 18 This is a comparison chart of the formation curves of Brazilin in Examples 1 and 8 of the present invention;
[0048] The components include: fermenter 1, microfluidic reactor 2, first conveying unit 3, second conveying unit 4, and mixing unit 5. Detailed Implementation
[0049] To enable those skilled in the art to better understand the present application, the technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present application, and not all embodiments. Based on the embodiments in the present application, all other embodiments obtained by those of ordinary skill in the art without creative effort should fall within the scope of protection of the present application.
[0050] See Figure 1 This invention discloses a method for preparing Brazilian sweet protein using a microfluidic reactor, comprising the following steps:
[0051] S1. The fermentation broth in the fermenter is continuously fed to the microflow reactor at a first flow rate of 5-30 ml / min. This step transfers the fermented broth to the flow field reactor.
[0052] S2. The methanol-containing substrate is continuously fed into the microfluidic reactor at a second flow rate of 0.05-0.3 ml / min. The first flow rate is greater than the second flow rate. This ensures that the inflow of methanol-containing substrate into the microfluidic reactor is much lower than that of the fermentation broth. This ensures that the high concentration of methanol at the inlet of the microfluidic reactor can be instantly diluted to below the safety threshold by a large amount of circulating fermentation broth. This creates a stable methanol concentration environment in the microfluidic reactor that is far below the poisoning threshold, allowing microorganisms to continuously and efficiently synthesize the target product under this optimal environment.
[0053] In addition, the methanol-containing substrate in step S2 is a methanol solution with a concentration of 50%-100% (V / V), and the aforementioned safety threshold represents the methanol fermentation broth diluted to ≤1g / L.
[0054] S3. The fermentation broth and the substrate methanol solution are mixed and reacted in the microfluidic reactor for a preset residence time, which is in the range of 2-5 minutes. The minimum residence time of 2 minutes ensures that the methanol-containing substrate and the fermentation broth can have sufficient contact and mass transfer in the microfluidic reactor. However, an excessively long residence time will reduce the number of cycles of the fermentation broth per unit time, thereby weakening the overall efficiency improvement advantage brought about by the high-frequency circulation of this invention. Therefore, the maximum residence time is 5 minutes.
[0055] The reaction temperature in the microfluidic reactor is controlled between 20°C and 35°C, because 20-35°C is the optimal growth temperature range for microorganisms that produce Brazil protein.
[0056] S4. The mixture treated by the microfluidic reactor is returned to the fermenter, thereby generating and accumulating Brazil gluten in the fermenter.
[0057] See Figure 2 The preparation method described above also includes a reaction apparatus for carrying out the method. This apparatus includes a fermenter 1, a microfluidic reactor 2, a first conveying unit 3, a second conveying unit 4, and a mixing unit 5. The outlet of the microfluidic reactor 2 is connected to the fermenter 1 via a pipeline. The first conveying unit 3 conveys the fermentation broth from the fermenter 1 to the microfluidic reactor 2 at a first flow rate. The second conveying unit 4 conveys a methanol-containing substrate to the microfluidic reactor 2 at a second flow rate. The mixing unit 5 is disposed between the first conveying unit 3, the second conveying unit 4, and the microfluidic reactor 2, and is used to mix the fermentation broth conveyed by the first conveying unit 3 and the methanol-containing substrate conveyed by the second conveying unit 4.
[0058] Furthermore, the first conveying unit 3 and the second conveying unit 4 are peristaltic pumps; the mixing unit is a Y-type mixer; and the microflow reactor 2 is a tubular reactor made of perfluoroalkoxyalkane material.
[0059] The above-mentioned reaction apparatus enables the preparation of brassin using a microfluidic reactor, thereby increasing the yield.
[0060] The following examples illustrate the concepts, starting with a description of general materials and experimental methods:
[0061] 1. General materials
[0062] 1. Culture medium and solution:
[0063] The culture medium and solution preparation methods used in the embodiments of the present invention are as follows, but the scope of protection of the present invention is not limited to this specific formulation.
[0064] Seed culture medium: 20 g / L peptone, 10 g / L yeast extract, 10 g / L sodium chloride, 0.5 g / L magnesium sulfate heptahydrate, 10 g / L glycerol, dissolved and brought to volume with deionized water, sterilized at 121℃ for 20 min before use.
[0065] Fermentation medium: 20 g / L peptone, 10 g / L yeast extract, 13.4 g / L YNB, 10 g / L glycerol, 10% (v / v) 1M pH6.0 phosphate buffer, dissolved and brought to volume with deionized water, sterilized at 121℃ for 20 min.
[0066] Glycerin replenishment solution: Prepare 500ml of glycerin at a concentration of 50% (W / V), put it into a 500L replenishment bottle, sterilize at 121℃ for 20min, and cool to room temperature for later use.
[0067] 1M pH 6.0 Phosphate Buffer: Mix 868 ml of 1M potassium dihydrogen phosphate and 132 ml of 1M dipotassium hydrogen phosphate thoroughly, adjust the pH to 6.0 with phosphate, sterilize at 121°C for 20 min, and cool to room temperature for later use.
[0068] II. Analysis and Detection Methods:
[0069] Determination of Brazilian sweet protein concentration: High performance liquid chromatography (HPLC) was used. A Thermo Scientific Vanquish HPLC system with a Phenomenex luna 5u C18 column was employed; the flow rate was 0.5 ml / min; the column temperature was 35℃; the injection volume was 10 μL; the UV detector wavelength was 220 nm; mobile phase A was 0.1% TFA solution, and mobile phase B was acetonitrile, eluted according to the gradient shown in Table 1 below.
[0070]
[0071] The biomass of the cells was determined by spectrophotometry: the fermentation broth was diluted 100-500 times and the absorbance was measured at a wavelength of 600 nm.
[0072] The residual methanol concentration was determined using an SBA biosensor. After centrifuging the fermentation broth at 12,000 rpm for 3 minutes, the supernatant was taken and diluted 5 times according to the methanol concentration. The methanol concentration of the diluted sample was controlled to be below 1 g / L. The diluted supernatant was then sent to the SBA for methanol residue detection.
[0073] Furthermore, the microfluidic reactor is a tubular reactor made of PFA material, with an inner diameter of 3.0 mm and a total retention volume of 100 ml. The fermenter uses a 5L mechanically stirred fermenter with a Bailun BLBIOB control system.
[0074] Example 1: Traditional Fermentation Method
[0075] Seed culture: The preserved strain of glycerol was inoculated into three 250 ml Erlenmeyer flasks containing 50 ml of seed culture medium and cultured overnight at 30°C and 200 rpm with shaking to obtain the seed culture.
[0076] Fermentation culture: Inoculate 150 ml of seed culture into a 5L fermenter containing 2 L of fermentation medium.
[0077] Cell culture stage: Control the temperature at 30℃, stir at 500 rpm, aeration rate at 2 vvm, use 25% ammonia to control the pH at 5.5, and add 500 ml of glycerol solution at a rate of 15-18 ml / hr. This process continues for about 30 hours until OD. 600 When the dissolved oxygen level reaches 350-400, it rebounds to over 80%.
[0078] Reaction phase: 100% (V / V) methanol is continuously pumped directly into the fermenter using a peristaltic pump. The initial flow rate is 0.15 ml / min, dynamically adjusted according to the residual methanol concentration in the fermentation broth, with a maximum flow rate not exceeding 0.25 ml / min. The temperature is maintained at 30℃, the stirring speed at 800 rpm, the aeration rate at 2 vvm, and the pH is controlled at 5.5. The reaction lasts for approximately 90-100 hours.
[0079] Final results: After 100 hours of reaction, the concentration of carbapenem in the fermentation broth was approximately 3.15 g / L. The entire reaction process consumed approximately 1200 ml of methanol. The formation curve of carbapenem is shown in [Figure number missing]. Figure 3 The methanol replenishment acceleration rate is shown in the figure. Figure 4 The changes in OD600 during the bacterial biomass reaction process are shown in [the table below]. Figure 5The methanol residue detection results throughout the reaction process are shown in [link to relevant documentation]. Figure 6 .
[0080] Example 2:
[0081] The seed culture, fermentation culture, and cell culture stages are the same as in Example 1, in order to obtain a fermentation broth that can be used for the reaction.
[0082] Reaction phase:
[0083] The substrate methanol solution is delivered to the mixing unit at a rate of 0.15 ml / min via the second delivery unit.
[0084] The fermentation broth in the fermenter is delivered to the mixing unit at a rate of 30 ml / min via the first delivery unit.
[0085] After the two liquid streams are mixed in the mixing unit, they enter the microfluidic reactor and react at 30°C for about 3 minutes.
[0086] The reaction mixture is returned to the fermenter to generate and accumulate Brazil gluten.
[0087] The fermenter's parameters were maintained as follows: temperature 30℃, stirring speed 800 rpm, aeration rate 2 vvm, and pH 5.5. This cycle lasted for approximately 100 hours.
[0088] Final results: After 100 hours of reaction, the concentration of carbapenem in the fermentation broth reached approximately 4.05 g / L, representing a 28.6% increase in yield compared to Example 1. The carbapenem formation curve is shown in [Figure number missing]. Figure 7 The methanol replenishment rate can be increased and maintained at 0.3 ml / min for an extended period, with a total methanol consumption of approximately 1500-1600 ml. (See attached image.) Figure 8 The bacterial biomass OD600 during the reaction process increased by 8% compared to Case 1. Figure 9 The control of methanol residue during the reaction process was more stable compared to Example 1, see... Figure 10 .
[0089] Compared to Example 1, the yield of Brazil gluten protein was significantly increased in this embodiment.
[0090] Example 3
[0091] The difference between this embodiment and Embodiment 2 is that the flow rate of the second delivery unit is set to 0.17 ml / min initially, and further increased to 0.35 ml / min in the middle and later stages, while other conditions remain unchanged.
[0092] Results: After 100 hours of reaction, the concentration of brassinolide was approximately 2.95 g / L, and the yield was not significantly increased compared to Example 1. Figure 11During the reaction, the bacterial biomass OD600 was significantly lower than in Case 1, indicating that bacterial growth essentially ceased in the later stages. Figure 12 During the reaction, the residual concentration of methanol gradually accumulates, see... Figure 13 In Case Study 3, the flow rate (0.17-0.35 ml / min) exceeded the optimal range (0.15-0.3 ml / min), resulting in excessively high methanol concentration, stagnation of cell growth, hindered product synthesis, and no increase in yield.
[0093] Example 4
[0094] The difference between this embodiment and Embodiment 2 is that the flow rate of the first delivery unit is set to 50 ml / min, and the residence time in the 100 ml microfluidic reactor is shortened to about 2 minutes.
[0095] Results: After 100 hours of reaction, the concentration of brassinolide was approximately 3.62 g / L, representing a 15% increase in yield compared to Example 1. Figure 14 At the same time, and in Example 2 Figure 7 In comparison, although the yield of Brazil gluten was reduced, the increased yield still met the demand. The results showed that within the flow rate range of 5-50 ml / min in the first delivery unit, higher flow rates still significantly increased yield, and shorter chemical residence times also significantly increased yield. This indicates that within a certain range, residence time has no significant impact on yield, but excessively high or low flow rates weaken the microfluidic effect.
[0096] Example 5
[0097] The difference between this embodiment and Embodiment 2 is that the flow rate of the first delivery unit is set to 20 ml / min, and the residence time in the 100 ml microfluidic reactor is extended to about 5 minutes.
[0098] Results: After 100 hours of reaction, the concentration of brassinolide was approximately 3.76 g / L, representing a 19.5% increase in yield compared to Example 1. Figure 15 The results showed that within the flow rate range of 5-50 ml / min in the first delivery unit, a lower flow rate of 20 ml / min could still significantly increase the yield. At the same time, a longer chemical residence time could still significantly increase the yield. This indicates that within a certain range, the residence time has no significant effect on the yield, but excessively high or low flow rates will weaken the microflow field effect.
[0099] Example 6
[0100] The difference between this embodiment and Embodiment 2 is that the flow rate of the first delivery unit is increased to 80 ml / min, and the residence time in the 100 ml microfluidic reactor is about 1.2 minutes.
[0101] Results: After 100 hours of reaction, the concentration of brassinolide was approximately 3.36 g / L, representing a 6.6% increase in yield compared to Example 1. Figure 16 And in Figure 7 Compared to Example 2, the yield increase of brassinolide was very low. The results indicate that once the flow rate in the first delivery unit reaches 80 ml / min or higher, the microfluidic reactor cannot be fully utilized under such high flow rate conditions, and the yield increase of brassinolide is not significant.
[0102] Example 7
[0103] The difference between this embodiment and Embodiment 2 is that the flow rate of the first delivery unit is reduced to 5 ml / min, and the residence time in the 100 ml microfluidic reactor is extended to 20 minutes.
[0104] Results: After 100 hours of reaction, the concentration of brassinolide was approximately 3.48 g / L, representing a 10.5% increase in yield compared to Example 1. Figure 17 The results showed that within the flow rate range of 5-50 ml / min in the first delivery unit, a lower flow rate of 20 ml / min still significantly increased the yield, and a longer chemical residence time also significantly increased the yield. This indicates that within a certain range, residence time has no significant effect on yield, but excessively high or low flow rates weaken the microfluidic effect.
[0105] Example 8
[0106] The difference between this embodiment and Embodiment 2 is that the flow rate of the first delivery unit is reduced to 3 ml / min, and the residence time in the 100 ml microfluidic reactor is extended to 30 minutes.
[0107] Results: After 100 hours of reaction, the concentration of brassinolide was approximately 3.20 g / L, representing only a 1.6% increase in yield compared to Example 1. Figure 18 And and Figure 7 Compared to Example 2, the yield increase of brassinolide was relatively small. The results indicate that when the flow rate in the first delivery unit was reduced to below 5 ml / min, the microfluidic reactor effect could not be fully utilized at lower flow rates, and the yield increase of brassinolide was not significant.
[0108] In summary, Examples 2, 4, and 5 demonstrate that the microfluidic circulation method and related parameters of this invention can achieve a higher yield of Brazilian sweet protein than traditional methods.
[0109] The above-described embodiments are only used to illustrate the technical solutions of this application, and are not intended to limit them. Although this application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions of the embodiments of this application.
Claims
1. A method for preparing Brazil protein using a microfluidic reactor, characterized in that, Includes the following steps: The fermentation broth in the fermenter is continuously fed to the microfluidic reactor at a first flow rate; The methanol-containing substrate is continuously fed into the microfluidic reactor at a second flow rate; The fermentation broth and the substrate methanol solution are mixed and reacted in the microfluidic reactor for a predetermined residence time. The mixture treated by the microfluidic reactor is returned to the fermenter, whereby Brazil protein is generated and accumulated.
2. The method for preparing Brazil protein using a microfluidic reactor as described in claim 1, characterized in that: The methanol-containing substrate is a methanol solution with a concentration of 50%-100% (V / V).
3. The method for preparing Brazilian sweet protein using a microfluidic reactor as described in claim 1, characterized in that: The first flow rate is 5-30 ml / min.
4. The method for preparing Brazil protein using a microfluidic reactor as described in claim 1, characterized in that: The second flow rate is 0.05-0.3 ml / min.
5. The method for preparing Brazilian sweet protein using a microfluidic reactor as described in claim 1, characterized in that: The reaction temperature inside the microfluidic reactor is controlled between 20°C and 35°C.
6. The method for preparing Brazilian sweet protein using a microfluidic reactor as described in claim 1, characterized in that: The fermentation broth in the microfluidic reactor reacts with the methanol-containing substrate for 2-5 minutes.
7. A reaction apparatus for implementing the method of preparing Brazilian sweet protein using a microfluidic reactor according to any one of claims 1 to 6, characterized in that, include: Fermentation tank; A microfluidic reactor, the outlet of which is connected to the fermenter via a pipeline; The first conveying unit is used to convey the fermentation liquid in the fermenter to the microflow field reactor at a first flow rate; The second conveying unit is used to convey the methanol-containing substrate to the microfluidic reactor at a second flow rate; A mixing unit is disposed between the first conveying unit, the second conveying unit and the microfluidic reactor, and is used to mix the fermentation broth conveyed by the first conveying unit and the methanol-containing substrate conveyed by the second conveying unit.
8. The reaction apparatus as described in claim 7, characterized in that: The first conveying unit and the second conveying unit are peristaltic pumps.
9. The reaction apparatus as described in claim 7, characterized in that: The mixing unit is a Y-type mixer.
10. The reaction apparatus as described in claim 7, characterized in that: The microflow reactor is a tubular reactor made of perfluoroalkoxyalkane material.