Device for synthesizing sodium sarcosinate through micro-channel continuous flow

Abstract

The invention discloses a device for synthesizing sodium sarcosinate through micro-channel continuous flow, and relates to the technical field of sodium sarcosinate synthesis. The device comprises a glycine methylation reaction channel unit, a catalyst recovery assembly, a sarcosine crystallization and purification channel unit, a sarcosine neutralization reaction pipeline and a sodium sarcosine concentration and crystallization one-piece tank unit, the glycine methylation reaction channel unit comprises a raw material mixing pre-reaction pipe, a catalyst adding tank, a plunger type high-pressure pump and a high-pressure micro-channel reaction pipeline combination; the sarcosine crystallization and purification channel unit comprises a hydrogen volatilization channel, a formaldehyde volatilization and concentration channel and a glycine crystallization channel; the sodium sarcosinate concentration and crystallization integrated tank unit comprises a concentration tank, a first crystallization tank, a redissolution tank and a second crystallization tank. According to the invention, the reaction is carried out through the continuous microchannel, the reaction process separation is simpler than the traditional reaction process separation, the raw material utilization rate is high, and the problems of high preparation cost, troublesome operation, incapability of continuous production and the like of the existing glycine methylation method are solved.

Description

TECHNICAL FIELD

[0001] The application belongs to the technical field of sarcosine sodium synthesis, and particularly relates to a device for continuously synthesizing sarcosine sodium through a microchannel. BACKGROUND

[0002] Sarcosine sodium is an important chemical raw material and is widely used in the fields of medicine, cosmetics, food and the like. In the prior art, there are three methods for preparing sarcosine sodium. One is a chloroacetic acid method, that is, chloroacetic acid reacts with monomethylamine under the action of sodium hydroxide to generate sarcosine sodium. Another method is a hydroxyacetonitrile method, which can also be referred to as a hydrocyanic acid method. The third method is a glycine methylation method. Among them, the hydroxyacetonitrile method is a commonly used method in the field for preparing sarcosine sodium. The hydroxyacetonitrile method is highly toxic and needs to be strictly controlled. The existing glycine methylation method is mainly a tank reaction, which requires high conditions and cannot be continuously reacted, and is troublesome to separate and purify, resulting in a high preparation cost. SUMMARY

[0003] The purpose of the present application is to provide a device for continuously synthesizing sarcosine sodium through a microchannel. The reaction is carried out through a continuous microchannel, the reaction process is relatively simple compared with the traditional method, the utilization rate of raw materials is high, and the problems of high preparation cost, troublesome operation and inability to continuously produce in the existing glycine methylation method are solved.

[0004] To solve the above technical problems, the present application is realized by the following technical scheme: The present application is a device for continuously synthesizing sarcosine sodium through a microchannel, which comprises a glycine methylation reaction channel unit, a catalyst recovery assembly, a sarcosine crystallization and purification channel unit, a sarcosine neutralization reaction pipeline and a sarcosine sodium concentration and crystallization integrated tank unit. The glycine methylation reaction channel unit comprises a raw material mixing pre-reaction pipe, a catalyst addition tank, a plunger type high-pressure pump and a high-pressure microchannel reaction pipeline combination. The catalyst addition tank is arranged at the pre-reaction end section of the raw material mixing pre-reaction pipe. A hydrogen gas discharge pipe is arranged on the output pipeline of the raw material mixing pre-reaction pipe. The plunger type high-pressure pump pressurizes the mixed pre-reaction raw materials into the high-pressure microchannel reaction pipeline combination. The gas-liquid mixture after the reaction of the high-pressure microchannel reaction pipeline combination is discharged into the catalyst recovery assembly to recover the catalyst. The sarcosine crystallization and purification channel unit comprises a hydrogen gas volatilization channel, a formaldehyde volatilization and concentration channel and a glycine crystallization channel. The liquid after the catalyst recovery assembly recovers the catalyst flows into the hydrogen gas volatilization channel to volatilize and recover under reduced pressure. The liquid in the hydrogen gas volatilization channel flows into the formaldehyde volatilization and concentration channel to volatilize formaldehyde and water vapor under reduced pressure distillation. The liquid in the formaldehyde volatilization and concentration channel flows into the glycine crystallization channel to crystallize and purify the sarcosine solution. After crystallization in the glycine crystallization channel, the liquid flows into the sarcosine neutralization reaction pipeline. Alkali solution is introduced into the inlet of the sarcosine neutralization reaction pipeline to carry out the neutralization reaction. The sodium sarcosinate concentration and crystallization integrated tank unit includes a concentration tank, a first crystallization tank, a resolution tank, and a second crystallization tank. After the reaction in the sarcosinate neutralization reaction pipeline is completed, the liquid flows into the concentration tank for depressurization concentration, and then is discharged into the first crystallization tank for the first low-temperature depressurization crystallization. The crystals at the bottom of the first crystallization tank are pumped into the resolution tank for dissolution, and then discharged into the second crystallization tank for the second low-temperature depressurization crystallization to obtain sodium sarcosinate crystals.

[0005] The present invention is further configured such that the raw material mixing pre-reaction tube includes a pre-reaction coarse tube, a raw material inlet tube, a catalyst inlet tube, a hydrogen outlet tube, and a raw material outlet tube. The two ends of the pre-reaction coarse tube are respectively connected to the raw material inlet tube and the raw material outlet tube. A raw material inlet branch tube is provided in the middle of the raw material inlet tube. A vertically upward catalyst inlet tube is provided at the top of the pre-reaction coarse tube near the raw material outlet tube. The bottom discharge port of the catalyst inlet tank is connected to the catalyst inlet tube. A hydrogen outlet tube is connected to the middle section of the raw material outlet tube. The raw material liquid, which is mixed in the raw material inlet pipe and the raw material addition branch pipe, flows into the pre-reaction coarse pipe at a pressure of 0.11-0.12 MPa. The raw material liquid, which is mixed in the raw material inlet pipe and the raw material addition branch pipe, can only flow into the raw material outlet pipe 15-20 minutes after entering the pre-reaction coarse pipe.

[0006] The present invention is further configured such that the catalyst addition tank includes a tank body, a conical bottom, and a pressurized tank cover. The bottom of the tank body is provided with a conical bottom, and the conical bottom is connected to the catalyst addition pipe through a connecting pipe. The pressurized tank cover is provided with a pressurized air inlet pipe, a pressurized air outlet pipe, and a feeding pipe. The pressurized air inlet pipe and the pressurized air outlet pipe ventilate and pressurize the catalyst addition tank. A micro-vibration motor is provided on the outer wall of the conical bottom.

[0007] The present invention is further configured such that the high-pressure microchannel reaction pipeline assembly includes a booster pipe, a U-shaped connecting pipe, and an injection pipe. The outlet port of the plunger-type high-pressure pump is connected to one end of the first booster pipe via a connecting long pipe. The booster pipe and the U-shaped connecting pipe are sequentially and alternately connected to form multiple sections of bent pipe. The booster pipe and the U-shaped connecting pipe are placed in the same horizontal plane. The outlet end of the last booster pipe is connected to an injection pipe. The injection pipe includes a thick pipe section and a thin pipe section. The inner diameter of the thick pipe section is equal to the inner diameter of the U-shaped connecting pipe. The inner diameter of the thick pipe section is 3-5 times the inner diameter of the thin pipe section. The inner diameter of the booster pipe is 3-5 times the inner diameter of the U-shaped connecting pipe. Both the booster pipe and the U-shaped connecting pipe are wrapped with heating jackets. The temperature inside the booster pipe and the U-shaped connecting pipe is 80-100℃, and the pressure inside the booster pipe is 0.6-0.9MPa.

[0008] The present invention is further configured such that the catalyst recovery assembly includes an inner filter ball and an outer cover ball. The inner filter ball has uniformly distributed filter pores. The inner filter ball has a liquid injection pipe on one side and a downward-facing catalyst discharge pipe at the bottom. The outer cover ball is fitted over the inner filter ball and the two are concentric. The end of the thin tube section of the injection pipe is connected to the liquid injection pipe. The catalyst discharge pipe extends from the outer cover ball to the outside. The catalyst discharge pipe is equipped with a solenoid valve. The outer cover ball is equipped with a filter liquid supply pipe.

[0009] The present invention is further configured such that the hydrogen evaporation channel includes a first box body and a first box cover, and the formaldehyde evaporation and concentration channel includes a second box body and a second box cover, wherein a first suction tube is provided at the right end of the first box cover and a second suction tube is provided at the right end of the second box cover. The first box and the second box have the same structure. The second box is provided with an overflow trough that sinks down in stages. All the overflow troughs in front are provided with an overflow port on the right side. The second box is provided with an inlet pipe on the left side near the top wall and an outlet pipe on the right side near the bottom.

[0010] The present invention is further configured such that the temperature inside the first box is 0-5℃, and the gas pressure inside the hydrogen evaporation channel is 0.08-0.09MPa; The internal temperature of the second box is 55-60℃, and the gas pressure in the formaldehyde volatilization and concentration channel is 0.07-0.08MPa.

[0011] The present invention is further configured such that the glycine crystallization channel includes a heating jacket, a liquid inlet box, multiple crystallization precipitation cylinders that are progressively lowered, a purification liquid box, a stirring mounting cover, and multiple stirring devices; The crystallization precipitation cylinder is equipped with a circular stirring tank and a settling tank. The circular stirring tank and the settling tank are connected at the bottom and the bottom of the connecting channel is inclined. The bottom of the circular stirring tank is connected to a downward-extending conical crystallization tank. The bottom of the conical crystallization tank is equipped with a suction and crystal discharge pipe. The right side wall of the circular stirring tank is equipped with an overflow channel. The left top wall of the settling tank is equipped with a square slot. The liquid inlet box is provided with a drain connector on the right side, and the drain connector is locked in the square slot of the first crystallization precipitator. The overflow channel on the right side of the crystallization precipitator is locked in the square slot of the next crystallization precipitator in turn. The overflow channel on the right side of the last crystallization precipitator is locked on the top left wall of the purification liquid box. The sarcosine drain pipe is provided on the right side wall of the purification liquid box near the bottom. The stirring installation cover is sealed on the top of the heating jacket. The heating jacket is sealed outside the liquid inlet box, multiple crystallization precipitation cylinders and purification liquid box in successive stages. An acid adjustment drip tube is provided on the stirring installation cover directly above the liquid inlet box. A stirring device is provided on the stirring installation cover at the position corresponding to each crystallization precipitation cylinder. The temperature inside the crystallization precipitation cylinder is 0-5℃.

[0012] The present invention is further configured such that the sarcosine neutralization reaction pipeline includes a neutralization reaction thick pipe, a neutralization inlet pipe and a reaction outlet pipe, wherein the pH value of the mixed liquid in the neutralization reaction thick pipe is between 8.5 and 9.0, and an alkali solution inlet pipe is connected to the middle of the neutralization inlet pipe, wherein the alkali solution discharged into the alkali solution inlet pipe is 30% sodium hydroxide. The raw material liquid, which is mixed with the neutralization inlet pipe and the alkali inlet pipe, enters the neutralization reaction coarse pipe 71 and can flow into the reaction outlet pipe after 25-30 minutes.

[0013] The present invention is further configured such that the tank structures of the concentration tank, the first crystallization tank, the remelting tank, and the second crystallization tank are identical; The concentration tank, the first crystallization tank and the second crystallization tank are all provided with thin liquid inlet pipes on the left side near the top side wall, and the remelting tank is provided with coarse liquid inlet pipes on the left side near the top side wall. Both the first and second crystallization tanks are equipped with coarse crystal discharge pipes at the bottom, and both the concentration tank and the remelting tank are equipped with fine liquid discharge pipes at the bottom. The fine drain pipe of the concentration tank is connected to the fine inlet pipe of the first crystallization tank, the coarse drain pipe of the first crystallization tank is connected to the coarse inlet pipe of the remelting tank, and the fine drain pipe of the remelting tank is connected to the fine inlet pipe of the second crystallization tank. An external discharge pipe for crystallization liquid is provided at the middle right side position of the first crystallizer and the second crystallizer. The concentration tank, the first crystallization tank, the remelting tank, and the second crystallization tank are all equipped with tank covers of the same structure. The tank covers are equipped with an adjusting air inlet pipe, an adjusting air outlet pipe, and a stirring rack. The adjusting air inlet pipe is equipped with an adjusting liquid addition pipe, and the stirring rack is equipped with a second stirring device that is inserted into the tank.

[0014] The present invention has the following beneficial effects: 1. In this invention, the glycine methylation reaction is carried out in a channel. The pipeline allows hydrogen to mix more fully with the liquid, thereby reducing the reaction pressure, making the reaction more thorough, shortening the reaction time, enabling continuous output of reaction products, improving overall reaction efficiency, and reducing labor costs.

[0015] 2. The catalyst recovery component of this invention can recover the catalyst without interrupting the reaction, with high recovery efficiency and minimal impact on catalyst activity.

[0016] 3. The sarcosine crystallization purification channel unit can recover hydrogen gas, which can be directly used as an initial reaction feedstock. The small amount of impurities in the hydrogen gas are also components of the reaction feedstock, so there is basically no need to purify the recovered hydrogen gas before it can be used as a feedstock. The formaldehyde evaporated under reduced pressure still contains water, which can cause the volatilized formaldehyde gas to condense into a 30-50% formaldehyde solution after condensation, which can be used as a feedstock without purification. The sarcosine contained in the crystallized glycine does not need to be purified after dissolution and can be used directly as a feedstock. The overall separation process basically does not require purification processes, and the recovered feedstock can be directly used in the initial reaction, which greatly improves the utilization rate of feedstock.

[0017] 4. The solution reacting in the sarcosine neutralization reaction pipeline can be concentrated, crystallized, redissolved, and recrystallized to improve product purity and yield. It can also achieve continuous crystallization and purification without removing the raw materials from the tank for crystallization and purification.

[0018] Of course, any product implementing this invention does not necessarily need to achieve all of the advantages described above at the same time. Attached Figure Description

[0019] To more clearly illustrate the technical solutions of the embodiments of the present invention, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0020] Figure 1 A schematic diagram of the apparatus for the continuous flow synthesis of sodium sarcosinate in microchannels.

[0021] Figure 2 This is a schematic diagram showing the location of the raw material mixing pre-reaction tube, the high-pressure microchannel reaction pipeline combination, and the catalyst recovery component.

[0022] Figure 3 This is an exploded structural diagram showing the locations of the raw material mixing pre-reaction tube, the high-pressure microchannel reaction pipeline combination, and the catalyst recovery component.

[0023] Figure 4 This is a schematic diagram of the raw material mixing pre-reaction tube.

[0024] Figure 5 This is a schematic diagram of the internal gas layer after the last booster pipe is connected to the injection pipe.

[0025] Figure 6 This is a schematic diagram of the explosion structure of the hydrogen volatilization channel, the formaldehyde volatilization and concentration channel, and the glycine crystallization channel.

[0026] Figure 7 This is a schematic diagram of the second box.

[0027] Figure 8 This is a schematic diagram of the cross-sectional structure of a crystallization precipitation cylinder.

[0028] Figure 9 This is a schematic diagram of the integrated tank unit for sodium sarcosinate concentration and crystallization.

[0029] Figure 10 This is a schematic diagram of the sarcosine neutralization reaction pathway.

[0030] Figure 11 A schematic diagram illustrating the process principle of continuous flow synthesis of sodium sarcosinate in microchannels.

[0031] The attached diagram lists the components represented by each number as follows: 1. Raw material mixing pre-reaction tube; 11. Raw material mixing pre-reaction tube; 111. Tank body; 112. Conical bottom; 12. Plunger-type high-pressure pump; 13. Pre-reaction coarse tube; 131. Raw material inlet pipe; 132. Raw material addition branch pipe; 133. Raw material outlet pipe; 14. Catalyst addition pipe; 15. Hydrogen discharge pipe; 2. High-pressure microchannel reaction pipeline assembly; 21. Pressurization pipe; 211. Gas layer; 22. U-shaped connecting pipe; 23. Injection pipe; 3. Catalyst recovery assembly; 31. Outer cover ball; 311. Filtrate supply pipe; 32. Inner filter ball; 321. Liquid injection pipe; 322. Catalyst discharge pipe; 4. Hydrogen volatilization channel; 41. First box body; 42. First box cover; 421. First suction pipe; 5. Formaldehyde volatilization and concentration channel; 51. Second box body; 511. Overflow tank; 512. Overflow port; 52. 521. Second suction pipe; 53. Inlet pipe; 54. Outlet pipe; 6. Glycine crystallization channel; 61. Stirring installation cover; 611. Acid adjustment drip pipe; 612. Stirring device; 62. Inlet box; 63. Crystallization precipitation cylinder; 631. Circular stirring tank; 632. Settling tank; 633. Conical crystallization tank; 634. Overflow channel; 64. Purified liquid box; 65. Heating jacket; 7. Sarcosine neutralization reaction pipeline; 71. Neutralization reaction coarse pipe; 72. Neutralization inlet pipe; 721. Alkali solution addition pipe; 73. Reaction outlet pipe; 8. Concentration tank; 9. First crystallization tank; 91. First crystallization tank thin inlet pipe; 92. Outlet crystallization liquid discharge pipe; 93. Tank cover; 931. Adjusting air inlet pipe; 932. Adjusting liquid addition pipe; 933. Adjusting air outlet pipe; 801. Redissolving tank; 802. Second crystallization tank. Detailed Implementation

[0032] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0033] Please see Figures 1-11 The present invention is a device for continuous flow synthesis of sodium sarcosinate in microchannels, comprising a glycine methylation reaction channel unit, a catalyst recovery component 3, a sarcosine crystallization and purification channel unit, a sarcosine neutralization reaction pipeline 7, and a sodium sarcosinate concentration and crystallization integrated tank unit. The glycine methylation reaction channel unit includes a raw material mixing pre-reaction tube 1, a catalyst addition tank 11, a plunger-type high-pressure pump 12, and a high-pressure microchannel reaction pipeline assembly 2. The raw material mixing pre-reaction tube 1 is equipped with a catalyst addition tank 11 at the end of the pre-reaction section. A hydrogen exhaust pipe 15 is provided on the output pipe of the raw material mixing pre-reaction tube 1. The plunger-type high-pressure pump 12 pressurizes the mixed pre-reaction raw materials into the high-pressure microchannel reaction pipeline assembly 2. The raw material glycine solution (concentration 15-25%) and the raw material formaldehyde solution (concentration 20-30%) are mixed and then introduced into the raw material mixing pre-reaction tube 1 for pre-reaction (reaction temperature 40-50℃). Near the end of the pre-reaction, palladium-on-carbon catalyst particles (particle size 0.3-0.6mm) are added, followed by the introduction of sufficient hydrogen gas. The mixture is then quickly drawn into the plunger-type high-pressure pump 12. After a certain amount of reaction liquid accumulates in the plunger-type high-pressure pump 12, it is forced under high pressure into the high-pressure microchannel reaction pipeline assembly 2 for channel reaction. Within the high-pressure microchannel reaction pipeline assembly 2, the reaction liquid flows, carrying hydrogen gas within the pipeline. Due to the flowing liquid and the flow of bubbles, the catalyst particles float uniformly within the reaction liquid, achieving the channel reaction. Before introducing the liquid, sufficient hydrogen gas is introduced into the high-pressure microchannel reaction pipeline assembly 2 to remove air. This hydrogen gas purging process is performed before each reaction start-up to remove any remaining air.

[0034] After the reaction is completed, the gas-liquid mixture of the high-pressure microchannel reaction pipeline assembly 2 is discharged into the catalyst recovery assembly 3 to recover the catalyst; the catalyst is filtered and recovered in the catalyst recovery assembly 3.

[0035] The sarcosine crystallization purification channel unit includes a hydrogen evaporation channel 4, a formaldehyde evaporation and concentration channel 5, and a glycine crystallization channel 6. After the catalyst is recovered by the catalyst recovery component 3, the liquid flows into the hydrogen evaporation channel 4 for vacuum evaporation and recovery. The liquid in the hydrogen evaporation channel 4 flows into the formaldehyde evaporation and concentration channel 5 for vacuum distillation to evaporate formaldehyde and water vapor. The liquid in the formaldehyde evaporation and concentration channel 5 flows into the glycine crystallization channel 6 for crystallization and purification of the sarcosine solution. Hydrogen has extremely low solubility in solutions at sub-atmospheric pressure. Combined with low temperatures (room temperature or 0-5℃), the basic raw material solution contains very little hydrogen. During the flow of the reaction solution in hydrogen evaporation channel 4, a large amount of hydrogen evaporates and is drawn off for reuse, entering formaldehyde evaporation and concentration channel 5 for heating and concentration (the liquid from hydrogen evaporation channel 4 enters formaldehyde evaporation and concentration channel 5 in stages, with each drainage lasting 60 seconds, followed by a 3-5 minute wait before the next drainage), ensuring that the internal pressure of formaldehyde evaporation and concentration channel 5 does not fluctuate significantly. This facilitates the evaporation of the reaction solution (formaldehyde and water; due to the sub-atmospheric pressure, water boils at 60-70℃, and evaporation is rapid here), allowing most of the water and formaldehyde (formaldehyde is more volatile than water) to evaporate. The remaining glycine and sarcosine solution enters glycine crystallization channel 6, where low-temperature, low-pressure crystallization occurs, allowing the glycine crystals to be recycled.

[0036] After crystallization in the glycine crystallization channel 6, the liquid flows into the sarcosine neutralization reaction pipeline 7. Alkali solution is introduced into the inlet of the sarcosine neutralization reaction pipeline 7 to carry out the neutralization reaction. After crystallization in glycine crystallization channel 6, the liquid is sarcosine solution, which is mixed with sodium hydroxide (concentration 30-50%) and reacted at room temperature for 15-30 minutes (the pH value of the reaction is 8.5-9.0). Then it enters the concentration tank 8 and is titrated with sulfuric acid or hydrochloric acid to adjust the pH value.

[0037] The sodium sarcosinate concentration and crystallization integrated tank unit includes a concentration tank 8, a first crystallization tank 9, a resolution tank 801, and a second crystallization tank 802. After the reaction in the sarcosinate neutralization reaction pipeline 7 is completed, the liquid flows into the concentration tank 8 for vacuum concentration, and then is discharged into the first crystallization tank 9 for the first low-temperature vacuum crystallization. The crystals at the bottom of the first crystallization tank 9 are sucked into the resolution tank 801 for dissolution, and then discharged into the second crystallization tank 802 for the second low-temperature vacuum crystallization to obtain sodium sarcosinate crystals.

[0038] Concentration is carried out under reduced pressure and heating in concentration tank 8, with a pressure of 0.6-0.8 atmospheres and a heating temperature of 60-70℃. The concentration process continues until the sarcosine neutralization reaction pipeline 7 continuously introduces new liquid. After concentration, no crystallization occurs. During concentration, sulfuric acid or hydrochloric acid is continuously added to adjust the pH value (7.7-8.0) to prevent side reactions from occurring in a strongly alkaline environment.

[0039] The concentration tank 8 is started and opened every once in a while to discharge concentrated liquid into the tank for low-temperature crystallization (0-5℃). After crystallization for a period of time, part of the reaction liquid (the upper layer) will be discharged from the first crystallization tank 9. When the crystals accumulate to a certain amount, they are drawn from the bottom of the first crystallization tank 9 to the redissolution tank 801 for redissolution (water is discharged or ethanol is added appropriately), stirred and dissolved, and then discharged into the second crystallization tank 802 for a second low-temperature reduced pressure crystallization.

[0040] The supernatant discharged from the first crystallization tank 9 can be discharged into another concentration tank for secondary concentration and then crystallization 1-2 times (not shown in the figure) to improve the recovery rate.

[0041] The raw material mixing pre-reaction pipe 1 includes a pre-reaction coarse pipe 13, a raw material inlet pipe 131, a catalyst addition pipe 14, a hydrogen exhaust pipe 15, and a raw material outlet pipe 133. The two ends of the pre-reaction coarse pipe 13 are respectively connected to the raw material inlet pipe 131 and the raw material outlet pipe 133. A raw material addition branch pipe 132 is provided in the middle of the raw material inlet pipe 131. A vertically upward catalyst addition pipe 14 is provided at the top of the pre-reaction coarse pipe 13 near the raw material outlet pipe. The bottom discharge port of the catalyst addition tank 11 is connected to the catalyst addition pipe 14. The middle section of the raw material outlet pipe 133 is connected to the hydrogen exhaust pipe 15. The raw material inlet pipe 131 discharges a glycine solution, and the raw material addition branch pipe 132 discharges a formaldehyde solution. After the two are mixed, the flow rate will decrease significantly when they enter the pre-reaction coarse pipe 13. The pre-reaction coarse pipe 13 forms a vortex and carries out the pre-reaction. Because the pre-reaction coarse pipe 13 is thick and long, the mixed liquid stays in it for an average of more than 15 minutes to achieve the pre-reaction. The catalyst is slowly discharged and mixed with the solution. Due to the flow of the liquid, the catalyst is evenly mixed in the solution and enters the plunger-type high-pressure pump 12.

[0042] The raw material liquid, which is mixed in the raw material inlet pipe 131 and the raw material addition branch pipe 132, flows into the pre-reaction coarse pipe 13 at a pressure of 0.11-0.12 MPa. The raw material liquid, which is mixed in the raw material inlet pipe 131 and the raw material addition branch pipe 132, can only flow into the raw material outlet pipe 133 15-20 minutes after entering the pre-reaction coarse pipe 13.

[0043] The pressure inside the pre-reaction tube 13 should not be too high, otherwise the catalyst will not be able to fall. It is advisable to control it at 1.1-1.2 times the atmospheric pressure (i.e. 0.11-0.12 MPa).

[0044] The catalyst addition tank 11 includes a tank body 111, a conical bottom 112, and a pressurized tank cover. The bottom of the tank body 111 is provided with a conical bottom 112, which is connected to the catalyst addition pipe 14 through a connecting pipe. The pressurized tank cover is provided with a pressurized air inlet pipe, a pressurized air outlet pipe, and a feeding pipe. The pressurized air inlet pipe and the pressurized air outlet pipe ventilate and pressurize the catalyst addition tank 11 (ventilation can ensure the catalyst is dry and protected by inert gas, so that its activity is not affected). A micro-vibration motor is provided on the outer wall of the conical bottom 112.

[0045] Since the total length of the connecting pipe and catalyst addition pipe 14 is 1.5-2.0 meters, and the dry inert gas flowing through the tank 111 creates an environment with a pressure higher than atmospheric pressure, the liquid fluctuates within the connecting pipe and catalyst addition pipe 14. However, the inner diameter of the connecting pipe and catalyst addition pipe 14 is 8-12 mm (this can be appropriately increased depending on the actual flow rate of the reaction liquid). Furthermore, the inner diameter of the palladium-carbon catalyst particles is only 0.3-0.6 mm. Combined with the vibration, the fine particles slowly sink to the end of the pre-reaction coarse pipe 13. They are quickly carried into the raw material outlet pipe 133. Additionally, hydrogen enters the raw material outlet pipe 133 from the hydrogen inlet pipe 15, further turbulenting and mixing the liquid. Finally, the liquid is drawn in by the plunger-type high-pressure pump 12 and forced into the high-pressure microchannel reaction pipeline assembly 2.

[0046] The high-pressure microchannel reaction pipeline assembly 2 includes a booster pipe 21, a U-shaped connecting pipe 22, and an injection pipe 23. The outlet port of the plunger-type high-pressure pump 12 is connected to one end of the first booster pipe 21 through a connecting long pipe. The booster pipe 21 and the U-shaped connecting pipe 22 are sequentially and alternately connected to form multiple sections of bent pipe. The booster pipe 21 and the U-shaped connecting pipe 22 are placed in the same horizontal plane. The outlet end of the last booster pipe 21 is connected to the injection pipe 23. The injection pipe 23 includes a thick pipe section and a thin pipe section. The inner diameter of the thick pipe section is equal to the inner diameter of the U-shaped connecting pipe 22. The inner diameter of the thick pipe section is 3-5 times the inner diameter of the thin pipe section. The inner diameter of the booster pipe 21 is 3-5 times the inner diameter of the U-shaped connecting pipe 22. Both the booster pipe 21 and the U-shaped connecting pipe 22 are covered with heating jackets. The temperature inside the booster pipe 21 and the U-shaped connecting pipe 22 is 80-100℃, and the pressure inside the booster pipe 21 is 0.6-0.9MPa.

[0047] like Figure 2 , 3 5. The booster pipe 21 is thicker than the U-shaped connecting pipe 22 and the thicker section of the injection pipe 23. Furthermore, since a large amount of hydrogen is added, it cannot completely dissolve in the reaction solution. Bubbles flow within the booster pipe 21 and the U-shaped connecting pipe 22, which will... Figure 5As shown, the gas accumulates above the upper half of the pressurization pipe 21, while the liquid flows below. When too much gas accumulates, it will flow in the U-shaped connecting pipe 22 (but mostly liquid). Due to the reaction in the pipe, the gas and solution are mixed, and the pressure does not need to reach the 10-15 atmospheres required in the tank; 6-8 atmospheres are sufficient. Moreover, the reaction efficiency is higher, with the highest efficiency in the early stage of the reaction in the tank (the raw material concentration is high, and the efficiency will decrease significantly in the latter half). Therefore, this application improves the reaction efficiency by controlling the discharge from the injection pipe 23 after only 1.5-2.0 hours of reaction, and the reaction conversion rate can reach 60-70%. Since the subsequent reaction conversion takes a long time, this application does not increase the reaction time but instead filters the catalyst and recovers the product to enter the initial position for re-reaction to improve the reaction efficiency, so that the reaction efficiency remains at a high rate.

[0048] The injection connector 23 includes a thick section and a thin section. The thin section reduces the outflow velocity of the liquid, ensuring that the liquid does not flow out rapidly after the pressurization pipe 21 is pressurized by the plunger-type high-pressure pump 12, thus ensuring that high pressure can be achieved.

[0049] The catalyst recovery assembly 3 includes an inner filter ball 32 and an outer cover ball 31. The inner filter ball 32 has uniformly distributed filter pores. One side of the inner filter ball 32 is provided with a liquid injection pipe 321 and the bottom is provided with a downward-facing catalyst discharge pipe 322. The outer cover ball 31 is sleeved on the inner filter ball 32 and the two are concentric. The end of the thin tube section of the injection pipe 23 is connected to the liquid injection pipe 321. The catalyst discharge pipe 322 extends from the outer cover ball 31 to the outside. A solenoid valve is provided inside the catalyst discharge pipe 322. The outer cover ball 31 is provided with a filter liquid supply pipe 311.

[0050] After the reaction liquid flows into the inner filter ball 32, since the catalyst particles are 0.3-0.6 mm and the filter pores can be set to be less than 0.1 mm, but the sum of the cross-sections of all filter pores is 5-8 times the inner diameter of the thin tube section, it is necessary to ensure that the pressure will be significantly reduced after the liquid enters the inner filter ball 32, so as to ensure the liquid flow. In addition, some of them can block the filter pores for a short time. Therefore, it is necessary to ensure the flow efficiency.

[0051] Once a certain amount of catalyst has accumulated, the solenoid valve inside catalyst drain pipe 322 is briefly opened. Due to the relatively large diameter of the catalyst drain pipe 322, the catalyst particles can be discharged smoothly. The solenoid valve is then immediately closed. The catalyst may require subsequent cleaning and drying for reuse. After the reaction liquid is free of catalyst, it enters hydrogen volatilization channel 4 for subsequent processes.

[0052] The hydrogen evaporation channel 4 includes a first box body 41 and a first box cover 42, and the formaldehyde evaporation and concentration channel 5 includes a second box body 51 and a second box cover 52. The right side of the first box cover 42 is provided with a first suction tube 421, and the right side of the second box cover 52 is provided with a second suction tube 521. The first box 41 and the second box 51 have the same structure. The second box 51 is provided with an overflow trough 511 that sinks down in stages. All the overflow troughs 511 in front are provided with an overflow port 512 on the right side. The second box 51 is provided with an inlet pipe 53 on the left side near the top wall and an outlet pipe 54 on the right side near the bottom.

[0053] Because the first container 41 and the first lid 42 are sealed, the filtrate supply pipe 311 will draw liquid into the first container 41 during the outward discharge of liquid. As the liquid flows within the first container 41, hydrogen gas will rapidly exit the reaction liquid due to the pressure drop and be drawn away by the first suction pipe 421 until the liquid reaches the tail end of the first container 41.

[0054] The temperature inside the first box 41 is 0-5℃, and the gas pressure inside the hydrogen evaporation channel 4 is 0.08-0.09MPa; The temperature inside the second box 51 is 55-60℃, and the gas pressure inside the formaldehyde volatilization and concentration channel 5 is 0.07-0.08MPa.

[0055] The pressure in the second box 51 must be less than the pressure inside the first box 41 to prevent liquid backflow when the drain pipe of the first box 41 is opened.

[0056] The glycine crystallization channel 6 includes a heating jacket 65, a liquid inlet box 62, multiple crystallization precipitation cylinders 63 that are progressively lowered, a purification liquid box 64, a stirring mounting cover 61, and multiple stirring devices 612. The crystallization precipitation cylinder 63 is provided with a circular stirring tank 631 and a settling tank 632. The circular stirring tank 631 and the settling tank 632 are connected at the bottom and the bottom of the connected channel is inclined 6321. The bottom of the circular stirring tank 631 is connected to a downwardly extending conical crystallization tank 633. The bottom of the conical crystallization tank 633 is provided with a suction and crystal discharge tube. The right side wall of the circular stirring tank 631 is provided with an overflow channel 634. The left top wall of the settling tank 632 is provided with a square slot. Multiple crystallization and precipitation cylinders 63 arranged in stages ensure that the liquid flows slowly downwards, overflowing one by one from the crystallization and precipitation cylinders 63.

[0057] like Figure 6 and 8As shown, the liquid first flows into the inlet box 62. Hydrochloric acid needs to be added dropwise into the inlet box 62 to mix with the reaction liquid, adjusting the pH value to 5.0-5.5, preferably around 5.2. The ratio of the amount of liquid discharged into the inlet box 62 to the amount of hydrochloric acid added each time is matched. Then, they flow together into the settling tank 632 of the first crystallization precipitator 63 for dilution, ensuring that the newly flowing liquid does not affect the pH value of the crystallization precipitator 63 (or has a small impact). The liquid flows downward from the settling tank 632 to the bottom of the circular stirring tank 631. Due to the low temperature environment, crystals will slide down from the inclined bottom 6321 and settle in the circular stirring tank 631. The stirring process is conducive to crystallization, and the crystals will settle and accumulate in the conical crystallization tank 633. Since the crystallization rate in the multiple crystallization precipitators 63 will be different, the time interval between the opening and closing of the suction and discharge pipes at the bottom of each conical crystallization tank 633 will be different. After all the liquid has crystallized in the last crystallization precipitator 63, it overflows into the purification liquid box 64. A large amount of liquid can accumulate in the purification liquid box 64 to ensure the continuous delivery of sarcosine solution to complete the neutralization reaction.

[0058] The liquid inlet box 62 is provided with a drain connector on the right side, and the drain connector is locked in the square slot of the first crystallization precipitator 63. The overflow channel 634 on the right side of the crystallization precipitator 63 is locked in the square slot of the next crystallization precipitator in turn. The overflow channel 634 on the right side of the last crystallization precipitator 63 is locked on the top left wall of the purification liquid box 64. The sarcosine drain pipe is provided on the right side wall of the purification liquid box 64 near the bottom. The last overflow tank 511 in the second box 51 has a large storage capacity, which can discharge a certain amount of liquid at a time and then stop the discharge. After being discharged into the inlet box 62, hydrochloric acid is dripped in. When the liquid is discharged into the inlet box 62, the discharge speed will match the downward dripping speed of the acid regulating drip tube 611 to effectively regulate the pH.

[0059] The stirring cover 61 is sealed on the top of the heating sleeve 65. The heating sleeve 65 is sealed outside the liquid inlet box 62, multiple crystallization precipitating cylinders 63 and purification liquid box 64 in successive stages. The stirring cover 61 located directly above the liquid inlet box 62 is provided with an acid adjustment drip tube 611. The stirring cover 61 is provided with a stirring device 612 corresponding to each crystallization precipitating cylinder 63. The temperature inside the crystallization precipitator 63 is 0-5℃.

[0060] During crystallization, the temperature of the liquid decreases as it flows from the inlet box 62 into the crystallization sedimentation cylinder 63. During this process, crystals precipitate and sink. The precipitation is slow and requires stirring to create a micro-vortex state in the liquid, allowing the solution in the circular stirring tank 631 to crystallize better.

[0061] The sarcosine neutralization reaction pipeline 7 includes a neutralization reaction thick pipe 71, a neutralization inlet pipe 72, and a reaction outlet pipe 73. The pH value of the mixed liquid in the neutralization reaction thick pipe 71 is between 8.5 and 9.0. An alkali solution inlet pipe 721 is connected to the middle of the neutralization inlet pipe 72. The alkali solution discharged into the alkali solution inlet pipe 721 is 30% sodium hydroxide. The raw material liquid, which is mixed in the neutralization inlet pipe 72 and the alkali inlet pipe 721, can flow into the reaction outlet pipe 73 after 25-30 minutes in the neutralization reaction coarse pipe 71.

[0062] When the cryogenic liquid is discharged from the purification liquid box 64 (the temperature can be increased at this location after crystallization, with the temperature at 20-30℃), it is pumped into the neutralization inlet pipe 72 by a micro-pump. Then, the corresponding proportion of alkali solution is added at the inlet of the alkali solution inlet pipe 721. The solution then quickly enters the neutralization reaction coarse pipe 71 for rapid mixing and neutralization. At this point, the pH of the reaction solution is 8.5-9.0. The solution then flows into the concentration tank 8, where negative pressure helps to draw the reaction solution in.

[0063] The tank structures of the concentration tank 8, the first crystallization tank 9, the remelting tank 801, and the second crystallization tank 802 are the same; The concentration tank 8, the first crystallization tank 9, and the second crystallization tank 802 are all provided with thin liquid inlet pipes on the left side near the top side wall, and the remelting tank 801 is provided with coarse liquid inlet pipes on the left side near the top side wall. The bottom of the first crystallization tank 9 and the second crystallization tank 802 are both equipped with coarse crystal discharge tubes, and the bottom of the concentration tank and the remelting tank are both equipped with fine liquid discharge tubes. The fine drain pipe of the concentration tank 8 is connected to the fine inlet pipe of the first crystallization tank 9, the coarse drain pipe of the first crystallization tank 9 is connected to the coarse inlet pipe of the remelting tank 801, and the fine drain pipe of the remelting tank 801 is connected to the fine inlet pipe of the second crystallization tank 802. The first crystallization tank 9 and the second crystallization tank 802 are provided with an external crystallization liquid discharge pipe 92 at the middle position on the right side.

[0064] The top of the concentration tank 8, the first crystallization tank 9, the remelting tank 801, and the second crystallization tank 802 are all provided with tank covers 93 of the same structure. The tank cover 93 is provided with an adjusting air inlet pipe 931, an adjusting air outlet pipe 933, and a stirring rack. The adjusting air inlet pipe 931 is provided with an adjusting liquid addition pipe 932. The stirring rack is equipped with a second stirring device that is inserted into the tank.

[0065] like Figure 9The liquid is rapidly mixed upon entering the concentration tank 8. The tank 8's cap (the caps of the four tanks are essentially the same) provides ventilation and drainage. The air inlet pipe 931 and outlet pipe 933 are adjusted to ventilate the tank and remove air. Then, the solenoid valve in the inlet pipe 931 of the concentration tank 8 is closed, and the liquid addition pipe 932 slowly drips hydrochloric acid or sulfuric acid, ensuring the pH of the neutralized liquid is between 7.5 and 8.0. The liquid is then concentrated by reduced pressure heating and distillation within the concentration tank 8 at 60-70℃ (this can be fine-tuned). The pressure is below atmospheric pressure, between 0.6 and 0.8 atmospheres. At this pressure, water boils at approximately 70℃, accelerating evaporation and concentrating the reaction liquid. However, to prevent over-concentration, the thin drain pipe at the bottom of the concentration tank 8 is periodically activated to drain a certain amount of liquid into the first crystallization tank 9, then closed before resuming the crystallization process.

[0066] Because the temperature inside the first crystallization tank 9 is relatively low (0-5℃), which is conducive to crystallization, the upper liquid will contain a small amount of sodium sarcosinate. However, there is no rush to drain the liquid out. The regulating vent pipe 933 at the top of the first crystallization tank 9 is used to release pressure, ensuring smooth drainage each time. The negative pressure inside the first crystallization tank 9 is lower than that in the concentration tank 8. When the liquid in the first crystallization tank 9 reaches more than 2 / 3, the drain pipe 92 of the first crystallization tank 9 is opened (equipped with a micro pump to drain outwards) to drain the liquid outwards. This continues until no more liquid can be drained (the liquid in the first crystallization tank 9 reaches 1 / 2), at which point the solenoid valve and the micro pump are closed.

[0067] Depending on the crystallization time period, after crystallization in the first crystallization tank 9 for 1 hour (1 hour is an example, depending on the actual setting), open the coarse crystal discharge tube at the bottom of the first crystallization tank 9. A greater negative pressure needs to be generated in the remelting tank 801 to draw the crystals and mixed liquids that have settled at the bottom of the first crystallization tank 9 into the remelting tank 801. Close the solenoid valve in the coarse crystal discharge tube in time, and then start to discharge water and a small amount of ethanol (enough for re-dissolution) into the remelting tank 801. The temperature is 50-60℃ for re-dissolution. After dissolution, the liquid is discharged into the second crystallization tank 802 multiple times for multiple recrystallizations. The crystallization conditions are the same as those in the first crystallization tank 9 to achieve the purification and crystallization effect. The upper liquid is discharged from the external crystallization liquid discharge pipe 92 on one side of the second crystallization tank 802.

[0068] The liquid discharged from the external discharge pipe 92 of the first crystallization tank 9 and the second crystallization tank 802 can be concentrated and recrystallized again to improve the recovery rate.

[0069] In the description of this specification, references to terms such as "an embodiment," "example," "specific example," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the invention. In this specification, illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples.

[0070] The preferred embodiments of the present invention disclosed above are merely illustrative of the invention. These preferred embodiments do not exhaustively describe all details, nor do they limit the invention to the specific implementations described. Clearly, many modifications and variations can be made based on the content of this specification. This specification selects and specifically describes these embodiments to better explain the principles and practical applications of the invention, thereby enabling those skilled in the art to better understand and utilize the invention. The invention is limited only by the claims and their full scope and equivalents.

Claims

1. An apparatus for the continuous flow synthesis of sodium sarcosinate in microchannels, characterized by: The glycine methylation reaction channel unit, catalyst recovery assembly (3), sarcosine crystallization purification channel unit, sarcosine neutralization reaction pipeline (7) and sarcosine sodium concentrated crystallization connected tank unit are included. The glycine methylation reaction channel unit includes a raw material mixing pre-reaction tube (1), a catalyst adding tank (11), a plunger type high-pressure pump (12) and a high-pressure micro-channel reaction pipeline combination (2). The raw material mixing pre-reaction tube (1) is provided with a catalyst adding tank (11) at the pre-reaction end section. A hydrogen discharge pipe (15) is arranged on the output pipeline of the raw material mixing pre-reaction tube (1). The plunger type high-pressure pump (12) pressurizes the mixed pre-reaction raw material into the high-pressure micro-channel reaction pipeline combination (2). The gas-liquid mixture after the reaction of the high-pressure micro-channel reaction pipeline combination (2) is discharged into the catalyst recovery assembly (3) to recover the catalyst. The sarcosine crystallization purification channel unit includes a hydrogen volatilization channel (4), a formaldehyde volatilization and concentration channel (5) and a glycine crystallization channel (6). The liquid after the catalyst recovery assembly (3) recovers the catalyst flows into the hydrogen volatilization channel (4) to perform pressure reduction volatilization recovery. The liquid in the hydrogen volatilization channel (4) flows into the formaldehyde volatilization and concentration channel (5) to perform pressure reduction distillation volatilization of formaldehyde and water vapor. The liquid in the formaldehyde volatilization and concentration channel (5) flows into the glycine crystallization channel (6) to perform crystallization and purification of the sarcosine solution. The liquid after the crystallization in the glycine crystallization channel (6) flows into the sarcosine neutralization reaction pipeline (7). An alkali solution is introduced into the liquid inlet end position of the sarcosine neutralization reaction pipeline (7) to perform neutralization reaction. The sarcosine sodium concentrated crystallization connected tank unit includes a concentration tank (8), a first crystallization tank (9), a resolvent tank (801) and a second crystallization tank (802). The liquid after the reaction of the sarcosine neutralization reaction pipeline (7) flows into the concentration tank (8) to perform pressure reduction concentration. Then, the liquid is discharged into the first crystallization tank (9) to perform the first low-temperature pressure reduction crystallization. The crystallization at the bottom of the first crystallization tank (9) is pumped into the resolvent tank (801) to be dissolved. Then, the liquid is discharged into the second crystallization tank (802) to perform the second low-temperature pressure reduction crystallization to obtain the sarcosine sodium crystalline body.

2. The device for the microchannel continuous flow synthesis of sodium sarcosinate according to claim 1, characterized in that, The raw material mixing pre-reaction tube (1) includes a pre-reaction rough tube (13), a raw material inlet pipe (131), a catalyst adding pipe (14), a hydrogen discharge pipe (15) and a raw material outlet pipe (133). The two ends of the pre-reaction rough tube (13) are respectively connected with the raw material inlet pipe (131) and the raw material outlet pipe (133). The raw material inlet pipe (131) is provided with a raw material adding branch pipe (132) at the middle position. The pre-reaction rough tube (13) is provided with a catalyst adding pipe (14) vertically upward at the top near the raw material outlet pipe position. The bottom discharge port of the catalyst adding tank (11) is connected with the catalyst adding pipe (14). The hydrogen discharge pipe (15) is connected with the middle section of the raw material outlet pipe (133). The pressure of the raw material liquid mixed by the raw material inlet pipe (131) and the raw material adding branch pipe (132) in the pre-reaction rough pipe (13) is 0.11-0.12 MPa, and the raw material liquid mixed by the raw material inlet pipe (131) and the raw material adding branch pipe (132) can flow into the raw material outlet pipe (133) after 15-20 minutes.

3. The device for the microchannel continuous flow synthesis of sodium sarcosinate according to claim 2, characterized by the fact that, The catalyst adding tank (11) comprises a tank body (111), a conical bottom (112) and a pressurized tank cover, the bottom of the tank body (111) is provided with the conical bottom (112), the conical bottom (112) is connected with the catalyst adding pipe (14) through a butt joint pipe, the pressurized tank cover is provided with a pressurized inlet pipe, a pressurized outlet pipe and a feeding pipe, the pressurized inlet pipe and the pressurized outlet pipe are used for air exchange and pressurization of the catalyst adding tank (11), and the outer wall of the conical bottom (112) is provided with a micro-vibration motor.

4. The device for the microchannel continuous flow synthesis of sodium sarcosinate according to claim 1, characterized by the fact that, The high-pressure micro-channel reaction pipeline combination (2) comprises a pressurized pipe (21), a U-shaped connecting pipe (22) and an injection connecting pipe (23), the liquid outlet port of the plunger type high-pressure pump (12) is connected with one end of the first pressurized pipe (21) through a connecting long pipe, the pressurized pipe (21) and the U-shaped connecting pipe (22) are sequentially and alternately connected to form a plurality of bending pipes, the pressurized pipe (21) and the U-shaped connecting pipe (22) are arranged in the same horizontal plane, the liquid outlet end of the last pressurized pipe (21) is connected with the injection connecting pipe (23), the injection connecting pipe (23) comprises a rough pipe section and a thin pipe section, the inner diameter of the rough pipe section is equal to the inner diameter of the U-shaped connecting pipe (22), the inner diameter of the rough pipe section is 3-5 times the inner diameter of the thin pipe section, and the inner diameter of the pressurized pipe (21) is 3-5 times the inner diameter of the U-shaped connecting pipe (22). The pressurized pipe (21) and the U-shaped connecting pipe (22) are wrapped with heating jackets, the temperature in the pressurized pipe (21) and the U-shaped connecting pipe (22) is 80-100℃, and the pressure in the pressurized pipe (21) is 0.6-0.9 MPa.

5. The apparatus for the microchannel continuous flow synthesis of sodium sarcosinate according to claim 4, characterized in that, The catalyst recovery assembly (3) comprises a filter inner ball (32) and an outer cover ball (31), the filter inner ball (32) is uniformly provided with filter fine holes, one side of the filter inner ball (32) is provided with a liquid injection pipe (321), and the bottom is provided with a downward catalyst discharge pipe (322), the outer cover ball (31) is sleeved outside the filter inner ball (32) and is concentric with the filter inner ball (32), the end of the thin pipe section of the injection connecting pipe (23) is connected with the liquid injection pipe (321), the catalyst discharge pipe (322) penetrates through the outer cover ball (31) to the outside, the catalyst discharge pipe (322) is provided with an electromagnetic valve, and the outer cover ball (31) is provided with a filter liquid supply pipe (311).

6. The device for the microchannel continuous flow synthesis of sodium sarcosinate according to claim 1, characterized by the fact that, The hydrogen gas volatilization channel (4) comprises a first box body (41) and a first box cover (42), the formaldehyde volatilization and concentration channel (5) comprises a second box body (51) and a second box cover (52), the right end of the first box cover (42) is provided with a first suction pipe (421), and the right end of the second box cover (52) is provided with a second suction pipe (521). The first box (41) and the second box (51) are of the same structure, the second box (51) is provided with overflow grooves (511) sinking step by step, overflow ports (512) are arranged on the right side of all the overflow grooves (511) in front, and liquid inlet pipes (53) are arranged on the left side of the second box (51) close to the top wall, liquid outlet pipes (54) are arranged on the right side of the second box (51) close to the bottom.

7. The device for the microchannel continuous flow synthesis of sodium sarcosinate according to claim 6, characterized by the fact that, The temperature in the first box (41) is 0-5 DEG C, and the gas pressure in the hydrogen gas volatilization channel (4) is 0.08-0.09 MPa. The temperature in the second box (51) is 55-60 DEG C, and the gas pressure in the formaldehyde volatilization and concentration channel (5) is 0.07-0.08 MPa.

8. The device for microchannel continuous flow synthesis of sodium sarcosinate according to claim 1, characterized by that, The glycine crystallization channel (6) comprises a heating jacket (65), a liquid inlet box (62), a plurality of crystallization precipitation cylinders (63) sinking step by step, a purification liquid box (64), a stirring installation cover (61) and a plurality of stirring devices (612). The crystallization precipitation cylinder (63) is provided with a circular stirring groove (631) and a sinking groove (632), the circular stirring groove (631) and the sinking groove (632) are communicated at the bottom position and the communicated channel bottom is an inclined bottom (6321), the circular stirring groove (631) is connected with a downwardly extending conical crystallization groove (633) at the bottom, the conical crystallization groove (633) is provided with a suction crystal discharge pipe at the bottom, the right side wall of the circular stirring groove (631) is provided with an overflow channel (634), and the left side top wall of the sinking groove (632) is provided with a square bayonet. The liquid outlet joint is arranged on the right side of the liquid inlet box (62) and is clamped in the square bayonet of the first crystallization precipitation cylinder (63), the overflow channel (634) on the right side of the crystallization precipitation cylinder (63) is clamped in the square bayonet of the next crystallization precipitation cylinder in sequence, the overflow channel (634) on the right side of the last crystallization precipitation cylinder (63) is clamped on the left side top wall of the purification liquid box (64), and the right side wall of the purification liquid box (64) is provided with a sarcosine liquid outlet pipe close to the bottom position. The stirring installation cover (61) is sealed on the top of the heating jacket (65), the heating jacket (65) is sealed on the outside of the liquid inlet box (62), the plurality of crystallization precipitation cylinders (63) sinking step by step and the purification liquid box (64), the acid adjusting liquid drop pipe (611) is arranged on the stirring installation cover (61) above the liquid inlet box (62), and one stirring device (612) is arranged on the stirring installation cover (61) corresponding to each crystallization precipitation cylinder (63). The temperature in the crystallization precipitation cylinder (63) is 0-5 DEG C.

9. The device for microchannel continuous flow synthesis of sodium sarcosinate according to claim 1, characterized by that, The sarcosine neutralization reaction pipeline (7) comprises a neutralization reaction rough pipe (71), a neutralization liquid inlet pipe (72) and a reaction liquid outlet pipe (73), the pH value of the mixed liquid in the neutralization reaction rough pipe (71) is 8.5-9.0, the alkali liquid adding pipe (721) is connected to the neutralization liquid inlet pipe (72) at the middle position, and the alkali liquid discharged from the alkali liquid adding pipe (721) is 30% sodium hydroxide. The raw material liquid mixed by the neutralization inlet pipe (72) and the lye inlet pipe (721) flows into the neutralization reaction rough pipe (71) and then flows into the reaction outlet pipe (73) after 25-30 minutes.

10. The device for the microchannel continuous flow synthesis of sodium sarcosinate according to claim 1, characterized by the fact that, The tank body structures of the concentration tank (8), the first crystallization tank (9), the resolvent tank (801) and the second crystallization tank (802) are the same; The left side of the concentration tank (8), the first crystallization tank (9) and the second crystallization tank (802) near the top side wall is respectively provided with a fine inlet pipe, and the left side of the resolvent tank (801) near the top side wall is respectively provided with a coarse inlet pipe; The bottom of the first crystallization tank (9) and the second crystallization tank (802) is respectively provided with a coarse outlet pipe, and the bottom of the concentration tank and the resolvent tank is respectively provided with a fine outlet pipe; The fine outlet pipe of the concentration tank (8) is connected with the fine inlet pipe of the first crystallization tank (9), the coarse outlet pipe of the first crystallization tank (9) is connected with the coarse inlet pipe of the resolvent tank (801), and the fine outlet pipe of the resolvent tank (801) is connected with the fine inlet pipe of the second crystallization tank (802); The right side of the first crystallization tank (9) and the second crystallization tank (802) is respectively provided with an external outlet pipe (92) at the middle position; The top of the concentration tank (8), the first crystallization tank (9), the resolvent tank (801) and the second crystallization tank (802) is respectively provided with a tank cover (93) with the same structure, the tank cover (93) is provided with an adjusting inlet pipe (931), an adjusting outlet pipe (933) and a stirring frame, the adjusting inlet pipe (931) is provided with an adjusting liquid inlet pipe (932), and the stirring frame is installed with a second stirring device inserted into the tank.

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