Gluconate production reaction system

Abstract

The utility model relates to the technical field of gluconate production equipment, and provides a gluconate production reaction system which comprises a reaction kettle, a jet aerator, a heating device and a temperature sensor, the reaction kettle is provided with a reaction chamber, a feeding port and a discharging port, and a mounting port is arranged above the reaction kettle. The reaction kettle is provided with a cooling interlayer, a cooling medium inlet and a cooling medium outlet; the jet aerator is provided with a mixing chamber, a gas outlet, a liquid outlet and a gas-liquid mixed outlet, the jet aerator is provided with a gas flow channel and a gas inlet, and the jet aerator is provided with a liquid flow channel and a liquid inlet; the mixing chamber comprises a first equal-diameter channel, a reducing channel, a second equal-diameter channel and an expanding channel which are communicated in sequence, and the gas outlet and the liquid outlet are both communicated with the first equal-diameter channel; an outlet of the expanding channel is used as a gas-liquid mixing outlet; the heating device is arranged in the reaction kettle; and the temperature sensor is arranged in the reaction kettle. The gluconate production reaction system provided by the utility model has higher production efficiency.

Description

Technical Field

[0001] The utility model relates to the technical field of gluconate production equipment, in particular to a gluconate production reaction system, such as zinc gluconate, calcium gluconate, sodium gluconate and other related production. Background Art

[0002] Gluconates are a widely used class of compounds, playing a vital role in a variety of industries, including food, healthcare, construction, and textile printing and dyeing. Zinc gluconate, for example, has broad application prospects in medicine, food, feed, and cosmetics. As a common adjuvant drug, zinc gluconate plays a vital role in clinical treatment. Due to its unique pharmacological effects, it is often used to treat the common cold, relieve ulcer symptoms, and improve taste and appetite. It can also promote growth and development, enhance immune system function, and provide a variety of health and therapeutic benefits.

[0003] Traditional gluconate production methods vary, primarily including conventional chemical methods, catalytic oxidation, electrolytic oxidation, fermentation, and dual-enzyme methods. Each of these methods offers unique advantages, meeting the diverse needs for gluconate products across various sectors. With the continuous advancement of technology and increasing market demand, gluconate production processes are constantly being optimized and improved to enhance product quality and efficiency, meeting a wider range of application requirements.

[0004] Among them, the dual-enzyme method is currently the most mainstream industrial production method. It is to place the prepared 30% glucose solution in a reactor, set the enzyme reaction temperature to 35°C, add 10% oxides such as zinc oxide, calcium oxide suspension during the reaction, adjust and control the pH to around 6.0, and add catalase and glucose oxidase to the reactor in turn.

[0005] Existing gluconate production systems typically introduce air directly into the reactor to provide the oxygen required for the oxidation process. A stirring paddle is then used to mix and react the various materials in the reactor. This system presents the following issues during production: The stirring process slows mass transfer from the gas phase to the liquid phase, limiting the reaction and reducing production efficiency. Utility Model Content

[0006] The utility model aims to provide a gluconate production reaction system to solve the problem of low production efficiency caused by the prior art gluconate production reaction system using a stirring method to achieve gas-liquid mass transfer.

[0007] To achieve the above-mentioned purpose, according to the first aspect of the present utility model, a gluconate production reaction system is provided, comprising: a reactor, the reactor comprising a reaction chamber and a feeding port and a discharging port connected to the reaction chamber, a mounting port being further provided above the reactor, the reactor further comprising a cooling interlayer for accommodating a cooling medium and a cooling medium inlet and a cooling medium outlet connected to the cooling interlayer; a jet aerator, the jet aerator being installed at the mounting port, the jet aerator comprising a mixing chamber and a gas outlet, a liquid outlet and a gas-liquid mixed outlet connected to the mixing chamber, the jet aerator further comprising a gas flow channel and a gas inlet connected to the gas outlet, and the jet aerator further comprising a liquid flow channel and a liquid inlet connected to the liquid outlet; the mixing chamber comprising a first constant diameter channel, a reducing diameter channel, a second constant diameter channel and an expanding diameter channel connected in sequence, the gas outlet and the liquid outlet both being connected to the first constant diameter channel; the outlet of the expanding diameter channel serving as a gas-liquid mixed outlet; a heating device, the heating device being arranged in the reactor; a temperature sensor, the detection end of the temperature sensor being arranged in the reactor for detecting the temperature in the reaction chamber, the temperature sensor being signal-connected to the heating device.

[0008] Furthermore, the diameter of the first equal-diameter channel: the radius of the second equal-diameter channel: the length of the second equal-diameter channel: the length of the expanded channel: the diameter of the liquid outlet: the distance from the liquid outlet to the inlet end of the second equal-diameter channel = 1: (0.18~0.26): (0.37~0.43): (0.55~0.58): (1.07~1.14): (1.144~1.292).

[0009] Furthermore, the jet aerator includes a liquid nozzle, a gas pipe section and a mixing pipe section, the liquid nozzle is connected to the mixing pipe section, and the gas pipe section is connected to the mixing pipe section; the liquid nozzle includes a connected equal-diameter section and a contraction section, the outlet end of the contraction section serves as the liquid outlet, the inlet end of the equal-diameter section serves as the liquid inlet, the interior of the equal-diameter section and the interior of the contraction section are connected and together form a liquid flow channel; the gas pipe section is an equal-diameter pipe section, the interior of the equal-diameter pipe section forms a gas flow channel, the inlet end of the equal-diameter pipe section serves as the gas inlet, and the outlet end of the equal-diameter pipe section serves as the gas outlet; the mixing pipe section includes a first equal-diameter pipe section, a contraction pipe section, a second equal-diameter pipe section and a diffusion pipe section connected in sequence, the interior of the first equal-diameter pipe section forms a first equal-diameter channel, the interior of the contraction pipe section forms a contraction channel, the interior of the second equal-diameter pipe section forms a second equal-diameter channel, and the interior of the diffusion pipe section forms an expansion channel; the contraction section and part of the equal-diameter section of the liquid nozzle extend from top to bottom into the first equal-diameter pipe section, the gas pipe section is connected to the side wall of the first equal-diameter pipe section, and the gas outlet is lower than the liquid outlet.

[0010] Furthermore, the contraction angle of the contraction section is 10°; and the divergence angle of the expansion channel is 16°.

[0011] Furthermore, the liquid inlet is used to introduce glucose solution; the gas inlet is used to introduce oxygen; at least one feeding port is provided on the side wall of the reactor, the feeding port is used to add glucose oxidase or catalase or zinc oxide or calcium oxide or sodium hydroxide, and a feeding valve is provided at the feeding port; at least one exhaust port is provided on the top wall of the reactor, the exhaust port is used to adjust the pressure in the reactor, and an exhaust valve is provided at the exhaust port.

[0012] Furthermore, a first feeding port and a second feeding port are respectively provided on the left and right sides of the side wall of the reactor, a first feeding valve is provided at the first feeding port, and a second feeding valve is provided at the second feeding port; a first exhaust port and a second exhaust port are provided at the top of the reactor, located on the right side of the installation port, the height of the first exhaust port is higher than the height of the second exhaust port, a first exhaust valve is provided at the first exhaust port, and a second exhaust valve is provided at the second exhaust port.

[0013] Furthermore, the gluconate production reaction system also includes: a reactor support frame, the reactor is arranged on the reactor support frame, a discharge port is provided at the bottom of the reactor, and a discharge valve is provided at the discharge port; a gas-liquid separator, the gas-liquid separator includes a shell, a separation chamber is formed in the shell, a gas-liquid two-phase inlet and a gas discharge port connected to the separation chamber are provided at the top of the shell, a gas-liquid two-phase inlet is provided with a gas-liquid inlet valve; an exhaust valve is provided at the gas discharge port; a liquid discharge port is provided at the bottom of the shell and is connected to the separation chamber, a discharge pipe is provided at the liquid discharge port, and a first liquid discharge valve and a second liquid discharge valve are provided on the discharge pipe in sequence; a mist catcher, the mist catcher is provided at In the separation chamber; a liquid inlet pipe, one end of the liquid inlet pipe extends from the liquid inlet into the liquid flow channel and is connected to the liquid flow channel, and the other end of the liquid inlet pipe serves as a liquid phase feed port; a return pipe, one end of the return pipe is connected to the discharge pipe, and the other end of the return pipe is connected to the liquid inlet pipe; the connection point between the return pipe and the discharge pipe is located between the first liquid discharge valve and the second liquid discharge valve; the connection point between the return pipe and the liquid inlet pipe is located between the liquid phase feed port and the liquid inlet; the gas-liquid inlet valve and the discharge valve are connected by a delivery pipe, and a first circulation pump is provided on the delivery pipe; a second circulation pump, the second circulation pump is arranged on the liquid inlet pipe, and is located between the connection point between the return pipe and the liquid inlet and the liquid inlet.

[0014] Furthermore, the top of the shell is arranged in an arc shape, the height of the gas-liquid two-phase inlet is higher than the height of the gas exhaust port, and two gas exhaust ports of different heights are provided on the top of the shell, which are respectively located on the left and right sides of the gas-liquid two-phase inlet; a third exhaust valve is provided at the gas exhaust port on the left, and a fourth exhaust valve is provided at the gas exhaust port on the right; the mist collector is arranged close to the top of the shell relative to the bottom of the shell.

[0015] Furthermore, the heating device includes an electromagnetic induction heating coil and a controller. The electromagnetic induction heating coil is attached to the inner wall of the reactor and is located below the feeding port. The controller is connected to the electromagnetic induction heating coil signal. The controller is connected to the temperature sensor signal.

[0016] Furthermore, the reactor includes an inner tube and an outer tube; the outer tube includes a connected outer tube side wall and an outer tube bottom wall, and the inner tube includes a connected inner tube bottom wall and an inner tube side wall; the outer tube bottom wall is located on the outside of the inner tube bottom wall, the height of the outer tube side wall is lower than the height of the inner tube side wall, and the outer tube side wall is located on the outside of part of the inner tube side wall to form a cooling interlayer in the lower half of the reactor; a cooling medium inlet is provided on the outer tube side wall at the top and a cooling medium outlet is provided at the bottom.

[0017] Using the technical solution of the present utility model, liquid enters the first equal-diameter channel of the mixing chamber through the liquid inlet, liquid flow channel, and liquid outlet. Gas enters the first equal-diameter channel of the mixing chamber through the gas inlet, gas flow channel, and gas outlet. Under the action of gravity, the gas and liquid enter the second equal-diameter channel through the reduced-diameter channel. In the second equal-diameter channel, they fully and efficiently dissolve to achieve an aeration effect. Then, the gas and liquid enter the expanded-diameter channel. The liquid violently shears the gas to form an emulsification. When fine bubbles are formed, oxygen absorption is correspondingly improved, which is conducive to increasing the mass transfer efficiency and rate of the liquid and gas, thereby improving production efficiency. The gluconate production reaction system provided by the present application has higher production efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] The above and other objects, features and advantages of the exemplary embodiments of the present invention will become readily understood by reading the detailed description below with reference to the accompanying drawings. In the accompanying drawings, several embodiments of the present invention are shown in an exemplary and non-limiting manner, and the same or corresponding reference numerals represent the same or corresponding parts, wherein:

[0019] Figure 1 A schematic diagram of the overall structure of a gluconate production reaction system provided in an optional embodiment of the present invention;

[0020] Figure 2 for Figure 1 Schematic diagram of the structure of the jet aerator;

[0021] Figure 3 for Figure 1 Schematic diagram of the structure of the gas-liquid two-phase vertical separator;

[0022] Figure 4 for Figure 1 Schematic diagram of the structure of the reactor;

[0023] Figure 5 This is the proportion of liquid phase in the jet aerator structure;

[0024] Description of Figure Numbers:

[0025] 1. Reactor; 101. Reaction chamber; 102. Feeding port; 103. Discharge port; 104. Mounting port; 11. Reactor support frame; 12. Second feeding valve; 13. First feeding valve; 14. First exhaust valve; 15. Second exhaust valve; 16. Discharge valve; 111. Inner tube; 112. Outer tube; 115. Outer tube bottom wall; 116. Outer tube side wall; 113. Inner tube bottom wall; 114. Inner tube side wall; 2. Jet aerator; 201. Mixing chamber; 202. Gas outlet; 203. Liquid outlet; 204. Gas-liquid mixed outlet; 205. Gas flow channel; 206. Liquid flow channel; 207. Liquid inlet; 21. Liquid feed port; 22. Gas inlet; 221. Gas pipe section; 222. Mixing pipe section; 23. Expansion channel; 24, second equal-diameter channel; 25, liquid nozzle; 251, equal-diameter section; 252, contraction section; 26, contraction channel; 27, first equal-diameter channel; 3, heating device; 31, controller; 32, electromagnetic induction heating coil; 4, cooling interlayer; 42, cooling medium inlet; 41, cooling medium outlet; 51, first circulation pump; 52, second circulation pump; 7, gas-liquid separator; 701, shell; 702, separation chamber; 703, gas-liquid two-phase inlet; 704, gas outlet; 71, second liquid discharge valve; 72, gas-liquid inlet valve; 73, first liquid discharge valve; 74, third exhaust valve; 75, fourth exhaust valve; 76, liquid inlet pipe; 77, return pipe; 78, discharge pipe; 8, mist collector; 17, delivery pipe. DETAILED DESCRIPTION

[0026] The exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. Although exemplary embodiments of the present disclosure are shown in the accompanying drawings, it should be understood that the present disclosure can be implemented in various forms and should not be limited by the embodiments described herein. On the contrary, these embodiments are provided to enable a more thorough understanding of the present disclosure and to fully convey the scope of the present disclosure to those skilled in the art. Unless otherwise specified, the technical means used in the examples are conventional means well known to those skilled in the art.

[0027] like Figures 1 to 4As shown, the present application provides a gluconate production reaction system, comprising: a reactor 1, the reactor 1 having a reaction chamber 101 and a feeding port 102 and a discharging port 103 connected to the reaction chamber 101, a mounting port 104 being further provided on the top of the reactor 1, the reactor 1 also having a cooling interlayer 4 for accommodating a cooling medium and a cooling medium inlet 42 and a cooling medium outlet 41 connected to the cooling interlayer 4; a jet aerator 2, the jet aerator 2 being installed at the mounting port 104, the jet aerator 2 having a mixing chamber 201 and a gas outlet 202, a liquid outlet 203 and a gas-liquid mixed outlet 204 connected to the mixing chamber 201, the jet aerator 2 also having a gas outlet 202 and a liquid outlet 203 connected to the gas outlet 204. 02 is connected to the gas flow channel 205 and the gas inlet 22, the jet aerator 2 also has a liquid flow channel 206 and a liquid inlet 207 connected to the liquid outlet 203; the mixing chamber 201 includes a first equal-diameter channel 27, a reducing channel 26, a second equal-diameter channel 24 and an expanding channel 23 connected in sequence, the gas outlet 202 and the liquid outlet 203 are both connected to the first equal-diameter channel 27; the outlet of the expanding channel 23 serves as a gas-liquid mixing outlet 204; a heating device 3, the heating device 3 is arranged in the reactor 1; a temperature sensor, the detection end of the temperature sensor is arranged in the reactor 1, for detecting the temperature in the reaction chamber 101, and the temperature sensor is connected to the heating device 3 signal.

[0028] In this way, the liquid enters the first equal-diameter channel 27 of the mixing chamber 201 through the liquid inlet 207, the liquid flow channel 206 and the liquid outlet 203, and the gas enters the first equal-diameter channel 27 of the mixing chamber 201 through the gas inlet 22, the gas flow channel 205 and the gas outlet 202. Under the action of gravity, the gas and liquid enter the second equal-diameter channel 24 through the reducing channel 26, and are fully and efficiently dissolved in the second equal-diameter channel 24 to achieve the aeration effect, and then enter the expanding channel 23. The liquid shears the gas violently to form an emulsification. When fine bubbles are reached, the absorption of oxygen is correspondingly improved, which is conducive to increasing the mass transfer efficiency and rate of the liquid and gas, thereby improving production efficiency. The gas-liquid mixture passing through the jet aerator 2 enters the reaction chamber 101 of the reactor, and then reacts with the material input through the feed port 102, is heated by the heating device 3, and the feedback value obtained by the temperature sensor is used to control the temperature in the reaction chamber 101 to avoid the activity failure of the enzyme and complete the efficient production of gluconate. The gluconate production reaction system provided by the present application has higher production efficiency.

[0029] Alternatively, the diameter of the first constant-diameter channel 27: the radius of the second constant-diameter channel 24: the length of the second constant-diameter channel 24: the length of the expanded-diameter channel 23: the diameter of the liquid outlet 203: the distance from the liquid outlet 203 to the inlet of the second constant-diameter channel 24 = 1: 0.18-0.26: 0.37-0.43: 0.55-0.58: 1.07-1.14: 1.144-1.292. Thus, the present application optimizes the parameters of the jet aerator, making it more suitable for the production of gluconate and further improving the production efficiency of gluconate.

[0030] Alternatively, as Figure 1 、 Figure 2 and Figure 4 As shown, the jet aerator 2 includes a liquid nozzle 25, a gas pipe section 221 and a mixing pipe section 222. The liquid nozzle 25 is connected to the mixing pipe section 222, and the gas pipe section 221 is connected to the mixing pipe section 222. The liquid nozzle 25 includes a connected equal-diameter section 251 and a contraction section 252. The outlet end of the contraction section 252 serves as the liquid outlet 203, and the inlet end of the equal-diameter section 251 serves as the liquid inlet 207. The interior of the equal-diameter section 251 and the interior of the contraction section 252 are connected and together form a liquid flow channel 206. The gas pipe section 221 is an equal-diameter section, and the interior of the equal-diameter section forms a gas flow channel 205. The inlet end of the equal-diameter section serves as The jet aerator 222 comprises a first, reduced diameter pipe section, a second, and a diffuser section, each connected in sequence. The first, reduced diameter pipe section forms a first, reduced diameter channel 27, the reduced diameter pipe section forms a reduced diameter channel 26, the second, reduced diameter pipe section forms a second, reduced diameter channel 24, and the diffuser section forms an expanded diameter channel 23. The liquid nozzle's contracting section 252 and a portion of the constant diameter section 251 extend from top to bottom into the first, constant diameter pipe section. The gas pipe section 221 is connected to the sidewall of the first, constant diameter pipe section, and the gas outlet 202 is lower than the liquid outlet 203. Thus, the jet aerator 2 has a rational structure and low manufacturing cost, facilitating the industrialized, mass-produced production of gluconate.

[0031] Preferably, the contraction angle of the contraction section 252 is 10°, and the diffusion angle of the expansion channel 23 is 16°. In this way, the gas-liquid mixing effect is better.

[0032] Optionally, the liquid inlet 207 is used to introduce glucose solution; the gas inlet 22 is used to introduce oxygen; at least one feeding port 102 is provided on the side wall of the reactor 1, and is used to introduce glucose oxidase, catalase, zinc oxide, calcium oxide, or sodium hydroxide, and is provided with a feeding valve; the top wall of the reactor 1 is provided with at least one exhaust port, and is used to regulate the pressure within the reactor 1, and is provided with an exhaust valve. Thus, the present application directly introduces oxygen through the gas inlet 22. Compared with the solution of introducing air into the reactor in the related art, the present application provides a dedicated oxygen supply device, which can ensure the reaction proceeds fully.

[0033] Alternatively, as Figure 1 and Figure 4 As shown, a first feeding port and a second feeding port are respectively provided on the left and right sides of the side wall of the reactor 1. A first feeding valve 13 is provided at the first feeding port, and a second feeding valve 12 is provided at the second feeding port. A first exhaust port and a second exhaust port are provided at the top of the reactor 1, located to the right of the mounting port 104. The first exhaust port is higher than the second exhaust port. A first exhaust valve 14 is provided at the first exhaust port, and a second exhaust valve 15 is provided at the second exhaust port. This allows different materials to be fed into the first and second feeding ports, further improving production efficiency. Increasing the number of exhaust ports and exhaust valves can also improve exhaust efficiency, thereby further increasing production efficiency.

[0034] Alternatively, as Figure 1As shown, the gluconate production reaction system also includes: a reactor support frame 11, the reactor 1 is arranged on the reactor support frame 11, the bottom of the reactor 1 is provided with a discharge port 103, and the discharge port 103 is provided with a discharge valve 16; a gas-liquid separator 7, the gas-liquid separator 7 includes a shell 701, a separation chamber 702 is formed in the shell 701, the top of the shell 701 is provided with a gas-liquid two-phase inlet 703 and a gas discharge port 704 connected to the separation chamber 702, the gas-liquid two-phase inlet 703 is provided with a gas-liquid inlet valve 72; the gas discharge port 704 is provided with an exhaust valve; the bottom of the shell 701 is provided with a liquid discharge port connected to the separation chamber 702, the liquid discharge port is provided with a discharge pipe 78, and the discharge pipe 78 is provided with a first liquid discharge valve 73 and a second liquid discharge valve 71 in sequence; a mist catcher 8, the mist catcher 8 is arranged in the separation chamber 702 73 and the second liquid discharge valve 71; the connection point between the return pipe 77 and the liquid inlet pipe 76 is located between the liquid phase feed port 21 and the liquid inlet 207; the gas-liquid inlet valve 72 and the discharge valve 16 are connected by a delivery pipe 17, and a first circulation pump 51 is provided on the delivery pipe 17; a second circulation pump 52 is provided on the liquid inlet pipe 76, and is located between the connection point between the return pipe 77 and the liquid inlet pipe 76 and the liquid inlet 207. In this way, when the discharge valve 16 and the gas-liquid inlet valve 72 are opened, the gas-liquid mixture after the reaction in the reactor enters the gas-liquid separator 7 through the delivery pipe 17 under the action of the first circulation pump 51, passes through the mist catcher 8, and the reacted gas is discharged from the gas outlet 704. The liquid flows downward into the bottom of the separation chamber 702 under the action of gravity. After sufficient reaction, the second drain valve 71 can be controlled to open and the first drain valve 73 can be controlled to open to collect the product after the reaction; when the reaction is not sufficient, the second drain valve 71 can be controlled to close and the first drain valve 73 can be controlled to open. The liquid enters the jet aerator under the action of the second circulation pump 52 for secondary aeration, and then enters the reaction chamber 101 of the reactor 1 to continue reacting until the reaction is sufficient. The gluconate production reaction system provided by the present application cancels the stirring mechanism to avoid the stirring mechanism affecting the activity of the enzyme, utilizes the circulation of the liquid to make it fully react, ensures the activity of the enzyme, and is conducive to improving the production efficiency and production quality of gluconate.

[0035] Alternatively, as Figure 1As shown, the top of the housing 701 is curved, with the gas-liquid two-phase inlet 703 at a higher height than the gas outlet 704. Two gas outlets 704 at different heights are provided at the top of the housing 701, one on the left and one on the right of the gas-liquid two-phase inlet 703. A third exhaust valve 74 is provided at the left gas outlet 704, and a fourth exhaust valve 75 is provided at the right gas outlet 704. The mist collector 8 is positioned closer to the top of the housing 701 than to the bottom. Increasing the number of gas outlets 704 helps improve the efficiency of exhausting the reacted gas.

[0036] Alternatively, as Figure 1 and Figure 4 As shown, heating device 3 includes an electromagnetic induction heating coil 32 and a controller 31. Electromagnetic induction heating coil 32 is attached to the inner wall of reactor 1, below feeding port 102. Controller 31 is signal-connected to electromagnetic induction heating coil 32, which is also signal-connected to a temperature sensor. Thus, the controller controls electromagnetic induction heating coil 32 based on the real-time temperature detected by the temperature sensor, achieving precise temperature control within reaction chamber 101 of reactor 1 to avoid affecting enzyme activity.

[0037] Alternatively, as Figure 1 and Figure 4 As shown, the reactor 1 comprises an inner tube 111 and an outer tube 112. The outer tube 112 comprises a connected outer tube sidewall 116 and an outer tube bottom wall 115. The inner tube 111 comprises a connected inner tube bottom wall 113 and an inner tube sidewall 114. The outer tube bottom wall 115 is located outside the inner tube bottom wall 113. The height of the outer tube sidewall 116 is lower than that of the inner tube sidewall 114. The outer tube sidewall 116 is located outside a portion of the inner tube sidewall 114, forming a cooling layer 4 in the lower half of the reactor 1. The outer tube sidewall 116 is provided with a cooling medium inlet 42 located at the top and a cooling medium outlet 41 located at the bottom. In this way, the temperature within the reaction chamber 101 is reduced by the cooling medium, preventing the heat generated during the reaction from increasing the temperature within the reactor 1 and affecting the activity of the enzyme. At the same time, the formation of the cooling layer 4 in the lower half of the reactor 1 can further reduce the manufacturing cost of the gluconate production reaction system.

[0038] In current reactors, air is passed through the reactor to provide the oxygen required for the oxidation process. A stirring paddle is used to mix all the materials in the reactor. Cooling water and steam are then introduced through the reactor jacket to control the temperature. The reaction ends when the reducing sugar concentration in the reaction solution drops below 0.5. This presents the following problems: The reactor currently lacks a device for controlling the reaction temperature. For example, the optimal temperature for the enzymes required for this production process is around 35°C. However, current reactors lack temperature control, making it prone to temperature increases. When the temperature reaches 80°C, the enzymes become completely inactive. The temperature distribution in the reactor is uneven, and localized high temperatures can affect enzyme activity. For example, when using a heating and stirring method for heat transfer, the steam temperature exceeds 100°C, resulting in localized high-temperature zones within the reactor. Enzymes typically react at a temperature of around 35°C. Above 80°C, the enzymes completely lose activity and do not recover even after cooling. The localized high temperatures caused by steam heating can cause some enzymes to become inactive and ineffective. The reactor also lacks oxygen flow. Because this reaction is an oxidation reaction, it requires a large amount of oxygen to fully proceed. The initial glucose concentration in the reaction material is low, and the amount of water required for evaporation in the subsequent evaporation stage is large. The agitator has low mass transfer efficiency. Considering that the reaction is a gas-liquid two-phase flow, the agitation method results in a slow mass transfer rate from the gas phase to the aqueous phase, thereby limiting the reaction and reducing industrial efficiency. Traditional agitators can cause enzyme damage. For example, the stirring blade speed can reach 450-500 rpm, and this high-speed stirring action can damage enzyme activity.

[0039] like Figure 1 and Figure 2As shown, the present application provides a gluconate production reaction system, including a reactor 1. The top of the reactor 1 is provided with a first exhaust valve 14 and a second exhaust valve 15, and a second feeding valve 12 and a first feeding valve 13 are respectively provided on the left and right sides of the reactor, and a discharge valve 16 is provided at the lower end. The jet aerator comprises a liquid phase feed port 21, a liquid nozzle 25, a gas inlet 22, a first equal-diameter channel 27, a second equal-diameter channel 24, and an expanding channel 23. The liquid phase feed port 21 and the liquid nozzle 25 are connected to each other, the gas inlet 22 is connected to the first equal-diameter channel 27 at the lower end of the liquid nozzle 25, the second equal-diameter channel 24 is placed upright in the reactor, and its upper end is connected to the lower end of the first equal-diameter channel 27, and the upper end of the expanding channel 23 is connected to the lower end of the second equal-diameter channel 24. An electromagnetic induction heating coil 32 is provided in the reaction chamber 101, and the electromagnetic induction heating coil 32 is close to the inner wall of the reaction chamber 101. A temperature sensor is also provided in the reaction chamber 101, which can monitor the temperature changes in the reaction chamber 101 of the reactor 1 in real time, and the target temperature can be set and controlled by the controller 31. One end of the delivery pipe 17 in the loop is connected to the discharge valve 16, and is transported to the other end through the first circulation pump 51 and connected to the gas-liquid inlet valve 72 of the gas-liquid separator 7. After entering the gas-liquid separator 7 and passing through the mist catcher 8, the reacted gas can flow out from the third exhaust valve 74 and the fourth exhaust valve 75 of the gas-liquid separator, and the remaining liquid naturally flows downward under the influence of gravity. The product can flow out from the second liquid discharge valve 71 of the gas-liquid separator; the unreacted liquid can flow through the liquid inlet pipe 76 by the second circulation pump 52; and then flow back into the jet aerator 2 to complete a cycle.

[0040] Alternatively, for a specific chemical reaction process under specific temperature and pressure conditions, the size and structure of the jet aerator has a significant impact on the mass transfer and oxygenation effect of the reaction, and may even reduce the production efficiency of the factory. Figure 2As shown, the present application has made a special design for the size of the jet aerator, only for the gluconate chemical reaction process; the size segments include the opening diameter of the first equal-diameter channel 27: the radius of the second equal-diameter channel 24: the length of the second equal-diameter channel 24: the length of the expanded channel 23: the outlet diameter of the liquid nozzle 25: the distance from the liquid nozzle 25 to the second equal-diameter channel 24, the ratio is 1: (0.18-0.26): (0.37-0.43): (0.55-0.58): (1.07-1.14): (1.144-1.292); in the reaction preparation stage of gluconate preparation, glucose is dissolved in water to form a glucose solution. When the initial glucose solution concentration is 30%-34%, the ratio of glucose to water volume is 1: (3-3.57), which is a suitable glucose solution concentration. The initial glucose solution concentration is very critical. When the glucose solution concentration is too high, the entire reaction cycle will be prolonged and the activity of the enzyme will be affected. Liquid enters the liquid-phase feed inlet 21 and flows into the liquid nozzle 25, generating a high-speed jet. This jet flows into the first constant-diameter channel 27. At this point, gas enters the gas inlet 22 of the jet aerator 2, ejecting the fluid at high speed, causing the gas to be drawn into the second constant-diameter channel 24. In the first half of the second constant-diameter channel 24, the liquid flows continuously, with surface contact between the liquid and the gas, which limits oxygen transmission. As the jet gradually diffuses, when the diffusion diameter equals the diameter of the second constant-diameter channel 24, a so-called mixing microwave is formed. During this process, the liquid violently shears the gas, causing it to form an emulsified state with a diameter less than 100 microns, thus forming a gas-liquid mixed two-phase flow. Upon entering the expanding channel 23, the increased cross-sectional area causes the velocity head to transform into a pressure head, further emulsifying the gas. As is well known, the surface area of the same amount of gas formed into a large bubble is much smaller than that of a dispersed, multiplying bubble. Therefore, the emulsification effect significantly increases the gas-liquid contact area, thereby enhancing the transfer of gas to liquid. The liquid flowing out of the expansion channel 23 has completed the process of gas to liquid mass transfer, thereby achieving the effect of aeration. The entire jet aerator 2 is installed in a vertical direction so that the liquid jets downward. Such a setting not only utilizes its inherent energy, but also is fully affected by the action of gravity. Therefore, water will not be retained in the first equal-diameter channel 27 and the second equal-diameter channel 24, thereby reducing the resistance of the system and improving the hydraulic conditions. In addition, the flow of fluid under this setting is relatively favorable, which also helps to reduce resistance losses. Moreover, when the equipment stops working, the entire jet aerator 2 will not accumulate water, which is conducive to subsequent inspection and maintenance operations.Specifically, after the liquid flows into the reaction chamber 101 of the reactor, in order to ensure that the optimal activity temperature of the enzyme is at 35°C, the electromagnetic induction heating coil 32 is started, and the temperature in the reaction chamber 101 and the temperature required by the reaction materials are precisely adjusted by the controller 31 externally mounted on the outer surface of the reaction chamber 101 of the reactor 1, so that the electromagnetic induction heating coil 32 heats the liquid. At this time, the jet aerator 2 continues to work, so that the liquid can circulate and the materials are mixed more evenly, thereby avoiding damage to the activity of the enzyme caused by high-speed stirring. Furthermore, as the reaction proceeds, if the reaction is to be terminated, the controller 31 is used to control the electromagnetic induction heating coil 32 to rapidly heat up. When the temperature reaches 90°C or above, the enzyme completely loses its activity, thereby terminating the reaction. In specific implementation, combined with. Figure 4 The cooling reflux system includes a cooling interlayer 4, a cooling medium inlet 42, and a cooling medium outlet 41. The cooling medium inlet 42 is located at the end of the cooling interlayer 4 of the reactor 1 away from the ground and is connected to one end of the water outlet of the chiller. The cooling medium outlet 41 is located at the end of the cooling interlayer 4 of the reactor 1 close to the ground and is connected to one end of the return water inlet of the chiller. Cooling water enters the cooling medium inlet 42 from the water outlet of the chiller, flows into the cooling interlayer 4, flows out from the cooling medium outlet 41, and enters the return water inlet of the chiller, forming a cycle. Since the temperature required for this reaction is not high, the cooling water is cooled between the outer cylinder 112 and the inner cylinder 111 of the reaction chamber 101 to achieve a cooling treatment for the material. After the chiller is started, the external cooling water flows into the cooling medium inlet 42 and then into the cooling medium outlet 41. The cooling medium outlet 41 is opened to allow the cooling water inside to flow back into the chiller. Further explanation: the chiller can be a split-cooling chiller, a steam-cooling chiller, or other types of chillers. Specifically, after the reaction is fully completed in the reaction chamber 101, the discharge valve 16 is opened, and the product after the reaction flows through the discharge valve 16 into the delivery pipe 17 and then into the gas-liquid inlet valve 72 of the gas-liquid separator 7. Figure 3As shown, after the product enters the gas-liquid separator 7, its design principle utilizes the different densities of gas and liquid in a gravitational field to achieve gas-liquid separation. Due to the different densities of the gas and liquid, the liquid is subject to a greater gravity force. Therefore, when flowing with the gas, the liquid will experience a downward velocity. Meanwhile, the gas continues to flow in its original direction. As a result, the liquid and gas within the gas-liquid separator 7 tend to separate. The liquid moves downward in the direction of gravity and settles on the walls, eventually flowing out through the second drain valve 71 of the gas-liquid separator 7, while the gas is discharged through the third and fourth exhaust valves 74 and 75. This principle effectively separates the gas and liquid, ensuring the proper operation of the separator. Upon completion of the gas-liquid separation, the product can be obtained from the second drain valve 71 at the liquid phase outlet of the gas-liquid separator. After the gas is discharged from the third and fourth exhaust valves 74 and 75 of the gas-liquid separator, the unreacted liquid flows out through the first drain valve 73 and is transported to the liquid inlet pipe 76 by the second circulation pump 52, thereby being directed to the jet aerator 2. This design allows the liquid to be recycled a second time and to undergo a secondary aeration process in the jet aerator 2. This process helps to increase the contact area between the dissolved gas and water, improve the gas mass transfer efficiency, and thus achieve more adequate gas utilization and treatment effects. The application method of the gluconate production reaction system includes: a liquid-phase and gas-phase mass transfer step, opening the liquid phase feed port 21 and the gas inlet 22 of the jet aerator 2, the liquid enters the jet aerator 2, passes through the first equal-diameter channel 27, the second equal-diameter channel 24, and the expanded diameter channel 23, at which time the liquid and gas have completed mass transfer and flow into the reaction chamber 101. Combined Figure 4 , material heating step, control the controller 31 of the heating device 3, turn on the electromagnetic induction heating coil 32 of the heating device 3, and adjust the temperature to 35°C. Material cooling step, control the controller 31 of the heating device 3, turn off the electromagnetic induction heating coil 32 of the heating device 3, and turn on the cooling reflux system. Furthermore, in the logistics heating step: the temperature change of the material in the reaction chamber 101 can be detected by the temperature sensor, and the electromagnetic induction heating coil 32 can be automatically turned on and off after the target temperature set by the controller. In the reaction feeding step, materials such as zinc oxide, calcium oxide, sodium hydroxide and other solid powder materials can be added to the reaction chamber 101 of the reactor through the second feeding valve 12 and the first feeding valve 13 for further reaction. As Figure 4 In the gas-liquid separation step, the discharge valve 16 at the bottom of the reactor 1 is opened to allow the material to flow into the gas-liquid separator 7 to separate the product from the gas. In the liquid circulation step, the gas and liquid are separated by passing through the mist catcher 8. The liquid flows out of the first discharge valve 73 and is returned to the jet aerator 2, completing the cycle; the next stage of aeration treatment is then carried out.

[0041] The specific embodiment of the present application provides a gluconate production reaction system, which relates to the technical field of gluconate production equipment, such as zinc gluconate, calcium gluconate, sodium gluconate and other related production. The gluconate production reaction system provided by this specific embodiment includes a reactor 1, a jet aerator 2, a gas-liquid separator 7 (two-phase gas-liquid vertical separator), a heating device 3 (electromagnetic heating coil and controller), a reactor support frame, and the reactor 1 has a cooling interlayer 4 (for forming a cooling water system) and a reactor insulation layer. Among them, by designing a loop reaction, increasing the reaction interface of the water and gas two phases, increasing the mass transfer efficiency and rate of the reactants glucose solution and oxygen, thereby improving the conversion efficiency of gluconate, and by optimizing the parameters of the jet aerator 2, the core component of the design device loop, the overall reaction efficiency is further improved.

[0042] The jet aerator 2 has two inlets: a liquid inlet 207 and a gas inlet 22. The jet aerator 2 is strategically positioned vertically within the reactor 1, occupying 3 / 7 of the reactor 1's total height. Between the inner and outer cylinders 111, 112 of the reactor 1, lies the cooling layer 4, which forms a cooling water system with the chiller. Cooling water flows into the reactor 1 from the side away from the ground and out from the side near the ground, lowering the temperature within the reaction chamber 101. After the material has fully reacted within the reaction chamber 101, the discharge valve 16 at the bottom of the reactor 1 can be opened. The product can then enter the vertical two-phase gas-liquid separation device, namely the gas-liquid separator 7, through a delivery pipe 17. The gas-liquid separator 7 is equipped with a gas-liquid two-phase inlet 703, a circulation port, and a discharge port. When the reaction product enters the gas-liquid two-phase inlet 703, it is separated into two phases due to the difference in gravity and density between the gas and liquid. The reacted gas will be separated from the liquid, and the waste gas will be discharged from the outlet at the upper end of the separator; the separated product liquid will flow out from the second liquid discharge valve 71 and the discharge port, and the unreacted liquid will enter the return pipe 77 through the circulation port and the first liquid discharge valve 73, and will flow back into the jet aerator 2 by the second circulation pump 52, achieving the effect of secondary aeration.

[0043] The jet aerator has two inlets, one for gas 22 and the other for liquid 207. Liquid flows from the liquid inlet 207 through the liquid nozzle 25 to form a high-speed jet. The high-speed jet creates a negative pressure in the first equal-diameter channel 27, allowing gas to be drawn into it. The gas and liquid fully and efficiently dissolve in the second equal-diameter channel 24, thereby achieving an aeration effect. As the jet gradually diffuses, after the diffusion diameter equals the throat diameter, a mixing shock wave is generated, and the liquid is violently sheared to form an emulsification of the gas. After the gas and liquid become an emulsified two-phase flow, they enter the expanding channel 23. Due to the increase in the flow cross-section, the gas is further emulsified. When fine bubbles are formed, the oxygen absorption will be improved. During the reaction process, the outlet diameter of the liquid nozzle 25 in the jet aerator is controlled to be 50 mm, the inlet diameter of the liquid nozzle 25 is set to 100 mm, the contraction angle of the contraction section of the liquid nozzle is 10°, the length of the cylindrical transition section is eliminated, the flow rate into the liquid nozzle inlet is set to 1 m / s, and the pressure is 6 MPa, so that the liquid fluid velocity at the liquid nozzle of the jet aerator can be controlled to be 4.86 m / s-5.62 m / s; and in the initial stage of the reaction, a glucose solution is introduced through the liquid inlet, and the glucose and water are mixed in a volume ratio of 1:3.57. At this time, the glucose solution concentration is 30%, which is the optimal initial concentration; the glucose solution flows into the jet aerator 2. In an optional specific embodiment, the liquid nozzle 25 is placed at a distance of 323 mm from the inlet end of the second equal-diameter channel 24; the optimal diameter of the first equal-diameter channel 27 of the jet aerator 2: the radius of the second equal-diameter channel 24: the length of the second equal-diameter channel 24: the length of the expansion channel 23: the outlet diameter of the contraction section 252 (i.e., the diameter of the liquid outlet 203): the distance from the liquid outlet 203 to the inlet end of the second equal-diameter channel 24 = 1:0.2:0.4:0.56:1.12:1.292, and the angle of the expansion channel 23 is 16°; at this time, the diameter of the gas inlet 22 is 120 mm, the air flow rate is 2.5 m / s, and the pressure at the gas inlet 22 is 7 MPa; as the reaction proceeds, 1% glucose oxidase and 0.8% catalase are added to the reactor successively, thereby completing the initial stage reaction.

[0044] Since the reaction involved in this device is an exothermic reaction, heat is generated during the reaction, causing the temperature in the reactor to rise, which in turn affects the activity of the enzyme or other effects. At this point, there should be a cooling system, which is equipped with a cooling medium inlet 42 and a cooling medium outlet 41; the cooling medium inlet 42 is set on the left side of the reactor 1, away from the ground end, and is located between the outer cylinder 112 and the inner cylinder 111 of the reactor 1; the cooling medium outlet 41 is set on the right side of the reactor 1, close to the ground end, and is located between the outer cylinder 112 and the inner cylinder 111 of the reactor 1; cooling water is introduced into the cooling medium inlet 42, and after circulation, it flows out of the cooling medium outlet 41 and enters the chiller (this device is not involved in this patent) for cooling, and finally returns to the cooling medium inlet 42 to complete the cycle; the discharge valve 16 at the bottom of the reactor 1 is opened, and the completely reacted material flows to the gas-liquid separator 7 through the conveying pipe 17. The reactor support frame 11 is located on both sides of the discharge valve 16 to ensure the stability of the reactor 1. The first feeding valve 13 and the second feeding valve 12 are located on the left and right sides of the inner cylinder of the reactor away from the ground. The first feeding valve 13 and the second feeding valve 12 are used to feed reactants such as zinc oxide, calcium oxide, sodium hydroxide, etc. Furthermore, the first exhaust valve 14 and the second exhaust valve 15 are located on the right side of the top of the reactor. Opening the first exhaust valve 14 or the second exhaust valve 15 can release the pressure in the reactor cylinder, so that the reaction can proceed under suitable conditions; further, the gas-liquid separator 7, a mist collector 8 is arranged inside the shell 701 of the gas-liquid separator 7; its function is to capture and separate suspended particles or droplets in the liquid. Under its action, the gas and liquid in the reacted material can be separated, and the liquid can flow back into the jet aerator 2 from the circulation port at the bottom of the gas-liquid separator 7 through the return pipe 77 and the liquid inlet pipe 76, and after being ejected by the liquid nozzle 25, the aeration and oxygenation effect is achieved; the outside of the reactor is provided with a thermal insulation material layer, and the inside is provided with a heating device 3 (including an electromagnetic induction heating coil 32 and a controller 31) to heat the material inside the reactor 1.

[0045] Optionally, the temperature sensor and the electromagnetic induction heating coil 32 may be integrated together or provided separately.

[0046] The best embodiments of this application are as follows:

[0047] A glucose solution formed by dissolving glucose in water is added to a 50L reactor 1. Prior to configuration, the glucose solution is prepared at a glucose to water volume ratio of 1:3.57 to form a 30% glucose solution. The total volume of the material in the reactor is approximately 35-40L, and the jet aerator 2 is vertically positioned at 30% ± 2% of the height of the entire reactor 1. After configuration, the glucose solution is flowed into the jet aerator 2 at a speed of 1 m / s and a constant pressure of 6 MPa. After flowing through the liquid nozzle 25, the liquid is directed at a speed of 5.6 m / s. At this point, oxygen is introduced into the jet aerator 2, entering the first constant-diameter channel 27 at a pressure of 7 MPa and a flow rate of 2.5 m / s. Liquid flows from the expansion channel 23 into the reaction chamber 101 of the reactor 1. As the liquid in the reaction chamber 101 increases, the temperature sensor can read the temperature information in the reaction chamber 101 at this time. The temperature target is set to 35°C±1°C by the controller, and the working state of the electromagnetic induction heating coil 32 is controlled by the controller. When the temperature is low, the electromagnetic induction heating coil 32 is controlled to start heating. When the temperature increases, the electromagnetic induction heating coil 32 is controlled to stop heating. When the volume of the material accounts for approximately one-quarter of the total material volume, 1% glucose oxidase is first added to the reactor, and then 0.8% catalase is added thereto. At this time, the reaction will release a large amount of heat, and the cooling system needs to be turned on for cooling treatment to ensure that the temperature in the reaction chamber 101 of the reactor 1 is 35°C±1°C.

[0048] After detailed analysis and calculation, Figure 5 It can be clearly found that for this reaction, the jet aerator 2 designed with the above dimensions has the best aeration effect when the gas and liquid ratios are about 50% each. This can be understood as the bubbles are broken up and evenly distributed in the liquid phase.

[0049] Compared with the current traditional reaction equipment, the gluconate production reaction system provided by the preferred embodiment of the present application can produce obvious effects: through the principle of jet aeration, the glucose solution and oxygen are fully aerated and oxygenated to produce micron-sized bubbles. Thereby, the oxygenation efficiency of the liquid material is improved, the material concentration of the reaction section output is high and the water content is low, and the amount of water required to be evaporated in the subsequent evaporation section is reduced. The cooling system will cool the circulating material to prevent the excessive heat release of the reaction from inactivating the enzyme. The heating device including the electromagnetic induction heating coil heats the material in the reaction chamber 101 to achieve precise temperature control so that the activity of the enzyme in the reaction is not affected. After the reaction is completed, the temperature can be quickly raised to over 100° to completely inactivate the enzyme and complete the inactivation process. The jet aerator 2 ejects high-speed fluid, so that the liquid in the reaction chamber 101 of the reactor can circulate in a directional manner, thereby avoiding the damage caused by high-speed stirring and further improving the activity of the enzyme.

[0050] The above description is merely a specific embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any modifications or substitutions that can be easily conceived by a person skilled in the art within the technical scope disclosed in the present invention should be included within the scope of protection of the present invention. Therefore, the scope of protection of the present invention should be based on the scope of protection of the claims.

[0051] It should be noted that, unless otherwise specified, the technical or scientific terms used in this disclosure should have the ordinary meanings understood by those skilled in the art to which this disclosure pertains. In this disclosure, relational terms such as "first" and "second" are used solely to distinguish one entity or operation from another, and do not necessarily require or imply any actual relationship or order between these entities or operations. Terms such as "connected" and "connected" should be interpreted broadly, meaning, for example, fixedly connected, removably connected, or integrally connected; mechanically connected, electrically connected; directly connected, or indirectly connected through an intermediary. The terms "comprise," "include," or any other variations thereof are intended to encompass non-exclusive inclusion, such that a process, method, article, or apparatus comprising a list of elements includes not only those elements but also other elements not explicitly listed, or elements inherent to such process, method, article, or apparatus. Without further limitation, the phrase "comprises..." does not preclude the presence of additional identical elements in the process, method, article, or apparatus comprising the elements.

Claims

1. A gluconate production reaction system, characterized in that: include: A reactor (1), the reactor (1) comprising a reaction chamber (101) and a feeding port (102) and a discharging port (103) in communication with the reaction chamber (101); a mounting port (104) is further provided above the reactor (1); the reactor (1) further comprising a cooling interlayer (4) for accommodating a cooling medium, and a cooling medium inlet (42) and a cooling medium outlet (41) in communication with the cooling interlayer (4); A jet aerator (2), the jet aerator (2) being installed at the installation port (104), the jet aerator (2) having a mixing chamber (201) and a gas outlet (202), a liquid outlet (203) and a gas-liquid mixed outlet (204) communicating with the mixing chamber (201), the jet aerator (2) also having a gas flow channel (205) and a gas inlet (22) communicating with the gas outlet (202), and the jet aerator (2) also having a liquid flow channel (206) and a liquid inlet (207) in communication with the liquid outlet (203); the mixing chamber (201) comprises a first constant diameter channel (27), a reduced diameter channel (26), a second constant diameter channel (24), and an expanded diameter channel (23) in communication with each other in sequence; the gas outlet (202) and the liquid outlet (203) are both in communication with the first constant diameter channel (27); the outlet of the expanded diameter channel (23) serves as the gas-liquid mixing outlet (204); A heating device (3), the heating device (3) being arranged in the reaction kettle (1); A temperature sensor, wherein a detection end of the temperature sensor is arranged in the reactor (1) and is used to detect the temperature in the reaction chamber (101), and the temperature sensor is connected to the heating device (3) by signal.

2. The gluconate production reaction system according to claim 1, characterized in that: The diameter of the first equal-diameter channel (27): the radius of the second equal-diameter channel (24): the length of the second equal-diameter channel (24): the length of the expanded channel (23): the diameter of the liquid outlet (203): the distance from the liquid outlet (203) to the inlet end of the second equal-diameter channel (24) = 1: (0.18-0.26): (0.37-0.43): (0.55-0.58): (1.07-1.14): (1.144-1.292).

3. The gluconate production reaction system according to claim 1, characterized in that: The jet aerator (2) comprises a liquid nozzle (25), a gas pipe section (221) and a mixing pipe section (222), wherein the liquid nozzle (25) is connected to the mixing pipe section (222), and the gas pipe section (221) is connected to the mixing pipe section (222); The liquid nozzle (25) comprises a connected constant diameter section (251) and a contraction section (252); the outlet end of the contraction section (252) serves as the liquid outlet (203); the inlet end of the constant diameter section (251) serves as the liquid inlet (207); the interior of the constant diameter section (251) and the interior of the contraction section (252) are connected and together form the liquid flow channel (206); The gas pipe section (221) is a pipe section of equal diameter, the interior of the pipe section of equal diameter forms the gas flow channel (205), the inlet end of the pipe section of equal diameter serves as the gas inlet (22), and the outlet end of the pipe section of equal diameter serves as the gas outlet (202); The mixing pipe section (222) comprises a first constant diameter pipe section, a reduced diameter pipe section, a second constant diameter pipe section and a diffuser pipe section connected in sequence, wherein the interior of the first constant diameter pipe section forms the first constant diameter channel (27), the interior of the reduced diameter pipe section forms the reduced diameter channel (26), the interior of the second constant diameter pipe section forms the second constant diameter channel (24), and the interior of the diffuser pipe section forms the expanded diameter channel (23); The contraction section (252) and part of the equal-diameter section (251) of the liquid nozzle extend from top to bottom into the first equal-diameter pipe section, the gas pipe section (221) is connected to the side wall of the first equal-diameter pipe section, and the gas outlet (202) is lower than the liquid outlet (203).

4. The gluconate production reaction system according to claim 3, characterized in that: The contraction angle of the contraction section (252) is 10°; The diffusion angle of the expansion channel (23) is 16°.

5. The gluconate production reaction system according to claim 1, characterized in that: The liquid inlet (207) is used to introduce glucose solution; The gas inlet (22) is used to introduce oxygen; At least one feeding port (102) is provided on the side wall of the reactor (1), and the feeding port (102) is used to feed glucose oxidase or catalase or zinc oxide or calcium oxide or sodium hydroxide, and a feeding valve is provided at the feeding port (102); At least one exhaust port is provided on the top wall of the reactor (1), and the exhaust port is used to adjust the pressure in the reactor (1). An exhaust valve is provided at the exhaust port.

6. The gluconate production reaction system according to claim 5, characterized in that: A first feeding port and a second feeding port are respectively provided on the left and right sides of the side wall of the reactor (1); a first feeding port is provided with a first feeding valve (13), and a second feeding port is provided with a second feeding valve (12); A first exhaust port and a second exhaust port are provided on the top of the reactor (1) on the right side of the installation port (104), wherein the height of the first exhaust port is higher than that of the second exhaust port, a first exhaust valve (14) is provided at the first exhaust port, and a second exhaust valve (15) is provided at the second exhaust port.

7. The gluconate production reaction system according to claim 1, characterized in that: The gluconate production reaction system also includes: A reactor support frame (11), wherein the reactor (1) is arranged on the reactor support frame (11), the bottom of the reactor (1) is provided with the discharge port (103), and the discharge port (103) is provided with a discharge valve (16); A gas-liquid separator (7), comprising a shell (701), a separation chamber (702) formed in the shell (701), a gas-liquid two-phase inlet (703) and a gas outlet (704) in communication with the separation chamber (702) provided at the top of the shell (701), a gas-liquid inlet valve (72) provided at the gas-liquid two-phase inlet (703), and an exhaust valve provided at the gas outlet (704); a liquid outlet in communication with the separation chamber (702) provided at the bottom of the shell (701), a discharge pipe (78) provided at the liquid outlet, and a first liquid discharge valve (73) and a second liquid discharge valve (71) provided on the discharge pipe (78) in sequence; a mist catcher (8), the mist catcher (8) being arranged in the separation chamber (702); a liquid inlet pipe (76), one end of which extends from the liquid inlet (207) into the liquid flow channel (206) and communicates with the liquid flow channel (206), and the other end of which serves as a liquid phase feed port (21); a return pipe (77), one end of the return pipe (77) being connected to the discharge pipe (78), and the other end of the return pipe (77) being connected to the liquid inlet pipe (76); a connection point between the return pipe (77) and the discharge pipe (78) being located between the first liquid discharge valve (73) and the second liquid discharge valve (71); and a connection point between the return pipe (77) and the liquid inlet pipe (76) being located between the liquid phase feed port (21) and the liquid inlet (207); The gas-liquid inlet valve (72) and the discharge valve (16) are connected via a delivery pipe (17), and a first circulation pump (51) is provided on the delivery pipe (17); A second circulation pump (52) is provided on the liquid inlet pipe (76) and is located between the connection point between the return pipe (77) and the liquid inlet pipe (76) and the liquid inlet (207).

8. The gluconate production reaction system according to claim 7, characterized in that: The top of the shell (701) is arranged in an arc shape. The height of the gas-liquid two-phase inlet (703) is higher than the height of the gas outlet (704). Two gas outlets (704) of different heights are provided on the top of the shell (701), which are respectively located on the left and right sides of the gas-liquid two-phase inlet (703). A third exhaust valve (74) is provided at the gas outlet (704) on the left, and a fourth exhaust valve (75) is provided at the gas outlet (704) on the right. The mist catcher (8) is arranged relative to the bottom of the shell (701) and close to the top of the shell (701).

9. The gluconate production reaction system according to claim 1, characterized in that: The heating device (3) comprises an electromagnetic induction heating coil (32) and a controller (31); the electromagnetic induction heating coil (32) is attached to the inner wall of the reactor (1), and the electromagnetic induction heating coil (32) is located below the feeding port (102); the controller (31) is signal-connected to the electromagnetic induction heating coil (32); and the controller (31) is signal-connected to the temperature sensor.

10. The gluconate production reaction system according to claim 1, characterized in that: The reactor (1) comprises an inner cylinder (111) and an outer cylinder (112); the outer cylinder (112) comprises an outer cylinder side wall (116) and an outer cylinder bottom wall (115) connected to each other, and the inner cylinder (111) comprises an inner cylinder bottom wall (113) and an inner cylinder side wall (114) connected to each other; the outer cylinder bottom wall (115) is located outside the inner cylinder bottom wall (113); the height of the outer cylinder side wall (116) is lower than the height of the inner cylinder side wall (114); the outer cylinder side wall (116) is located outside a portion of the inner cylinder side wall (114) to form the cooling interlayer (4) in the lower half of the reactor (1); the outer cylinder side wall (116) is provided with a cooling medium inlet (42) located above and a cooling medium outlet (41) located below.

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