Low-energy-consumption gibberellic acid production device

Abstract

The utility model discloses a gibberellic acid producing device with low energy consumption, which comprises a tank body, a feed port and a discharge port are arranged on the tank body, an inner cavity of the tank body is enclosed by the tank body, the feed port is arranged at the top of the tank body, the discharge port is arranged at the bottom of the tank body, the tank body is further provided with a material supplementing and air passing port, and the material supplementing and air passing port is arranged at the lower part of the tank body. The material supplementing and air passing opening is connected with a header pipe, the header pipe penetrates through the tank body, one part of the header pipe is located in an inner cavity of the tank body, the other part of the header pipe is located outside the inner cavity of the tank body, the end, located outside the inner cavity of the tank body, of the header pipe is communicated with an air inlet pipe and a material supplementing pipe, a material supplementing valve and a material supplementing cup are installed on the material supplementing pipe, and an air inlet valve is installed on the air inlet pipe. An inner cylinder is mounted in the inner cavity of the tank body, an upper opening is formed in the top of the inner cylinder, and a lower opening is formed in the bottom. According to the gibberellic acid production device, high gibberellic acid yield can be obtained without stirring.

Description

Technical Field

[0001] The utility model relates to gibberellic acid production, in particular to a low-energy consumption gibberellic acid production device. Background Art

[0002] Gibberellic acid 3 (GA3) is a plant growth hormone produced by Gibberellin. It plays an important role in regulating plant growth and development and is used in many fields, including agriculture, forestry, and brewing, with significant economic and social benefits. Traditional methods for producing GA3 include plant extraction, chemical synthesis, and microbial fermentation. However, plant-based GA3 extraction yields low yields, generates significant waste, and is costly. Chemical synthesis is also limited by cumbersome process steps and the resulting pollution. With the rapid development of synthetic biology, microbial production of GA3 is gaining increasing attention.

[0003] Currently, GA3 can be produced by a variety of fungi, such as Gibberellin (Fujikuroi), Aspergillus niger, and Fusarium oxysporum. A strain from the same group, Fusarium moniliforme, offers higher yields, but requires solid-state fermentation, making it unsuitable for industrial production. Therefore, Gibberellin (Fujikuroi) is primarily used for industrial production of GA3 due to its high yield and controlled fermentation.

[0004] In recent years, due to its wide application in agriculture and horticulture, the GA3 market has significant potential and market demand. Although the industrial production of GA3 has been achieved using Fusarium fujikura, there are still problems such as low GA3 production level and high cost. The existing GA3 production adopts universal ventilated stirred reactor technology for industrial product production (for example, CN201990659U). In GA3 production, energy consumption (air oxygen supply, steam sterilization, stirring power consumption, circulating water cooling) accounts for 20% to 30% of the total product cost, of which stirring accounts for 20% to 40% of the total energy consumption.

[0005] In the existing ventilated stirred reactor technology (such as CN201990659U), in the fermentation tank production stage of GA3, such as CN108285915A, the seed liquid, culture medium and feed all enter through the feed port, and the feeding process is: the dissolved oxygen rebounds by 20%, and the automatic flow of glucose and salad oil is turned on, glucose (45%) solution: oil (3.2L:1L), sugar and oil are added at the same time, and the dissolved oxygen control point is 20% to 30%.

[0006] Therefore, how to reduce energy consumption without reducing GA3 production has become an urgent problem that the industry needs to solve.

[0007] The above background technology is for facilitating understanding of the present invention and is not a known technology disclosed to the general public before the application of the present invention. Utility Model Content

[0008] In view of the above-mentioned defects, the utility model provides a low-energy consumption gibberellic acid production device, in which a higher gibberellic acid yield can be obtained without stirring in the acid production step.

[0009] The technical solution is: a low-energy consumption gibberellic acid production device, including a tank body, a feed port and a discharge port are provided on the tank body, the tank body forms an inner cavity of the tank body, the feed port is provided at the top of the tank body, and the discharge port is provided at the bottom of the tank body, the tank body is also provided with a feeding and air passage port, the feeding and air passage port are located at the lower part of the tank body, the feeding and air passage port are connected with a main pipe, the main pipe passes through the tank body, wherein a part is located in the inner cavity of the tank body, and the rest is located outside the inner cavity of the tank body, the end of the main pipe located outside the inner cavity of the tank body is connected with an air inlet pipe and a feeding pipe, a feeding valve and a feeding cup are installed on the feeding pipe, an air inlet valve is installed on the air inlet pipe, an inner cylinder is installed in the inner cavity of the tank body, the top of the inner cylinder is provided with an upper opening, the bottom is provided with a lower opening, the inner cylinder The inner cavity of the inner cylinder is surrounded by the main pipe, and the part of the main pipe located in the inner cavity of the tank passes through the inner cylinder and is located in the inner cavity of the inner cylinder. Its end opening is downward and is connected to the distributor. A first pushing unit is provided below the bottom of the distributor, and more than three horizontal distribution pipes are connected to the side wall of the distributor. The more than three horizontal distribution pipes are evenly distributed along the circumference. More than two second pushing units are provided above each horizontal distribution pipe. The first pushing unit is located below the bottom of the inner cylinder, and the second pushing unit is located in the inner cavity of the inner cylinder. The first pushing unit is connected to the distributor through a connecting pipe, and the second pushing unit is connected to the horizontal distribution pipe through a connecting pipe. The pushing inlet of the first pushing unit is at the top, and the pushing outlet is at the bottom. The pushing inlet of the second pushing unit is at the bottom, and the pushing outlet is at the top.

[0010] Furthermore, the feed valve and the air intake valve are both solenoid valves.

[0011] Furthermore, there are eight horizontal distribution pipes, and two second pushing units are installed on each horizontal distribution pipe.

[0012] Furthermore, the main bodies of the first pushing unit and the second pushing unit are both cylinders, one end of the cylinder is connected to the pushing inlet, and the other end is connected to the pushing outlet.

[0013] Furthermore, the push inlet and the push outlet are both conical structures, the small ends of the push inlet and the push outlet are connected to the cylinder, and the large ends are away from the cylinder.

[0014] Furthermore, the diameter of the portion of the connecting pipe located in the push inlet gradually decreases along the gas running direction.

[0015] Furthermore, the pushing outlet of the first pushing unit is adjacent to the discharge port and is located above the discharge port.

[0016] Furthermore, the upper opening is in the shape of an inverted truncated cone. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 It is a schematic diagram of the overall structure of the utility model;

[0018] In the figure: 1. Tank body, 2. Feed port, 3. Discharge port, 4. Feed and air passage, 5. Main pipe, 51. Air inlet pipe, 52. Feed pipe, 53. Feed valve, 54. Feed cup, 55. Air inlet valve, 6. Inner cylinder, 61. Upper opening, 62. Lower opening, 7. Tank cavity, 8. Inner cylinder cavity, 9. Distributor, 10. First pushing unit, 11. Horizontal distribution pipe, 12. Second pushing unit, 13. Connecting pipe. DETAILED DESCRIPTION

[0019] The present invention will be further described below with reference to the accompanying drawings.

[0020] In the description of this utility model, it should be noted that, unless otherwise expressly specified or limited, the terms "mounted," "connected," and "connected" should be understood in a broad sense. For example, they may refer to a fixed connection, an indirect connection via an intermediate medium, internal communication between two components, or an interaction between two components. Those skilled in the art will understand the specific meanings of these terms in this utility model based on specific circumstances.

[0021] In the description of the present invention, it should be understood that the terms "upper," "lower," "front," "back," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like, indicating positions or relationships, are based on the positions or relationships shown in the accompanying drawings and are intended solely to facilitate the description of the present invention and simplify the description. They do not indicate or imply that the devices or components referred to must have a specific orientation, be constructed, or operate in a specific orientation. Therefore, they should not be construed as limitations on the present invention. In the description of the present invention, "plurality" means two or more, unless otherwise specifically specified.

[0022] The terms "first", "second", "third", "fourth", etc. (if any) in the specification and claims of the present application and the above-mentioned drawings are used to distinguish similar objects and are not necessarily used to describe a specific order or sequential order. It should be understood that the numbers used in this way can be interchangeable where appropriate, so that the embodiments of the present application described herein can, for example, be implemented in an order other than those illustrated or described herein. In addition, the terms "including" and "having" and any variations thereof are intended to cover non-exclusive inclusions, for example, a process, method, system, product or device comprising a series of steps or units is not necessarily limited to those steps or units clearly listed, but may include other steps or units that are not clearly listed or inherent to these processes, methods, products or devices.

[0023] To make the purpose, technical solutions, and advantages of the embodiments of this application more clear, the technical solutions in the embodiments of this application will be clearly and completely described below in conjunction with the drawings in the embodiments of this application. Obviously, the described embodiments are part of the embodiments of this application, not all of the embodiments. Based on the embodiments in this application, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of this application.

[0024] The following specific embodiments are used to describe the technical solution of the present invention in detail. The following specific embodiments can be combined with each other, and the same or similar concepts or processes may not be described in detail in some embodiments.

[0025] Please refer to Figure 1 , Figure 1 It is a schematic diagram of the overall structure of the utility model.

[0026] A low-energy consumption gibberellic acid production tank, comprising a tank body 1, which is provided with a feed port 2, a discharge port 3 and a feed and air passage port 4. The tank body 1 forms a tank inner cavity 7, the feed port 2 is opened at the top of the tank body 1, the discharge port 3 is opened at the bottom of the tank body 1, the feed and air passage port 4 is located at the lower part of the tank body 1, the feed and air passage port 4 is connected to a main pipe 5, the main pipe 5 passes through the tank body 1, a part of the main pipe 5 is located in the tank inner cavity 7, and the rest of the main pipe 5 is located outside the tank inner cavity 7, the end of the main pipe 5 located outside the tank inner cavity 7 is connected with an air inlet pipe 51 and a feed pipe 52, a feed valve 53 and a feed cup 54 are installed on the feed pipe 52, an air inlet valve 55 is installed on the air inlet pipe 51, and the air inlet end of the air inlet pipe 51 is connected to an air compressor (not shown in the figure), a cooling coil (not shown in the figure) and an inner cylinder 6 are installed in the tank inner cavity 7, the top of the inner cylinder 6 is provided with an upper opening 61, and the bottom is opened. There is a lower opening 62, and the inner tube 6 forms an inner tube cavity 8. The part of the main pipe 5 located in the inner cavity 7 of the tank body passes through the inner tube 6 and is located in the inner tube cavity 8. Its end opening is downward and is connected to the distributor 9. A first pushing unit 10 is provided below the bottom of the distributor 9. More than three horizontal distribution pipes 11 are connected to the side wall of the distributor 9. The more than three horizontal distribution pipes 11 are evenly distributed along the circumference. More than two second pushing units 12 are provided above each horizontal distribution pipe 11. The first pushing unit 10 is located below the bottom of the inner tube 6, and the second pushing unit 12 is located in the inner tube cavity 8. The first pushing unit 10 is connected to the distributor 9 through the connecting pipe 13, and the second pushing unit 12 is connected to the horizontal distribution pipe 11 through the connecting pipe 13. The pushing inlet of the first pushing unit 10 is at the top, and the pushing outlet is at the bottom. The pushing inlet of the second pushing unit 12 is at the bottom, and the pushing outlet is at the top.

[0027] Both the feed valve 53 and the air inlet valve 55 are solenoid valves. The cooling coil and tank body 1 are identical to those in the prior art, as are the positions of the feed port 2 and discharge port 3. In the prior art, the cooling coil removes heat generated during the reaction to maintain the reaction temperature. The main pipe 5 passes through the feed and air inlet 4, where it is secured to the tank body 1 by welding. The bottom of the inner tube 6 is secured by a support, the bottom of which is connected to the inner wall of the bottom of the tank body 1.

[0028] Furthermore, there are eight horizontal distribution pipes 11 , and two second pushing units 12 are installed on each distribution pipe 11 .

[0029] Furthermore, the main bodies of the first pushing unit 10 and the second pushing unit 12 are both cylinders, one end of the cylinder is connected to the pushing inlet, and the other end is connected to the pushing outlet.

[0030] Furthermore, the push inlet and the push outlet are both conical structures, the small ends of the push inlet and the push outlet are connected to the cylinder, and the large ends are away from the cylinder.

[0031] Furthermore, the diameter of the portion of the connecting pipe 13 located inside the push inlet gradually decreases along the gas running direction.

[0032] Furthermore, the pushing outlet of the first pushing unit 10 is adjacent to the discharge port 3 and is located above the discharge port 3 .

[0033] Furthermore, the upper opening 61 is in the shape of an inverted truncated cone.

[0034] Before production, the production materials enter the tank body cavity 7 and the inner tube cavity 8 through the feed port 3. During production, the compressed gas enters the main pipe 5 from the air inlet pipe 51, and runs through the first pushing unit 10 and the second pushing unit 12. Among them, the second pushing unit 12 diffuses and flows upward, and circulates from the inside to the outside, forming an inside-up, outside-down, and the first pushing unit 10 disturbs and mixes the material retained at the bottom of the tank body cavity 7, and the rising gas drives the material in the retention area to the inner tube cavity 8.

[0035] Example 1 Preparation of Seed Liquid Before Fermentation

[0036] The seed solution before fermentation was prepared according to the process 1.1-1.3 of Example 1 of CN108285915A, wherein the GA3 strain, process, and culture medium were identical. The GA3 strain was Gibberella fujikura, with a deposit number of CGMCC No. 23265 (General Microbiology Center of China Culture Collection Administration).

[0037] The seed liquid test data is shown in Table 1 below.

[0038] Table 1 Seed liquid test data before fermentation

[0039] Wet weight PH Mycelium length Mycelium thickness Is the cytoplasm uniform? Presence of cavitation Fermentation broth viscosity 17-25％ 4.9-5.5 Longer Thinner relatively uniform Small amount ++++

[0040] The seed liquid prepared in Example 1 was used to prepare the fermentation liquids of the following Examples 2 to 7 and Comparative Examples 1 to 2.

[0041] In Examples 2 to 7 and Comparative Examples 1 to 2, the concentration and amount of the seed solution were the same.

[0042] Example 2

[0043] This embodiment adopts Figure 1 The low-energy consumption gibberellic acid production tank of the present invention has a volume of the inner cavity 7 of the tank body of 156 tons (measured in terms of water volume), the axis of the inner tube 6 is the same as the axis of the tank body 1, the diameter of the inner tube 6 is 4 / 5 of the inner diameter of the tank body 1, and the height is 0.7 of the height of the tank body 1. The distance between the end of the other end of the horizontal distribution pipe 11 and the inner wall of the inner tube 6 is 1 / 16 of the inner radius of the inner tube 6, and the distance between the outer wall of the bottom of the inner tube 6 and the discharge port is approximately 1 / 4 of the inner radius of the tank body 1. The tank body 1 is 12m high and 4m in diameter.

[0044] A low-energy consumption gibberellic acid fermentation method comprises the following steps:

[0045] S1. Take the seed solution and fermentation culture medium of Example 1, wherein the mass of the seed solution is 10% of the mass of the fermentation culture medium.

[0046] S2, adding the seed liquid and fermentation culture liquid into the tank body 1 from the feed port 2.

[0047] S3, turn on the heating device ( Figure 1 Not shown in the figure) and open the air inlet valve 55 to carry out the acid production reaction. During the acid production reaction, the nitrogen source and carbon source are supplemented and the pH is controlled by adding ammonia water. The biosynthesis reaction time is 198h.

[0048] Air flow rate is 2200Nm 3 / h, the operating tank pressure is controlled at 0.035MPa, the temperature is controlled at 29±0.2℃, the pH is 5.0~5.2, and the feed and ammonia water are added from the feed pipe 52 (when feeding, open the feed valve 53).

[0049] After the fermentation was completed, samples were taken for testing. The results are shown in Table 3 below.

[0050] In S1, the fermentation broth and the amount added are as shown in Table 2:

[0051] Table 2 Fermentation broth and addition amount

[0052]

[0053] In S3, the feeding method is as follows:

[0054] The first stage: Acid production reaction occurs until the dissolved oxygen rebounds to 60%, and glucose (45%) solution is started to be added. The initial rate of glucose solution addition is 30L / h, and then gradually increased until the glucose solution addition rate reaches 130L / h. The glucose solution addition rate is maintained unchanged. This stage is about 3-4h.

[0055] The second stage: oil addition begins, the initial oil addition rate is 2L / h, and then gradually increases until the oil addition rate reaches 42L / h. During this stage, the glucose solution addition rate is constant at 130L / h, and this stage lasts for about 40-45h.

[0056] The third stage: feed according to the sugar-to-oil ratio (sugar solution volume / oil volume) of 3.2:1. The dissolved oxygen control point is 45%. When the dissolved oxygen is lower than 45%, the feeding rate is reduced. When the dissolved oxygen is higher than 45%, the feeding rate is increased. This stage lasts for 24 hours.

[0057] The fourth stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 2.7:1. The dissolved oxygen control point is 35%. When the dissolved oxygen is lower than 35%, the feeding rate is reduced. When the dissolved oxygen is higher than 35%, the feeding rate is increased. This stage lasts for 24 hours.

[0058] The fifth stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 2.5:1, the dissolved oxygen control point is 25%. When the dissolved oxygen is lower than 25%, the feeding rate is reduced, and when the dissolved oxygen is higher than 25%, the feeding rate is increased. This stage lasts for 6 hours.

[0059] The sixth stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 2.0:1. The dissolved oxygen control point is 20%. When the dissolved oxygen is lower than 20%, reduce the feeding speed. When the dissolved oxygen is higher than 20%, increase the feeding speed. This stage lasts for 6 hours.

[0060] The seventh stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 1.5:1. The dissolved oxygen control point is 15%. When the dissolved oxygen is lower than 15%, reduce the feeding speed. When the dissolved oxygen is higher than 15%, increase the feeding speed. This stage lasts for 6 hours.

[0061] The eighth stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 1.0:1. The dissolved oxygen control point is 10%. When the dissolved oxygen is lower than 10%, the feeding speed is reduced. When the dissolved oxygen is higher than 10%, the feeding speed is increased. This stage lasts until the end of production (i.e., unloading from the tank).

[0062] Example 3

[0063] The difference between this embodiment and embodiment 2 is only the feeding method. The feeding method of this embodiment is:

[0064] The first stage: Acid production reaction occurs until the dissolved oxygen rebounds to 60%, and glucose (45%) solution is started to be added. The initial rate of glucose solution addition is 30L / h, and then gradually increased until the glucose solution addition rate reaches 130L / h. The glucose solution addition rate is maintained unchanged. This stage is about 3-4h.

[0065] The second stage: oil addition begins, the initial oil addition rate is 2L / h, and then gradually increases until the oil addition rate reaches 42L / h. During this stage, the glucose solution addition rate is constant at 130L / h, and this stage lasts for about 40-45h.

[0066] The third stage: feed according to the sugar-to-oil ratio (sugar solution volume / oil volume) of 3.2:1. The dissolved oxygen control point is 45%. When the dissolved oxygen is lower than 45%, the feeding rate is reduced. When the dissolved oxygen is higher than 45%, the feeding rate is increased. This stage lasts for 24 hours.

[0067] The fourth stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 2.7:1. The dissolved oxygen control point is 35%. When the dissolved oxygen is lower than 35%, the feeding rate is reduced. When the dissolved oxygen is higher than 35%, the feeding rate is increased. This stage lasts for 24 hours.

[0068] The fifth stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 2.5:1, the dissolved oxygen control point is 25%. When the dissolved oxygen is lower than 25%, the feeding rate is reduced, and when the dissolved oxygen is higher than 25%, the feeding rate is increased. This stage lasts for 6 hours.

[0069] The sixth stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 2.0:1. The dissolved oxygen control point is 20%. When the dissolved oxygen is lower than 20%, reduce the feeding speed. When the dissolved oxygen is higher than 20%, increase the feeding speed. This stage lasts for 6 hours.

[0070] The seventh stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 1.5:1. The dissolved oxygen control point is 15%. When the dissolved oxygen is lower than 15%, reduce the feeding speed. When the dissolved oxygen is higher than 15%, increase the feeding speed. This stage lasts until the end of production (i.e., unloading the tank).

[0071] After the fermentation was completed, samples were taken for testing. The results are shown in Table 3 below.

[0072] Example 4

[0073] The difference between this embodiment and embodiment 2 is only the feeding method. The feeding method of this embodiment is:

[0074] The first stage: Acid production reaction occurs until the dissolved oxygen rebounds to 60%, and glucose (45%) solution is started to be added. The initial rate of glucose solution addition is 30L / h, and then gradually increased until the glucose solution addition rate reaches 130L / h. The glucose solution addition rate is maintained unchanged. This stage is about 3-4h.

[0075] The second stage: oil addition begins, the initial oil addition rate is 2L / h, and then gradually increases until the oil addition rate reaches 42L / h. During this stage, the glucose solution addition rate is constant at 130L / h, and this stage lasts for about 40-45h.

[0076] The third stage: feed according to the sugar-to-oil ratio (sugar solution volume / oil volume) of 3.2:1. The dissolved oxygen control point is 45%. When the dissolved oxygen is lower than 45%, the feeding rate is reduced. When the dissolved oxygen is higher than 45%, the feeding rate is increased. This stage lasts for 24 hours.

[0077] The fourth stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 2.7:1. The dissolved oxygen control point is 35%. When the dissolved oxygen is lower than 35%, the feeding rate is reduced. When the dissolved oxygen is higher than 35%, the feeding rate is increased. This stage lasts for 24 hours.

[0078] The fifth stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 2.5:1, the dissolved oxygen control point is 25%. When the dissolved oxygen is lower than 25%, the feeding rate is reduced, and when the dissolved oxygen is higher than 25%, the feeding rate is increased. This stage lasts for 6 hours.

[0079] The sixth stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 2.0:1. The dissolved oxygen control point is 20%. When the dissolved oxygen is lower than 20%, the feeding speed is reduced. When the dissolved oxygen is higher than 20%, the feeding speed is increased. This stage lasts until the end of production (i.e., unloading from the tank).

[0080] Example 5

[0081] The difference between this embodiment and embodiment 2 is only the feeding method. The feeding method of this embodiment is:

[0082] The first stage: Acid production reaction occurs until the dissolved oxygen rebounds to 60%, and glucose (45%) solution is started to be added. The initial rate of glucose solution addition is 30L / h, and then gradually increased until the glucose solution addition rate reaches 130L / h. The glucose solution addition rate is maintained unchanged. This stage is about 3-4h.

[0083] The second stage: oil addition begins, the initial oil addition rate is 2L / h, and then gradually increases until the oil addition rate reaches 42L / h. During this stage, the glucose solution addition rate is constant at 130L / h, and this stage lasts for about 40-45h.

[0084] The third stage: feed according to the sugar-to-oil ratio (sugar solution volume / oil volume) of 3.2:1. The dissolved oxygen control point is 45%. When the dissolved oxygen is lower than 45%, the feeding rate is reduced. When the dissolved oxygen is higher than 45%, the feeding rate is increased. This stage lasts for 24 hours.

[0085] The fourth stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 2.7:1. The dissolved oxygen control point is 35%. When the dissolved oxygen is lower than 35%, the feeding rate is reduced. When the dissolved oxygen is higher than 35%, the feeding rate is increased. This stage lasts for 24 hours.

[0086] The fifth stage: feed according to the sugar-oil ratio (sugar solution volume / oil volume) of 2.5:1. The dissolved oxygen control point is 25%. When the dissolved oxygen is lower than 25%, the feeding speed is reduced. When the dissolved oxygen is higher than 25%, the feeding speed is increased. This stage lasts until the end of production (i.e., unloading from the tank).

[0087] Example 6

[0088] Compared with Example 2, the only difference between this embodiment and Example 2 is that the feeding method adopts the feeding method of Example 1 of CN108285915B, that is, the feeding method is: when the dissolved oxygen rebounds by 20%, automatic flow addition of glucose and salad oil is turned on for feeding, glucose (45%) solution: oil (3.2L:1L), the dissolved oxygen control point is 20% to 30%, when the dissolved oxygen is lower than 20%, the feeding speed is reduced, and when the dissolved oxygen is higher than 30%, the feeding speed is increased.

[0089] After the fermentation was completed, samples were taken for testing. The results are shown in Table 3 below.

[0090] Example 7

[0091] The only difference between this embodiment and embodiment 2 is that the supplementary material is added from the feed port 2.

[0092] After the fermentation was completed, samples were taken for testing. The results are shown in Table 3 below.

[0093] Comparative Example 1

[0094] The difference between this comparative example and Example 2 is that the feed is added from feed port 2, and the feeding method is the same as the feeding method in Example 1 of CN108285915A.

[0095] After the fermentation was completed, samples were taken for testing. The results are shown in Table 3 below.

[0096] Comparative Example 2

[0097] Compared with Example 2, this comparative example has the following differences:

[0098] 1. The production tank adopts the production tank of CN201990659U. The tank body, height, diameter, volume, heating and cooling systems of the production tank are the same as those of the production tank of the present invention. The only difference is that the CN201990659U is a stirring type with an agitator installed, while the present invention has an inner cylinder 6 and supporting components such as the first pushing unit 10.

[0099] 2. The stirring speed of this comparative example is: 150-200 rpm, and the motor power is 500 kw.h.

[0100] 3. Supplementary material is added from the feed port, and the feeding method is the same as that in Example 1 of CN108285915A.

[0101] After the fermentation was completed, samples were taken for testing. The results are shown in Table 3 below.

[0102] Table 3 Fermentation broth test data

[0103]

[0104]

[0105] The above description is merely a preferred embodiment of the present invention and is not intended to limit the present invention. Those skilled in the art will readily appreciate that the present invention is susceptible to various modifications and variations. Any modifications, equivalent substitutions, or improvements made within the spirit and principles of the present invention shall be included within the scope of protection of the present invention.

Claims

1. A low-energy consumption gibberellic acid production device, comprising a tank body (1), a feed inlet (2) and a discharge outlet (3) being provided on the tank body (1), the tank body (1) forming a tank inner cavity (7), the feed inlet (2) being provided at the top of the tank body (1), and the discharge outlet (3) being provided at the bottom of the tank body (1), characterized in that: The tank body (1) is also provided with a feeding and air passage port (4), which is located at the lower part of the tank body (1). The feeding and air passage port (4) is connected to a main pipe (5), which passes through the tank body (1), wherein a portion of the main pipe (5) is located in the tank body cavity (7) and the remaining portion is located outside the tank body cavity (7). The end of the main pipe (5) located outside the tank body cavity (7) is connected to an air inlet pipe (51) and A feeding pipe (52) is provided, a feeding valve (53) and a feeding cup (54) are installed on the feeding pipe (52), an air intake valve (55) is installed on the air intake pipe (51), an inner cylinder (6) is installed in the inner cavity (7) of the tank body, an upper opening (61) is opened on the top of the inner cylinder (6), and a lower opening (62) is opened on the bottom, and the inner cylinder (6) forms an inner cylinder cavity (8), and the part of the main pipe (5) located in the inner cavity (7) of the tank body passes through the inner cylinder (6) and is located The inner cavity (8) of the inner cylinder has an end opening facing downward and is connected to the distributor (9). A first pushing unit (10) is provided below the bottom of the distributor (9). Three or more horizontal distribution pipes (11) are connected to the side wall of the distributor (9). The three or more horizontal distribution pipes (11) are evenly distributed along the circumference. Two or more second pushing units (12) are provided above each horizontal distribution pipe (11). The first pushing unit (10) is located below the bottom of the inner cylinder (6). The second pushing unit (12) is located in the inner cavity (8) of the inner cylinder. The first pushing unit (10) is connected to the distributor (9) through a connecting pipe (13). The second pushing unit (12) is connected to the horizontal distribution pipe (11) through a connecting pipe (13). The pushing inlet of the first pushing unit (10) is at the top and the pushing outlet is at the bottom. The pushing inlet of the second pushing unit (12) is at the bottom and the pushing outlet is at the top.

2. The low-energy consumption gibberellic acid production device according to claim 1, characterized in that: The feed valve (53) and the air inlet valve (55) are both solenoid valves.

3. The low-energy consumption gibberellic acid production device according to claim 1, characterized in that: There are eight horizontal distribution pipes (11), and two second pushing units (12) are installed on each horizontal distribution pipe (11).

4. The low-energy consumption gibberellic acid production device according to claim 1, characterized in that: The main bodies of the first pushing unit (10) and the second pushing unit (12) are both cylinders, one end of the cylinder is connected to the pushing inlet, and the other end is connected to the pushing outlet.

5. The low-energy consumption gibberellic acid production device according to claim 4, characterized in that: The push inlet and the push outlet are both conical structures, the small ends of the push inlet and the push outlet are connected to the cylinder, and the large ends are away from the cylinder.

6. The low-energy consumption gibberellic acid production device according to claim 1, characterized in that: The diameter of the portion of the connecting pipe (13) located in the driving inlet gradually decreases along the running direction of the gas.

7. The low-energy consumption gibberellic acid production device according to claim 1, characterized in that: The pushing outlet of the first pushing unit (10) is adjacent to the discharge port (3) and is located above the discharge port (3).

8. The low-energy consumption gibberellic acid production device according to claim 1, characterized in that: The upper opening (61) is in the shape of an inverted truncated cone.

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