Oxygenation energy-saving device for fermentation of high-viscosity materials

Abstract

The utility model provides an oxygen-increasing energy-saving device for fermentation of high-viscosity materials. The oxygen-increasing energy-saving device comprises a tank body, a stirring shaft, a plurality of stirring blades, a guide cylinder, an air circular ring pipe, an upper layer of venturi nozzles and a lower layer of venturi nozzles, the lower stirring blade is a semi-open type stirring impeller, and an outlet of the guide cylinder directly faces the central part of the lower stirring blade; the upper layer of Venturi nozzles and the lower layer of Venturi nozzles are respectively upward nozzles and downward nozzles, the Venturi nozzles are uniformly distributed on the annular air pipe, the upward nozzles and the downward nozzles are alternately arranged, the upward nozzles are arranged in an upward and inward inclined manner, the downward nozzles are arranged in a downward and inward inclined manner, and the inward inclined directions of the upward nozzles and the downward nozzles are opposite. Through the combination of the guide cylinder and the semi-open type stirring impeller in the tank body and the distribution of the Venturi nozzles, the size and dispersion of bubbles can be effectively controlled, so that gas and liquid are mixed more sufficiently, the mixing efficiency, the oxygen dissolving efficiency and the production efficiency are improved, meanwhile, the stirring energy consumption is reduced, and the gas-liquid mixer is particularly suitable for a fermentation system of high-viscosity materials.

Description

Technical Field

[0001] The utility model belongs to the technical field of biological fermentation and relates to an oxygen-enhancing energy-saving device for fermenting high-viscosity materials. Background Art

[0002] Aerobic fermentation is one of the types of microbial fermentation. The dissolution efficiency of oxygen is crucial to the growth of microorganisms and product synthesis, especially for high-viscosity fermentation systems. High-viscosity media will affect the oxygen transfer efficiency, thereby limiting the growth of microorganisms and product formation. The equipment used for fermentation is usually a fermentation tank. Based on the key role of mechanical stirring in the fermentation process, mechanical stirring fermentation tanks are the most commonly used type. They play a significant role in the entire product development and production process and can be widely used in the pharmaceutical, food, chemical and other industries.

[0003] Mechanically stirred fermentation tanks often use methods such as increasing the mechanical stirring speed, increasing the compressed air pressure or flow, and increasing the tank pressure to increase dissolved oxygen, but the fermentation of high-viscosity materials is often not effective and has high energy consumption. Due to the flow characteristics of the liquid, traditional oxygenation methods often have difficulty in achieving effective oxygen transfer and mixing, resulting in the fermentation dissolved oxygen failing to meet the needs of microorganisms, and the product volume is low, resulting in poor fermentation results. The traditional methods adopted in this way also generate a lot of energy consumption, further restricting the economic benefits of the fermentation process. Therefore, for the fermentation application of high-viscosity materials, it is necessary to improve the structure of traditional fermentation equipment to improve the oxygen transfer efficiency and reduce energy consumption.

[0004] CN 203212564U discloses a fermentation tank, which includes a tank body, a stirring shaft arranged in the tank body, a paddle stirrer in the middle and a turbine stirrer at the bottom respectively arranged on the stirring shaft, a venting device is also arranged in the tank body, an air inlet of the venting device is connected to an air compressor, the venting device is arranged between the paddle stirrer and the turbine stirrer, the venting device is composed of a ring-spray ejector with a plurality of nozzles arranged in an annular manner, the air compressor is connected to a ring-shaped pipe connected to each nozzle on the ring-spray ejector, and the ejection port of the nozzle faces the bottom of the tank body. The fermentation tank sets the venting device in the middle, which is not conducive to the mixing of air and the lower fluid. Although a guide tube is also provided, the air tends to move upward after being ejected. To achieve outflow from the bottom, a higher air pressure and a slower rate are required, and the increase in dissolved oxygen rate is not utilized, and energy consumption will be increased.

[0005] CN 201485447U discloses an energy-saving high-viscosity fermentation tank built-in homogenizing mixer and a fermentation tank thereof, wherein the mixer comprises an air distributor, a nozzle arranged on the air distributor, and a gas-liquid homogenizing injector with a drainage device arranged corresponding to the injection direction of the nozzle, and the drainage device faces the injection direction of the nozzle; the projection of the axis of the gas-liquid homogenizing injector on the horizontal section forms an angle with the circumferential tangent at the nozzle outlet, and the axis also forms an angle with the horizontal plane, so that the injection gas-liquid flow direction formed by the gas-liquid homogenizing injector is inclined upward along the stirring axis direction. Although the homogenizing mixer arranged in the fermentation tank can also improve the mixing and dispersion effect and energy-saving effect to a certain extent, the distribution regularity of the nozzle and the injector is not strong, and the bubbles formed cannot be effectively controlled.

[0006] In summary, the setting of stirring, spraying and other components in the fermentation equipment needs to be reasonably arranged and selected according to the function of each component, so as to improve the uniformity of gas distribution and dissolved oxygen efficiency, improve production efficiency, and reduce stirring energy consumption. Utility Model Content

[0007] In view of the problems existing in the prior art, the purpose of the utility model is to provide an oxygen-enriching and energy-saving device for the fermentation of high-viscosity materials. The device can effectively control the size and dispersion of bubbles through the combination of a guide tube and a semi-open stirring impeller in the tank body and the distribution of Venturi nozzles on the air ring tube, so that the gas-liquid mixing is more sufficient, the mixing efficiency and the dissolved oxygen efficiency are improved, the dissolved oxygen dead zone is effectively eliminated, the production efficiency is improved, and the stirring energy consumption can also be reduced. The device is particularly suitable for the fermentation system of high-viscosity materials.

[0008] To achieve this purpose, the utility model adopts the following technical solutions:

[0009] The utility model provides an oxygen-enriching and energy-saving device for fermenting high-viscosity materials, the oxygen-enriching and energy-saving device comprising a tank body, a stirring shaft and a plurality of stirring blades arranged on the stirring shaft, a guide tube, an air annular tube and upper and lower layers of Venturi nozzles arranged on the air annular tube; the stirring blade at the bottom of the stirring shaft is a stirring lower blade, the stirring lower blade is a semi-open stirring impeller, the lower part of the stirring lower blade is a guide tube, and the outlet of the guide tube is directly opposite to the central part of the stirring lower blade;

[0010] The air annular tube and the Venturi nozzle are located below the guide tube. The upper and lower layers of Venturi nozzles are respectively an upward nozzle and a downward nozzle, which are located on the upper and lower sides of the air annular tube, and the upward nozzle faces the inlet of the guide tube. The Venturi nozzles are evenly distributed on the circumference of the air annular tube, and the upward nozzle and the downward nozzle are arranged alternately. The upward nozzle is arranged to be inclined upward and inward, and the downward nozzle is arranged to be inclined downward and inward, and the inward inclination directions of the upward nozzle and the downward nozzle are opposite.

[0011] In the utility model, for the device used for fermentation of high-viscosity materials, it is necessary to reasonably design its internal structure. On the basis of the traditional fermentation tank structure, the stirring lower blade is designed as a semi-open stirring impeller structure, and a guide tube is arranged below it. The centrifugal force when the stirring lower blade rotates can be used to better disperse and throw out the gas-liquid mixture flowing out of the guide tube, and at the same time, the bubbles in the mixed phase are broken up, and the size and dispersion of the bubbles are controlled, so as to greatly improve the gas-liquid mixing efficiency, thereby improving the dissolved oxygen efficiency; at the same time, the potential energy of the compressed air can drive the kinetic energy of the gas-liquid mixed phase conversion, generate radial driving force on the impeller, reduce the power load of mechanical stirring, and achieve energy-saving effect; and the design form of the Venturi nozzle on the air ring tube enables the air and the material to fully contact, eliminates the dissolved oxygen dead zone at the bottom of the tank, and improves the uniformity of dissolved oxygen; through the design of the internal structure of the above-mentioned device, the dissolved oxygen can be effectively increased, the energy consumption can be reduced, and it is particularly suitable for high-viscosity material systems, and the fermentation efficiency can be improved.

[0012] In the utility model, the high-viscosity material used in the fermentation industry refers to the fermentation liquid containing different bacteria. Due to the different properties of the bacteria, such as the long and scattered hyphae of fungi, the appearance of the liquid shows a high viscosity, which affects the fluidity of the liquid. It is a solid-liquid mixed phase, which is different from the viscosity of a single liquid phase in the traditional sense. It is an abstract qualitative description in this field. After removing solid phases such as bacteria, the high viscosity of the liquid fermentation liquid alone can usually reach more than 1000 centipoise.

[0013] The following are preferred technical solutions of the present invention, but are not intended to be limitations of the technical solutions provided by the present invention. Through the following technical solutions, the technical objectives and beneficial effects of the present invention can be better achieved and realized.

[0014] As a preferred technical solution of the utility model, the shape of the tank body includes cylindrical or conical. In addition to selecting the tank body of the above shapes, other shapes suitable for fermentation can also be selected.

[0015] A stirring motor is arranged at the upper outer portion of the tank body, and the stirring motor is connected to a stirring shaft, and the stirring shaft passes through the top of the tank body and extends to the lower portion of the tank body.

[0016] In the utility model, the stirring shaft needs to pass through the top of the tank body, and also has a part outside the tank body. The connection between the stirring shaft on the outside and the tank body is fixed by a mechanical seal to avoid air leakage; and because the stirring shaft is relatively long, it is supported and fixed in the tank body by a square seat connected to the tank wall. The middle and upper part of the stirring shaft is provided with stirring blades of different forms and numbers, and these stirring blades are stirring blades of traditional forms.

[0017] As a preferred technical solution of the utility model, the lower stirring blade is a semi-open large-width impeller. The lower stirring blade is disc-shaped as a whole, including a central part and surrounding blade parts. The blades are welded and attached to the bottom of the disc plane. The overall diameter of the lower stirring blade is 1.5 to 3 times the diameter of the central part, for example, 1.5 times, 1.8 times, 2 times, 2.2 times, 2.5 times, 2.7 times or 3 times, etc., but is not limited to the listed values, and other unlisted values ​​within this numerical range are also applicable.

[0018] In the utility model, the stirring lower blade is also called bottom stirring, which selects a semi-open large-width impeller, and its main function is to generate centrifugal force through high-speed rotation, guide the gas-liquid mixed phase upward from the guide tube, and pass through the stirring blade flow channel below the impeller through the radial direction, and throw it outward and downward around, while breaking up large bubbles in the gas-liquid mixed phase and converting them into small bubbles, increasing the gas-liquid contact area, and increasing the retention time of the gas in the tank body, thereby increasing the dissolved oxygen rate.

[0019] Since the upward outlet of the guide tube is located at the central suction port of the stirring impeller, the compressed air flows out at high speed through the Venturi nozzle. The potential energy of the compressed air drives the kinetic energy of the gas-liquid mixed phase conversion, which produces a large continuous circulating axial and circumferential driving force on the impeller stirring blades, which can effectively reduce the dynamic load of mechanical stirring and achieve an energy saving effect of more than 20% compared with other similar stirring machines.

[0020] As a preferred technical solution of the present invention, the number of blades in the stirring lower blade is 6 to 12, for example, 6, 7, 8, 9, 10, 11 or 12, etc. The blades are curved, and the angle between them and the plane of the disk is 15 to 45 degrees, for example, 15 degrees, 20 degrees, 25 degrees, 30 degrees, 35 degrees, 40 degrees or 45 degrees, etc., but are not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable. The width of the blade is 1 / 15 to 1 / 5 of the diameter of the center part of the stirring lower blade, for example, 1 / 15, 2 / 25, 1 / 10, 1 / 9, 1 / 8, 1 / 7, 3 / 20, 1 / 6 or 1 / 5, etc., but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0021] In the utility model, the number of blades in the stirring lower blade can be adjusted according to the scale of the fermentation tank and the material characteristics.

[0022] As a preferred technical solution of the utility model, the guide cylinder is divided into two parts: a main cylinder and a tapered inlet, and the diameter of the tapered inlet gradually decreases until it becomes the same as the diameter of the main cylinder.

[0023] As a preferred technical solution of the present invention, the overall height of the guide tube is 1 / 20 to 1 / 5 of the height of the tank body, for example, 1 / 20, 1 / 15, 2 / 25, 1 / 10, 1 / 9, 1 / 8, 1 / 7, 3 / 20, 1 / 6 or 1 / 5, etc., but is not limited to the listed values, and other unlisted values ​​within the numerical range are equally applicable, wherein the ratio of the height of the main cylinder to the height of the guide tube is 1 / 4 to 3 / 4, for example, 1 / 4, 3 / 10, 1 / 3, 2 / 5, 1 / 2, 3 / 5, 2 / 3 or 3 / 4, etc., but is not limited to the listed values, and other unlisted values ​​within the numerical range are equally applicable.

[0024] The diameter of the main cylinder in the guide tube is 1 / 10 to 1 / 3 of the inner diameter of the tank body, for example, 1 / 10, 3 / 20, 1 / 5, 1 / 4, 3 / 10 or 1 / 3, etc., but is not limited to the listed values, and other values ​​not listed within the numerical range are also applicable. The maximum diameter of the conical inlet is 2 to 5 times the diameter of the main cylinder, for example, 2 times, 2.5 times, 3 times, 3.5 times, 4 times, 4.5 times or 5 times, etc., but is not limited to the listed values, and other values ​​not listed within the numerical range are also applicable.

[0025] The diameter of the main cylinder in the guide cylinder is the same as the diameter of the center of the stirring lower blade.

[0026] In the utility model, the main function of the guide tube is to guide and accelerate the gas-liquid mixture to flow from bottom to top, thereby enhancing the mass transfer effect between gas and liquid. Combined with the concentrated jet effect of the Venturi nozzle on the air ring tube, an overall Venturi tube effect is formed. The outlet of the guide tube is located below the center of the stirring lower blade, and the distance between the controller and the stirring lower blade is smaller than the width of the blade, which can promote the gas-liquid mixture to escape and be thrown out along the direction of the flow channel between the stirring blades.

[0027] As a preferred technical solution of the utility model, the air ring tube is connected to the air inlet at the bottom of the tank body, the air inlet at the bottom of the tank body is connected to an air compressor, and the air ring tube is connected to the inlet of each venturi nozzle.

[0028] In the utility model, when the device is in use, the air ring tube at the bottom of the tank is connected to the air inlet at the bottom of the fermentation tank body, the air compressor is turned on, and the compressed air enters the venturi nozzle through the air ring tube at the bottom of the tank. At the same time, the stirring motor is turned on to rotate the stirring lower blade to stir the material evenly.

[0029] The diameter of the air ring tube is 1 / 4 to 3 / 4 of the inner diameter of the tank body, for example 1 / 4, 3 / 10, 1 / 3, 2 / 5, 1 / 2, 3 / 5, 2 / 3 or 3 / 4, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable. The diameter of the air ring tube is 80 to 250 mm, for example 80 mm, 100 mm, 125 mm, 150 mm, 200 mm or 250 mm, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0030] In the utility model, the size and position of the air ring pipe at the bottom of the tank can be adjusted according to the viscosity and density characteristics of the material to achieve the best dissolved oxygen effect and energy consumption performance.

[0031] As a preferred technical solution of the present invention, the number of the Venturi nozzles is 4 to 20, for example, 4, 6, 8, 10, 12, 14, 16, 18 or 20, and the number of the upward nozzles and the downward nozzles is the same.

[0032] In the utility model, the number of the venturi nozzles can be adjusted according to the scale of the fermentation tank and the material characteristics.

[0033] When the Venturi nozzle is tilted upward or downward, the angle with the horizontal direction is 10 to 60 degrees, for example 10 degrees, 20 degrees, 30 degrees, 40 degrees, 45 degrees, 50 degrees or 60 degrees, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0034] The angle between the projection of the Venturi nozzle on the horizontal plane and the radial direction of the air ring tube passing through its inlet is 10 to 60 degrees, for example, 10 degrees, 20 degrees, 30 degrees, 40 degrees, 45 degrees, 50 degrees or 60 degrees, but is not limited to the listed values, and other unlisted values ​​within this numerical range are also applicable.

[0035] In the utility model, the venturi nozzle is arranged in two layers, the upper venturi nozzle sprays toward the inlet direction of the guide tube, so that the gas-liquid mixed phase enters the center of the stirring lower blade upward from the guide tube, and is thrown out to the side and lower through the flow channel, which increases the gas phase retention time, thereby increasing the dissolved oxygen and reducing the stirring energy consumption; the lower venturi nozzle sprays obliquely downward, and the gas-liquid mixed phase diverges upward from the bottom of the tank to stir the material, further increasing the dissolved oxygen. By adjusting the number and angle of the venturi nozzles, the dissolved oxygen efficiency and stirring energy consumption can be further optimized.

[0036] As a preferred technical solution of the utility model, the inward tilting direction of the upward nozzle is generally clockwise, and the inward tilting direction of the downward nozzle is generally counterclockwise, or the inward tilting direction of the upward nozzle is generally counterclockwise, and the inward tilting direction of the downward nozzle is generally clockwise.

[0037] In the utility model, the main function of the venturi nozzle is to eject the gas-liquid mixture in a specific direction and speed to enhance the mass transfer effect. The ejection direction of the upward nozzle should be inward at a certain angle to the horizontal plane and in a clockwise direction, while the ejection direction of the downward nozzle should be inward at a certain angle to the horizontal plane and in a counterclockwise direction.

[0038] As a preferred technical solution of the utility model, a support structure is provided in the tank body, and the support structure is connected to the inner wall of the tank body to support and fix the stirring shaft, the guide cylinder and the air ring tube.

[0039] In the utility model, the support structure is used to support and fix the structural components in the tank body to ensure the stable operation of the entire device.

[0040] Compared with the prior art, the utility model has the following beneficial effects:

[0041] (1) The device of the utility model can utilize the centrifugal force of the rotating impeller to better disperse and throw out the gas-liquid mixture flowing out of the guide tube, and at the same time break up the bubbles in the mixed phase, control the size and dispersion of the bubbles, greatly improve the gas-liquid mixing efficiency, and thus improve the dissolved oxygen efficiency.

[0042] (2) The device of the utility model utilizes the potential energy of compressed air to drive the kinetic energy of the gas-liquid mixed phase conversion, generates axial and circumferential driving forces on the impeller, reduces the power load of mechanical stirring, achieves energy-saving effects, and can save more than 20% of energy consumption;

[0043] (3) The design of the upper and lower venturi nozzles of the air annular tube of the utility model allows the air and the material to fully contact, eliminating the dead zone of dissolved oxygen at the bottom of the tank and improving the uniformity of dissolved oxygen;

[0044] (4) The utility model can achieve efficient oxygen transfer and mixing through the comprehensive regulation of the device, meet the dissolved oxygen demand of aerobic microorganisms, and effectively reduce stirring energy consumption, especially in high-viscosity fermentation systems, thereby improving fermentation production efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0045] Figure 1 It is a structural schematic diagram of an oxygen-enriching and energy-saving device for fermentation of high-viscosity materials provided in Example 1 of the utility model;

[0046] Figure 2 This is a bottom view of the stirring lower blade in the oxygen-enhancing and energy-saving device provided in Example 1 of the utility model;

[0047] Figure 3 It is a top view of the cross section of the air annular tube and the Venturi nozzle in the oxygen-enhancing energy-saving device provided in Example 2 of the utility model;

[0048] Among them, 1-tank body, 2-stirring shaft, 3-stirring lower blade, 4-guide tube, 5-air ring tube, 6-Venturi nozzle. DETAILED DESCRIPTION

[0049] In order to better illustrate the present invention and facilitate understanding of the technical solution of the present invention, the present invention is further described in detail below. However, the following embodiments are only simple examples of the present invention and do not represent or limit the scope of protection of the present invention. The scope of protection of the present invention shall be subject to the claims.

[0050] The following are typical but non-limiting embodiments of the present invention:

[0051] Embodiment 1:

[0052] This embodiment provides an oxygen-enhancing energy-saving device for fermentation of high-viscosity materials. The structural schematic diagram of the oxygen-enhancing energy-saving device is as follows: Figure 1 As shown, it includes a tank body 1, a stirring shaft 2 and a plurality of stirring blades arranged on the stirring shaft 2, a guide tube 4, an air ring tube 5 and upper and lower layers of Venturi nozzles 6 arranged on the air ring tube 5; the stirring blade at the bottom of the stirring shaft 2 is a lower stirring blade 3, and the lower stirring blade 3 is a semi-open stirring impeller, and its bottom view is as shown in Figure 2 As shown, below the stirring lower blade 3 is a guide tube 4, and the outlet of the guide tube 4 is directly facing the center of the stirring lower blade 3;

[0053] The air annular tube 5 and the Venturi nozzle 6 are located below the guide tube 4. The upper and lower layers of the Venturi nozzles 6 are respectively an upward nozzle and a downward nozzle, which are located on the upper and lower sides of the air annular tube 5, and the upward nozzle faces the inlet of the guide tube 4. The Venturi nozzles 6 are evenly distributed on the circumference of the air annular tube 5, and the upward nozzles and the downward nozzles are arranged alternately. The upward nozzle is arranged to be inclined upward and inward, and the downward nozzle is arranged to be inclined downward and inward, and the inward inclination directions of the upward nozzle and the downward nozzle are opposite.

[0054] The tank body 1 is cylindrical in shape; a stirring motor is provided on the upper outer portion of the tank body 1 , and the stirring motor is connected to a stirring shaft 2 , and the stirring shaft 2 passes through the top of the tank body 1 and extends to the lower portion of the tank body 1 .

[0055] The stirring lower blade 3 is a semi-open large-width impeller. The stirring lower blade 3 is disc-shaped as a whole, including a central part and surrounding blade parts. The blades are welded and attached below the disc plane. The overall diameter of the stirring lower blade 3 is twice the diameter of the central part.

[0056] The number of blades in the stirring lower blade 3 is 8. The blades are curved, and the angle between them and the plane of the disk is 30 degrees. The width of the blades is 1 / 10 of the diameter of the central part of the stirring lower blade 3.

[0057] The guide cylinder 4 is divided into two parts: a main cylinder and a conical inlet. The diameter of the conical inlet gradually decreases until it becomes the same as the diameter of the main cylinder.

[0058] The overall height of the guide tube 4 is 1 / 8 of the height of the tank body 1 , wherein the height of the main cylinder accounts for 1 / 2 of the height of the guide tube 4 .

[0059] The diameter of the main cylinder in the guide tube 4 is 1 / 5 of the inner diameter of the tank body 1, and the maximum diameter of the conical inlet is 3 times the diameter of the main cylinder.

[0060] The diameter of the main cylinder in the guide tube 4 is the same as the diameter of the center of the stirring lower blade 3.

[0061] The air annular tube 5 is connected to the air inlet at the bottom of the tank body 1 , the air inlet at the bottom of the tank body 1 is connected to an air compressor, and the air annular tube 5 is communicated with the inlet of each venturi nozzle 6 .

[0062] The diameter of the air ring tube 5 is 3 / 5 of the inner diameter of the tank body 1, and the diameter of the air ring tube 5 is 150 mm.

[0063] The number of the Venturi nozzles 6 is 10, and the number of the upward nozzles and the downward nozzles is the same.

[0064] When the Venturi nozzle 6 is tilted upward or downward, the angle between it and the horizontal direction is 30 degrees.

[0065] The included angle between the projection of the Venturi nozzle 6 on the horizontal plane and the radial direction of the air annular tube 5 passing through the inlet thereof is 30 degrees.

[0066] The inwardly inclined direction of the upward nozzle is generally clockwise, and the inwardly inclined direction of the downward nozzle is generally counterclockwise.

[0067] A support structure is provided inside the tank body 1 , and the support structure is connected to the inner wall of the tank body 1 to support and fix the stirring shaft 2 , the guide tube 4 and the air ring tube 5 .

[0068] Embodiment 2:

[0069] This embodiment provides an oxygen-enhancing and energy-saving device for fermenting high-viscosity materials, the oxygen-enhancing and energy-saving device comprises a tank body 1, a stirring shaft 2 and a plurality of stirring blades arranged on the stirring shaft 2, a guide tube 4, an air annular tube 5 and upper and lower layers of Venturi nozzles 6 arranged on the air annular tube 5, and a top view of the cross section of the air annular tube 5 and the Venturi nozzle 6 is shown in FIG. Figure 3 As shown; the lowest stirring blade on the stirring shaft 2 is the stirring lower blade 3, the stirring lower blade 3 is a semi-open stirring impeller, and below the stirring lower blade 3 is a guide tube 4, and the outlet of the guide tube 4 is directly opposite to the center of the stirring lower blade 3;

[0070] The air annular tube 5 and the Venturi nozzle 6 are located below the guide tube 4. The upper and lower layers of the Venturi nozzles 6 are respectively an upward nozzle and a downward nozzle, which are located on the upper and lower sides of the air annular tube 5, and the upward nozzle faces the inlet of the guide tube 4. The Venturi nozzles 6 are evenly distributed on the circumference of the air annular tube 5, and the upward nozzles and the downward nozzles are arranged alternately. The upward nozzle is arranged to be inclined upward and inward, and the downward nozzle is arranged to be inclined downward and inward, and the inward inclination directions of the upward nozzle and the downward nozzle are opposite.

[0071] The tank body 1 is cylindrical in shape; a stirring motor is provided on the upper outer portion of the tank body 1 , and the stirring motor is connected to a stirring shaft 2 , and the stirring shaft 2 passes through the top of the tank body 1 and extends to the lower portion of the tank body 1 .

[0072] The stirring lower blade 3 is a semi-open large-width impeller. The stirring lower blade 3 is disc-shaped as a whole, including a central part and surrounding blade parts. The blades are welded and attached below the disc plane. The overall diameter of the stirring lower blade 3 is 3 times the diameter of the central part.

[0073] The number of blades in the stirring lower blade 3 is 6. The blades are curved, and the angle between them and the plane of the disk is 45 degrees. The width of the blades is 1 / 5 of the diameter of the central part of the stirring lower blade 3.

[0074] The guide cylinder 4 is divided into two parts: a main cylinder and a conical inlet. The diameter of the conical inlet gradually decreases until it becomes the same as the diameter of the main cylinder.

[0075] The overall height of the guide tube 4 is 1 / 20 of the height of the tank body 1 , wherein the height of the main cylinder accounts for 3 / 4 of the height of the guide tube 4 .

[0076] The diameter of the main cylinder in the guide tube 4 is 1 / 10 of the inner diameter of the tank body 1, and the maximum diameter of the conical inlet is 4 times the diameter of the main cylinder.

[0077] The diameter of the main cylinder in the guide tube 4 is the same as the diameter of the center of the stirring lower blade 3.

[0078] The air annular tube 5 is connected to the air inlet at the bottom of the tank body 1 , the air inlet at the bottom of the tank body 1 is connected to an air compressor, and the air annular tube 5 is communicated with the inlet of each venturi nozzle 6 .

[0079] The diameter of the air ring tube 5 is 2 / 3 of the inner diameter of the tank body 1, and the diameter of the air ring tube 5 is 100 mm.

[0080] The number of the Venturi nozzles 6 is 8, and the number of the upward nozzles and the downward nozzles is the same.

[0081] When the Venturi nozzle 6 is tilted upward or downward, the angle between it and the horizontal direction is 60 degrees.

[0082] The included angle between the projection of the Venturi nozzle 6 on the horizontal plane and the radial direction of the air annular tube 5 passing through the inlet thereof is 60 degrees.

[0083] The inwardly inclined direction of the upward nozzle is generally clockwise, and the inwardly inclined direction of the downward nozzle is generally counterclockwise.

[0084] A support structure is provided in the tank body 1 , and the support structure is connected to the inner wall of the tank body 1 to support and fix the stirring shaft 2 , the guide tube 4 and the air ring tube 5 .

[0085] Embodiment 3:

[0086] The present embodiment provides an oxygen-enriching and energy-saving device for fermenting high-viscosity materials, the oxygen-enriching and energy-saving device comprising a tank body 1, a stirring shaft 2 and a plurality of stirring blades arranged on the stirring shaft 2, a guide tube 4, an air annular tube 5 and upper and lower layers of Venturi nozzles 6 arranged on the air annular tube 5; the lowest stirring blade on the stirring shaft 2 is a lower stirring blade 3, the lower stirring blade 3 is a semi-open stirring impeller, the lower part of the lower stirring blade 3 is a guide tube 4, and the outlet of the guide tube 4 is directly opposite to the center of the lower stirring blade 3;

[0087] The air annular tube 5 and the Venturi nozzle 6 are located below the guide tube 4. The upper and lower layers of the Venturi nozzles 6 are respectively an upward nozzle and a downward nozzle, which are located on the upper and lower sides of the air annular tube 5, and the upward nozzle faces the inlet of the guide tube 4. The Venturi nozzles 6 are evenly distributed on the circumference of the air annular tube 5, and the upward nozzles and the downward nozzles are arranged alternately. The upward nozzle is arranged to be inclined upward and inward, and the downward nozzle is arranged to be inclined downward and inward, and the inward inclination directions of the upward nozzle and the downward nozzle are opposite.

[0088] The tank body 1 is conical in shape; a stirring motor is provided on the upper outer portion of the tank body 1 , and the stirring motor is connected to a stirring shaft 2 , and the stirring shaft 2 passes through the top of the tank body 1 and extends to the lower portion of the tank body 1 .

[0089] The stirring lower blade 3 is a semi-open wide-channel impeller. The stirring lower blade 3 is disc-shaped as a whole, including a central part and surrounding blade parts. The blades are welded and attached below the disc plane. The overall diameter of the stirring lower blade 3 is 1.5 times the diameter of the central part.

[0090] The number of blades in the stirring lower blade 3 is 12. The blades are curved, and the angle between them and the plane of the disk is 15 degrees. The width of the blades is 1 / 15 of the diameter of the central part of the stirring lower blade 3.

[0091] The guide cylinder 4 is divided into two parts: a main cylinder and a conical inlet. The diameter of the conical inlet gradually decreases until it becomes the same as the diameter of the main cylinder.

[0092] The overall height of the guide tube 4 is 1 / 5 of the height of the tank body 1 , wherein the height of the main cylinder accounts for 1 / 3 of the height of the guide tube 4 .

[0093] The diameter of the main cylinder in the guide tube 4 is 1 / 3 of the inner diameter of the tank body 1, and the maximum diameter of the conical inlet is twice the diameter of the main cylinder.

[0094] The diameter of the main cylinder in the guide tube 4 is the same as the diameter of the center of the stirring lower blade 3.

[0095] The air annular tube 5 is connected to the air inlet at the bottom of the tank body 1 , the air inlet at the bottom of the tank body 1 is connected to an air compressor, and the air annular tube 5 is communicated with the inlet of each venturi nozzle 6 .

[0096] The diameter of the air ring tube 5 is 1 / 2 of the inner diameter of the tank body 1, and the diameter of the air ring tube 5 is 250 mm.

[0097] The number of the Venturi nozzles 6 is 16, and the number of the upward nozzles and the downward nozzles is the same.

[0098] When the Venturi nozzle 6 is tilted upward or downward, the angle between it and the horizontal direction is 15 degrees.

[0099] The included angle between the projection of the Venturi nozzle 6 on the horizontal plane and the radial direction of the air annular tube 5 passing through the inlet of the Venturi nozzle 6 is 15 degrees.

[0100] The inwardly inclined direction of the upward nozzle is generally counterclockwise, and the inwardly inclined direction of the downward nozzle is generally clockwise.

[0101] A support structure is provided in the tank body 1 , and the support structure is connected to the inner wall of the tank body 1 to support and fix the stirring shaft 2 , the guide tube 4 and the air ring tube 5 .

[0102] Comparative Example 1:

[0103] This comparative example provides a device for fermenting high-viscosity materials. The structure of the device refers to the structure in Example 1, with the only difference being that the guide tube 4 is not included, and the lower stirring blade 3 is a conventional stirring blade, which is the same as the stirring blade in the upper part of the stirring shaft 2.

[0104] The apparatus in Example 1 and Comparative Example 1 was used to ferment high-viscosity materials. For example, the fermentation of Trichoderma reesei to produce cellulase was used as an example. The volume was 120 m 3 The fermentation tank body of Example 1 is compared with that of Comparative Example 1, and the energy consumption of mechanical stirring can be reduced by more than 20%, and the dissolved oxygen value is significantly improved under the same fermentation conditions and ventilation pressure and flow conditions, and the improvement ratio can reach more than 10%, the enzyme activity of cellulase can be increased by 10 to 20 FPU / ml (Comparative Example 1 usually produces enzyme activity of about 50 FPU / ml), and the fermentation cycle can be shortened by 12 to 24 hours, and the shortening ratio is about 15%.

[0105] It can be seen from the above embodiments and comparative examples that the device of the utility model can utilize the centrifugal force of the stirring lower blade during the rotation of the guide tube to better disperse and throw out the gas-liquid mixture flowing out of the guide tube, and at the same time break up the bubbles in the mixed phase, control the size and dispersion of the bubbles, greatly improve the gas-liquid mixing efficiency, and thus improve the dissolved oxygen efficiency; the device utilizes the potential energy of compressed air to drive the kinetic energy of the gas-liquid mixed phase conversion, generate radial driving force on the impeller, reduce the power load of mechanical stirring, achieve energy-saving effect, and save more than 20% of energy consumption; the design form of the upper and lower venturi nozzles of the air ring tube enables the air and the material to fully contact, eliminates the dissolved oxygen dead zone at the bottom of the tank, and improves the uniformity of dissolved oxygen; through the comprehensive adjustment of the device, efficient oxygen transfer and mixing can be achieved, the dissolved oxygen demand of oxygen-consuming microorganisms can be met, and the stirring energy consumption can be effectively reduced, especially in the high-viscosity fermentation system, thereby improving the fermentation production efficiency.

[0106] The applicant declares that the utility model uses the above embodiments to illustrate the detailed device of the utility model, but the utility model is not limited to the above detailed device, that is, it does not mean that the utility model must rely on the above detailed device to be implemented. The technicians in the relevant technical field should understand that any improvement to the utility model, the equivalent replacement of the device of the utility model, the addition of auxiliary devices, the selection of specific methods, etc., all fall within the protection scope and disclosure scope of the utility model.

Claims

1. An oxygen-enriching and energy-saving device for fermentation of high-viscosity materials, characterized in that: The oxygen-enriching and energy-saving device comprises a tank body, a stirring shaft and a plurality of stirring blades arranged on the stirring shaft, a guide tube, an air annular tube and upper and lower layers of Venturi nozzles arranged on the air annular tube; the stirring blade at the bottom of the stirring shaft is a lower stirring blade, the lower stirring blade is a semi-open stirring impeller, the lower part of the lower stirring blade is a guide tube, and the outlet of the guide tube is directly opposite to the center of the lower stirring blade; The air annular tube and the Venturi nozzle are located below the guide tube. The upper and lower layers of Venturi nozzles are respectively an upward nozzle and a downward nozzle, which are located on the upper and lower sides of the air annular tube, and the upward nozzle faces the inlet of the guide tube. The Venturi nozzles are evenly distributed on the circumference of the air annular tube, and the upward nozzle and the downward nozzle are arranged alternately. The upward nozzle is arranged to be inclined upward and inward, and the downward nozzle is arranged to be inclined downward and inward, and the inward inclination directions of the upward nozzle and the downward nozzle are opposite.

2. The oxygen-enhancing and energy-saving device for fermentation of high-viscosity materials according to claim 1, characterized in that: The shape of the tank body includes cylindrical or conical; A stirring motor is arranged at the upper outer portion of the tank body, and the stirring motor is connected to a stirring shaft, and the stirring shaft passes through the top of the tank body and extends to the lower portion of the tank body.

3. The oxygen-enriching and energy-saving device for fermentation of high-viscosity materials according to claim 1, characterized in that: The lower stirring blade is a semi-open large-width impeller. The lower stirring blade is disc-shaped as a whole, including a central part and surrounding blade parts. The blade is welded and attached below the disc plane. The overall diameter of the lower stirring blade is 1.5 to 3 times the diameter of the central part.

4. The oxygen-enriching and energy-saving device for fermentation of high-viscosity materials according to claim 3, characterized in that: The number of blades in the stirring lower blade is 6 to 12, the blades are curved, the angle between the blades and the disc plane is 15 to 45 degrees, and the width of the blades is 1 / 15 to 1 / 5 of the diameter of the central part of the stirring lower blade.

5. The oxygen-enhancing and energy-saving device for fermentation of high-viscosity materials according to claim 3, characterized in that: The guide cylinder is divided into two parts: a main cylinder and a conical inlet. The diameter of the conical inlet gradually decreases until it becomes the same as the diameter of the main cylinder.

6. The oxygen-enhancing and energy-saving device for fermentation of high-viscosity materials according to claim 5, characterized in that: The overall height of the guide tube is 1 / 20 to 1 / 5 of the tank body height, wherein the height of the main cylinder accounts for 1 / 4 to 3 / 4 of the guide tube height; The diameter of the main cylinder in the guide tube is 1 / 10 to 1 / 3 of the inner diameter of the tank body, and the maximum diameter of the conical inlet is 2 to 5 times the diameter of the main cylinder; The diameter of the main cylinder in the guide cylinder is the same as the diameter of the center of the stirring lower blade.

7. The oxygen-enhancing and energy-saving device for fermentation of high-viscosity materials according to claim 1, characterized in that: The air annular tube is connected to the air inlet at the bottom of the tank body, the air inlet at the bottom of the tank body is connected to an air compressor, and the air annular tube is connected to the inlet of each venturi nozzle; The diameter of the air ring tube is 1 / 4 to 3 / 4 of the inner diameter of the tank body, and the tube diameter of the air ring tube is 80 to 250 mm.

8. The oxygen-enhancing and energy-saving device for fermentation of high-viscosity materials according to claim 1, characterized in that: The number of the Venturi nozzles is 4 to 20, and the number of the upward nozzles and the downward nozzles is the same; When the Venturi nozzle is tilted upward or downward, the angle with the horizontal direction is 10 to 60 degrees; The angle between the projection of the Venturi nozzle on the horizontal plane and the radial direction of the air ring tube passing through the inlet of the Venturi nozzle is 10 to 60 degrees.

9. The oxygen-enhancing and energy-saving device for fermentation of high-viscosity materials according to claim 8, characterized in that: The inward tilting direction of the upward nozzle is generally clockwise, and the inward tilting direction of the downward nozzle is generally counterclockwise, or the inward tilting direction of the upward nozzle is generally counterclockwise, and the inward tilting direction of the downward nozzle is generally clockwise.

10. The oxygen-enhancing and energy-saving device for fermentation of high-viscosity materials according to claim 1, characterized in that: A support structure is provided in the tank body, and the support structure is connected to the inner wall of the tank body to support and fix the stirring shaft, the guide cylinder and the air ring tube.

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