CN205948877U - Reactor device - Google Patents

Abstract

The utility model discloses a reactor device, which belongs to the fields of biological engineering, chemical engineering and environmental engineering. The main body of the stirring system of a reactor device of the utility model is composed of multiple sets of radial flow stirrers and multiple sets of axial flow stirrers. The heat transfer device in the tank also has the function of diversion. Through its reasonable arrangement, combined with the diversion effect of the perforated sieve plate on the side of the conical truncated cone and the multiple gas-liquid dispersion of the radial flow agitator, the heat transfer device in the reactor and The flow fields generated by the stirring system are interconnected, and the mass transfer process and the heat transfer process are organically integrated. Arranging air distributors at multiple points in the reaction vessel not only promotes gas-liquid dispersion, but also further strengthens the circulation and mixing of the reaction flow field. The utility model overcomes the problem that the high-strength gas-liquid dispersion and heat removal in large-scale gas-liquid and gas-liquid-solid reactor devices are difficult to meet at the same time, and can realize high-efficiency mass transfer and heat transfer in large-scale gas-liquid and gas-liquid-solid reactors process.

Description

A reactor device

technical field

The utility model relates to a reactor device, which belongs to the fields of biological engineering, chemical engineering and environmental engineering.

Background technique

Gas-liquid two-phase dispersion and mixing are widely used in aerated fermentation, oxidation reaction, hydrogenation reaction, biological aeration and other process units. At present, the devices that can realize gas-liquid and gas-liquid-solid reactions mainly include: bubble towers, air-lift reactors, stirred tank reactors, and aeration tanks. Ventilated stirred tank reactors are widely used in ventilated fermentation processes and biotransformation processes.

Whether it is a chemical reaction involving gas-liquid two-phase or an aerobic biological reaction, the gas-liquid dispersion process is often accompanied by a heat transfer process. In small-scale reactor devices, the heat transfer process often does not become a technical bottleneck. Engineers pay more attention to Gas-liquid dispersion efficiency. However, in the large-scale fermentation process, as the volume of the reactor increases, the heat transfer area that can be installed per unit volume tends to be smaller, which often makes the effective removal of reaction heat (metabolic heat) a technical bottleneck for reactor enlargement. During the high cell density ventilation fermentation process, the exothermic intensity generated by cell metabolism can reach 30kW/m ³ fermentation broth; the heat transfer area required per unit volume even reaches 3.0m ² /m ³ fermentation broth, this high-intensity heat transfer The demand is difficult to meet in conventional large-scale ventilated fermenters.

Common heat transfer devices outside the tank include: ordinary integral jacket, integral jacket with spiral guide belt, semicircular pipe jacket, honeycomb jacket, channel jacket, etc. Common heat transfer devices in the tank include: vertical coils, large spiral coils, spring coils, etc.

Specifically, in small-scale (<10m ³ ) and medium-scale (10-100m ³ ) ventilated bioreactors, in order to meet the high-efficiency heat transfer requirements during the reaction process, jackets are generally installed outside the tank and inside the tank. Set up the coil. Taking a typical medium-scale ventilated fermentation tank as an example, the heat transfer area per unit volume is in the range of 1.2 to 2.0m ² /m ³ fermentation broth. In a large-scale (>100m ³ ) ventilated fermenter, the heat transfer area per unit volume The area is not easy to exceed 2.0m ² /m ³ fermentation broth. As the volume of the reactor increases, the area of the jacket that can be installed outside the tank is very limited, so it is more and more dependent on installing more coils in the tank, resulting in a smaller gap between the coils, which affects the flow of fluid in the tank. Flow rates, mixing, mass transfer and heat transfer efficiencies within.

Although the vertical coils also have the function of baffles, the appropriate number and density of coils are beneficial to the mass transfer and heat transfer process in the tank, but with the increase of the volume of the reactor, the coil device is getting closer and closer to the tank. As the central area extends, the distance between the stirring paddle and the coil tends to be smaller, and the function of an overly wide baffle plate will not be conducive to the dispersion and mixing functions of the agitator; the gap between the coils tends to be smaller, even less than 30-50mm, which is It will seriously affect the effect and uniformity of mass transfer and heat transfer in the tank.

Since the cooling water in the large spiral coil and the spring coil can be completely drained, the steam consumption can be saved during the sterilization process of the fermenter, but when the volume of the reactor increases, the pitch between the coils tends to be smaller , the gap between the coils is even less than 30-50mm, which will lead to different zones formed in the reactor: a fully turbulent zone in the center of the tank, an internal stagnant zone surrounded by spring coils, a large helical coil and a reactor. The mass transfer and heat transfer efficiency in the stagnant zone is low, and the overall flow field in the reactor is highly inhomogeneous.

Due to the large volume of large-scale gas-liquid and gas-liquid-solid reactors, the overall equipment often cannot be transported. Generally, each component of the reactor needs to be manufactured and transported separately, and then processed and assembled on site at the owner's location. Due to the complexity of the stirring problem, the manufacture of the stirring system and the manufacture of the reaction vessel (including the heat transfer device) are often completed by different manufacturers, so it is easy to cause different understandings of mass transfer and heat transfer, resulting in mass transfer and heat transfer in the reactor. The efficiency of the heat transfer process cannot be compromised. At present, the design and manufacturing technology of large-scale gas-liquid and gas-liquid-solid reactors still mainly rely on the experience of various manufacturers, and the design and manufacturing concepts of medium-scale reactors are still used, and there is insufficient understanding of new problems in large-scale reactors. Effective solutions and measures.

Utility model content

In order to solve the above problems, the utility model considers the overall structure of the reactor, cleverly arranges the space position of the heat transfer device, the ventilation pipe and the flow guide element in the reactor, and the space combination of different function stirring paddles, so that the heat transfer device and the The flow field generated by the stirring system is integrated to provide a solution and equipment for high-efficiency mass transfer and heat transfer in large-scale gas-liquid and gas-liquid-solid reactors. The utility model adopts the component composition of the reactor device which is basically the same as that of the ordinary reactor, but effectively optimizes its space structure and combination mode, so that the efficiency of gas-liquid dispersion, heat transfer and mixing is significantly improved, and it has lower power consumption and plays a role The effect of improving reaction performance and saving energy consumption.

The utility model provides a reactor device, which is a large-scale gas-liquid and gas-liquid-solid reactor device suitable for high-efficiency mass transfer and heat transfer, and can also be applied to medium-scale gas-liquid and gas-liquid-solid reactor devices.

The reactor device mainly includes a reaction vessel, a stirring system, a heat transfer device, a flow guiding device, and an air distributor; the main body of the stirring system is composed of multiple sets of radial flow stirrers and multiple sets of axial flow stirrers, The radial flow agitator includes a bottom agitator and 1 to 3 middle radial flow agitators; the heat transfer device installed inside the reaction vessel is composed of multiple groups of cylindrical heat transfer elements arranged coaxially; the air The distributor includes multiple sets of ventilation pipes arranged in different spatial positions in the reaction vessel and porous sieve plates on the side of the truncated cone; The diameter of the lower end surface of the perforated sieve plate on the side of the platform is equal to the diameter of the reaction vessel, and the diameter of the upper end surface is between 0.5 and 1.0D; where D is the diameter of the cylindrical heat transfer element inside the reaction vessel.

In one embodiment, the heat transfer device installed inside the reaction vessel is composed of cylindrical heat transfer elements arranged coaxially.

In one embodiment, the cylindrical heat transfer element may be closely arranged large spiral coils, or may be a built-in honeycomb jacket or channel jacket.

In one embodiment, the ratio of the diameter (D) of the cylindrical heat transfer element to the inner diameter (T) of the reaction vessel is between 0.5 and 0.9.

In one embodiment, the diameter of the large spiral coil is between 30mm and 125mm, and the gap between the coils in the group is between 0mm and 50mm.

In one embodiment, the radial flow agitator in the middle of the mixing system is matched with the perforated sieve plate on the side of the truncated cone one by one, and 1 to 3 pairs are arranged, and the radial flow agitator in the middle is arranged on the perforated sieve plate on the side of the corresponding truncated cone. Directly above.

In one embodiment, the ratio of the diameter (d _M ) of the middle radial flow agitator to the inner diameter (T) of the reaction vessel is between 0.15 and 0.5.

In one embodiment, the radial flow agitator in the stirring system can be a Rushton agitator, an arrow blade disc agitator, a CD-6 agitator, a BT-6 agitator or other radial flow agitators, It can be multiple groups of the same agitator combination, or multiple groups of different agitator combinations.

In one embodiment, the axial flow agitator in the stirring system can be a four-bladed open agitator, a propeller, a three-wide-blade propeller agitator, a four-wide-blade propeller agitator, a three-narrow blade agitator Blade propeller agitators, four narrow blade propeller agitators and other similar axial flow agitators may be a combination of multiple sets of the same agitator, or a combination of multiple sets of different agitators.

In one embodiment, the number of sets of radial flow agitators is between 1 and 3, and the number of sets of axial flow agitators is between 3 and 8 sets.

In one embodiment, the ratio of the diameter (d) of the stirrer to the inner diameter (T) of the reaction vessel is between 0.2 and 0.5.

In one embodiment, the ratio of the diameter (d) of the stirrer to the diameter (D) of the cylindrical heat transfer element is between 0.3 and 0.6.

In one embodiment, different agitator diameters can be the same or different.

In one embodiment, the ratio of the distance (M) between adjacent agitators to the diameter (d) of the agitators is between 1.5 and 3.

In one embodiment, the agitation of the agitation system can be constant speed agitation or stepless speed regulation agitation, and the agitation speed can be determined according to the oxygen consumption rate of the reaction system, or can be controlled by feedback based on the dissolved oxygen value of the reaction system and regulation.

In one embodiment, in the reactor device, the type, spatial position, and diameter of the stirrer cooperate with the installation position of the cylindrical heat transfer element, the diameter of the cylindrical heat transfer element, and the spacing between groups, and the bottom stirring Most of the stirrers near the perforated sieve plate on the side of the central conical truncated are radial flow stirrers, and most of the other stirrers are axial flow stirrers. The group spacing of cylindrical heat transfer elements is an important parameter to control fluid guidance. In the lower part of the reactor, the group spacing (C _B ) should be small, and the spacing should be between 0 and 100mm to increase the heat transfer area and at the same time It has the function of partially isolating the bubbling area and the stirring area, but when it is close to the conical frustum of the perforated sieve plate on the side of the central conical frustum, the distance C _M of the cylindrical heat transfer elements in the middle must be large enough, 0.4-1.6d _M , to The fluid is guided to the bottom of the radial flow agitator in the middle to promote the secondary dispersion of the gas-liquid flow. Above the radial flow agitator in the middle, a multi-layer axial flow agitator can be installed, which can be up-turned or down-pressed, or down-pressed and up-turned agitator can be set from bottom to top device. If it is a combination of the push-down type and the upturned type, the combination matches the gaps between the cylindrical heat transfer element groups one by one and aligns laterally; then the corresponding cylindrical heat transfer element group spacing (C _U ) should be wider, and the distance between them should be between 0.2 and 0.8d _M , so as to facilitate the gas-liquid multiphase flow in the near-wall region to enter the stirring zone and generate a circulating flow, thereby enhancing the gas-liquid mass transfer and heat transfer process.

In one embodiment, when the cylindrical heat transfer element is arranged in the lower half of the reactor, the distance C _B between groups of cylindrical heat transfer elements is between 0 and 100 mm; For the conical frustum of the porous sieve plate on the side, the distance C _M between the cylindrical heat transfer element groups in the middle is 0.4-1.6d _M ; where d _M is the diameter of the radial flow agitator in the middle.

In one embodiment, a multi-layer axial flow agitator is arranged above the middle radial flow agitator, and the distance between the cylindrical heat transfer element groups C _U is between 0.2 and 0.8d _M ; where d _M is the diameter of the radial flow agitator in the middle.

In one embodiment, in the large-scale gas-liquid and gas-liquid-solid reactor device, the stirring shaft can be an integral shaft or a multi-section stirring shaft connected; it can be a solid shaft or a hollow shaft; The installation method of the shaft can be single-span type or multi-point support installation.

In one embodiment, the cylindrical heat transfer element in the reactor also functions as a flow guiding device.

The heat transfer device in the reactor is composed of multiple groups of cylindrical heat transfer elements arranged coaxially, which can increase the heat transfer area and heat transfer efficiency, and also has the function of diversion; the number and spacing of the cylindrical heat transfer elements between groups Closely cooperate with the flow direction of the flow field of the stirring system, so that the fluid forms a circular flow in the tank. When the cylindrical heat transfer element is a large helical coil, the large helical coils in the group are closely arranged, and the gap is between 0 and 30 mm.

In ordinary ventilated fermentation tanks, the tube spacing of the inner coil is relatively large (50-150mm), and the fluid can only ensure effective mass transfer and heat transfer through the gap of the inner coil, but this makes the unit volume installable The heat transfer area is limited, so it is inevitable that there will be multiple stagnation areas in the scale-up of the reactor. The utility model adopts multiple groups of coaxially installed cylindrical heat transfer elements, which increases the installable heat transfer area in the large-scale reactor and improves the heat transfer intensity. At the same time, the cylindrical heat transfer elements also serve as guides Flow device, no stagnation zone in the fermenter, which strengthens the circulation and mixing of gas-liquid mass transfer.

In one embodiment, the plurality of groups of ventilation tubes include a first ventilation tube and a second ventilation tube.

In one embodiment, the first ventilation pipe is arranged directly under the bottom agitator.

The first air pipe is arranged directly under the bottom stirrer, and this installation method can efficiently disperse the air passing through and form fine air bubbles. The bottom stirrer is installed near the lower end surface of the reaction vessel cylinder, the distance (B) from the bottom of the reaction vessel is 0.25-0.5T, the diameter of the bottom stirrer (d _B ) and the diameter of the cylindrical heat transfer element (D) The ratio is 0.3-0.5, and the bottom end surface of a group of cylindrical heat transfer elements at the bottom is lower than the lower end surface of the cylinder body, and the distance from the installation plane of the bottom agitator is between _0.1-0.4dB .

In one embodiment, small holes are evenly distributed above the first air pipe, the diameter of which is between 4mm and 20mm, and the ratio of the total area of the small holes to the cross section of the air pipe is between 0.5 and 1.0. Preferably, several drain holes are arranged at the bottom of the ventilation pipe, and the diameter of the holes is between 4 and 20 mm.

In one embodiment, the second ventilation pipe is arranged between the outer circumference of the cylindrical heat transfer element near the bottom of the reaction vessel and the wall of the reaction vessel.

In one embodiment, small holes are evenly distributed above the second air pipe, the diameter of which is between 4 and 20 mm, and the ratio of the total area of the small holes to the cross section of the air pipe is between 0.2 and 0.5. Several drain holes are arranged at the bottom of the vent pipe, and the hole diameter is between 4 and 20mm.

In one embodiment, 1 to 3 perforated sieve plates on the side of the truncated cone are arranged in the middle of the reaction vessel cylinder of the reactor device, the bottom angle of the truncated cone is between 20° and 60°, and the porosity is between 15° and 40°. %, the hole diameter is between 5 and 30mm.

In one embodiment, the sieve openings of the frustum-conical perforated sieve plate may be arranged in a rectangular arrangement, a square arrangement, a rhombus arrangement, or an equilateral triangle arrangement. The diameter of the lower end surface of the sieve plate is equal to the diameter of the container, and the diameter of the upper end surface is less than or equal to the diameter D of the cylindrical heat transfer element, which may be 0.5-1.0D.

In one embodiment, the distance between the upper end surface of the conical platform of the perforated sieve plate on the side of the truncated cone and the lower end surface of the adjacent cylindrical heat transfer element is between 0.2 and 0.8d _M ; where d _M is the middle The diameter of the radial flow agitator.

In one embodiment, the perforated sieve plate on the side of the truncated cone can be integrated or split to facilitate installation and maintenance. The sieve plate can be directly welded on the wall, or indirectly connected by a support plate. There is a certain gap between the bottom of the sieve plate and the wall to prevent liquid accumulation and facilitate cleaning.

In the space between the second vent pipe and the perforated sieve plate on the side of the conical truncated cone, the effect of gas-liquid dispersion is similar to that of a bubble tower. The bubbles coming out of the second vent pipe collide with each other and coalesce during the upward process. decrease, the bubbles become larger and larger, and the mass transfer efficiency decreases. The purpose of setting a porous sieve plate in the middle of the cylinder is: (1) the sieve holes can re-segment and disperse the large bubbles to reduce the diameter of the bubbles; (2) play a diversion function to guide the gas-liquid two-phase flow to the middle diameter In the suction area of the flow agitator, the bubbles are dispersed twice through the agitator, the diameter of the bubbles is reduced, the velocity of the bubbles is increased, and the gas-liquid dispersion efficiency and mass transfer efficiency are improved.

In one embodiment, the plurality of sets of ventilation pipes also includes a third ventilation pipe, and the third ventilation pipe is installed between the cylindrical heat transfer element on the conical platform of the perforated sieve plate on the side of the truncated cone and the wall of the device. between.

In one embodiment, the radial flow agitator in the middle of the reactor device can be installed at the same level as the lower end surface of the cylindrical heat transfer element above the perforated sieve plate on the side of the conical platform, or it can be higher than the The lower end surface of the cylindrical heat transfer element. At the position between the cylindrical heat transfer element above the conical platform and the reactor wall, a third ventilation pipe can be installed to enhance the ventilation strength and gas-liquid dispersion efficiency of the near wall area of the reactor, and at the same time promote circulation flow, heat transfer and Mixing efficiency. It is also possible not to install the ventilation pipe, and the secondary dispersed gas-liquid two-phase flow or gas-liquid-solid three-phase flow generated by the radial flow agitator in the middle part can utilize the relative position between the lower end surface of the cylindrical heat transfer element and the radial flow agitator in the middle part. The shunt effect generated by the installation position makes a part of the gas-liquid two-phase flow or gas-liquid-solid three-phase flow enter the space between the cylindrical heat transfer element and the reactor wall, and the other part of the two-phase flow or gas-liquid-solid three-phase flow The flow enters the inner area of the cylindrical heat transfer element (stirring zone), so that the heat transfer device in the reactor and the flow field generated by the stirring system communicate with each other, and the mass transfer process and the heat transfer process are organically integrated.

In one embodiment, each ventilation pipe of the reactor device can be installed horizontally, or can maintain a slight slope (0.005-0.01), so as to facilitate the drainage of the liquid in the operation such as cleaning and emptying.

In one embodiment, in the reactor device, the diameter of the second vent pipe and the third vent pipe, the size of the vent hole, and the number can be the same or different; according to the characteristics of the local area in the reactor device, the cycle time depends. The third ventilation pipes in the reactor device can be in a single group or in multiple groups, between 1 and 3 groups. There is a drain hole at the bottom of the vent pipe.

In one embodiment, in the reactor device, the flow guide device also includes a baffle, and the baffle is set to meet the condition of a full baffle, and the number of baffles in different vertical areas in the reactor device can be the same or can be different. The number of baffles is between 4 and 10, and the baffles are installed inside the cylindrical heat transfer element.

In one embodiment, the reaction vessel is thin and tall, and its aspect ratio is between 2.5 and 6. This is beneficial to increase the bubble residence time, increase the installable heat transfer area per unit volume, and is beneficial to mass transfer and heat transfer efficiency.

In one embodiment, the cylindrical part of the reaction vessel may be straight, or partially enlarged at the upper part.

In one embodiment, the material of the reaction vessel may be carbon steel, stainless steel or other high-strength suitable materials. The upper and lower heads of the reaction vessel can be elliptical heads or disc-shaped heads. The upper and lower heads can be arranged with various nozzles, nozzles and attachments according to the needs of the production process. One manhole can be set at the top of the reaction vessel or one manhole at the top and one at the bottom, and a manway ladder can be set in the reactor for installation, cleaning and maintenance.

In one embodiment, the reactor device also includes ancillary equipment, such as manholes, bearing brackets, cylindrical heat transfer element brackets, discharge outlets, feed inlets, feed inlets, inoculation inlets, man ladders, convex Edge flange etc.

In one embodiment, the reactor device further includes an outer jacket, and the outer jacket can be an integral jacket, an integral jacket with a spiral guide belt, a semicircular pipe jacket, a honeycomb jacket , Channel jacket, etc. any one.

The beneficial effects of the utility model:

(1) The reactor device of the present utility model exerts the heat transfer function and flow diversion function of the built-in cylindrical heat transfer element at the same time, and optimizes the space in the reactor with the agitator with different functions in the stirring system, so that the reactor The internal heat transfer device and the flow field generated by the stirring system are integrated together, which not only improves the installable heat transfer area and heat transfer efficiency per unit volume, but also strengthens the gas-liquid dispersion and mass transfer efficiency of the reactor.

(2) The reactor device of this utility model arranges air distributors at multiple points in different spaces, introduces the advantages of bubble towers in local areas, and integrates the gas-liquid flow of the porous sieve plate on the side of the conical frustum and the radial flow agitator in the middle. The secondary dispersion function makes there is no stagnation zone in the reactor, which can overcome the bubble coalescence process in the bubbling zone, and further strengthen the circulation flow and dispersion efficiency of the reaction flow field.

(3) The reactor device of the utility model has the characteristics of high dispersion efficiency, fast heat transfer, and low energy consumption. heat process.

Description of drawings

Figure 1: Schematic diagram of the reactor device; among them, 1 first vent pipe, 2 second vent pipe, 3 bottom stirrer, 4 second stirrer, 5 cylindrical heat transfer element (large spiral coil), 6 Three-layer agitator, 7 first intermediate bearing bracket, 8 perforated sieve plate on the side of conical frustum, 9 middle radial flow agitator, 10 fifth-layer agitator, 11 baffle plate, 12 sixth-layer agitator, 13 second middle Bearing bracket, 14 stirring shaft, 15 frame, 16 drive system, 17 mechanical seal, 18 manhole, 19 first coupling, 20 semicircular pipe jacket, 21 second bearing, 22 second coupling, 23 first Three air pipes, 24 third bearings, 25 barrels, 26 first bearings, 27 outlets, 28 skirts;

Figure 2: Schematic diagram of the perforated sieve plate components on the side of the conical truncated truncated cone; among them, 29 sieve holes and 30 liquid guide holes;

Figure 3: Schematic diagram of the perforated sieve plate on the side of the truncated cone; among them, 8 perforated sieve plates on the side of the truncated cone;

Figure 4: Top view of the internal components of the reaction vessel; among them, 1 first vent pipe, 2 second vent pipe, 5 cylindrical heat transfer element (large spiral coil), 11 baffle plate, 20 semicircular pipe jacket, 25 cylinder , 31 ventilation holes;

Figure 5: Schematic diagram of cylindrical heat transfer element (built-in honeycomb jacket); among them, 32 cooling water inlet and outlet pipes, 33 cylindrical bottom plate, 34 bulging plate;

Figure 6: Schematic diagram of cylindrical heat transfer element (built-in honeycomb jacket);

Figure 7: Schematic diagram of cylindrical heat transfer element (built-in honeycomb jacket);

Fig. 8: Schematic diagram of the flow field in the reactor device, in which, 35 is a stirring zone and 36 is a bubbling zone.

detailed description

Embodiment 1: reactor device

As shown in Figure 1, the reactor device involved in the utility model includes a reaction vessel, a stirring system, a heat transfer device, a flow guiding device, an air distributor and some auxiliary devices.

The reaction vessel is composed of a cylinder body 25 , an upper head, a lower head, and a skirt 28 .

The stirring system is composed of multiple sets of stirrers, stirring shafts 14, bearings, shaft couplings, mechanical seals 17, frame 15 and drive system 16. The multiple sets of agitators include a bottom agitator 3 , a second agitator 4 , a third agitator 6 , a middle radial flow agitator 9 , a fifth agitator 10 , and a sixth agitator 12 . Described bearing has 3, comprises first bearing 26, second bearing 21, the 3rd bearing 24. There are two couplings, including a first coupling 19 and a second coupling 22 .

The heat transfer system is composed of a semicircular pipe jacket 20 outside the tank and a cylindrical heat transfer element 5 .

The flow guiding device is composed of a cylindrical heat transfer element 5 , a perforated sieve plate 8 on the side of the truncated cone, and a baffle plate 11 .

The air distributor is composed of a first air pipe 1 , a second air pipe 2 , a third air pipe 23 and a perforated sieve plate 8 on the side of the truncated cone.

The auxiliary equipment also includes a manhole 18, a first intermediate bearing bracket 7, a second intermediate bearing bracket 13, a discharge port 27, a feed port, a feed port, a ladder, and a flange.

As shown in Figure 1, the large-scale reactor device involved in the utility model has a relatively large height-to-diameter ratio of the reaction vessel, and the upper and lower heads can be elliptical heads or dish-shaped heads, which are used to support the stirring system. The motor, reducer and other devices can thicken and strengthen the head, and can also increase the support strength by installing a reinforcing ring; the support base of the reaction vessel is generally a skirt. The outside of the cylinder 25 in the reaction vessel can also be equipped with a heat transfer device, which can be any one of an integral jacket, an integral jacket with a spiral guide belt, a semicircular pipe jacket, a honeycomb jacket, and a channel jacket. Or a combination of multiple types, the honeycomb jacket and the channel jacket are the best, and the semi-circular pipe jacket is more cost-effective.

The bottom agitator 3 is generally a radial flow agitator, preferably the BT-6 agitator. The diameter (d _B ) of the bottom agitator 3 is between 0.2 and 0.5T, and there is a first ventilation pipe 1 directly below the agitator. , the function of the bottom agitator 3 is to efficiently disperse the incoming air to form small air bubbles. The agitator 3 is installed near the lower end surface of the cylinder, and the distance (B) from the bottom of the reaction vessel is 0.25 to 0.5T. The distance between the installation planes is between 0.1 and 0.4d _B. A plurality of drain holes are arranged at the bottom of the first ventilation pipe, and the diameter of the holes is between 4 and 20 mm.

The bottom-up second and third-layer agitators (4, 6) are axial flow agitators, which can be four-bladed open-type agitators, propellers, three-wide-blade propeller agitators, and four-wide-blade propeller-type agitators. The stirrer, three-narrow-blade propeller stirrer, four-narrow-blade propeller-type stirrer and other similar axial flow stirrers may be a combination of multiple sets of the same stirrer, or a combination of multiple sets of different stirrers. For conventional low-viscosity fermented liquid, it is better to use four wide-bladed propeller type stirrers, the ratio of the diameter (d) of the stirrer to the internal diameter (T) of the reaction vessel is between 0.2～0.5, and the inner coil diameter ( D) The ratio is between 0.3 and 0.6. The stirrer diameters can be the same or different. The ratio of the distance (M) between adjacent stirrers to the diameter (d) of the stirrers is between 1.5 and 3.

The stirring of the stirring system can be constant speed stirring or stepless speed regulating stirring. The stirring speed can be determined according to the oxygen consumption rate of the reaction system, and can also be controlled and adjusted according to the dissolved oxygen value of the reaction system.

The heat transfer device in the reactor is composed of multiple groups of cylindrical heat transfer elements arranged coaxially. The cylindrical heat transfer elements can be closely arranged large spiral coils, or built-in honeycomb jacket or channel type jacket. The number of groups and the heat transfer area of the cylindrical heat transfer elements are determined according to the heat transfer requirements and installation conditions of the actual reaction process.

When the cylindrical heat transfer element is a large spiral coil, the large spiral coils in the group are closely arranged, and the gap is between 0 and 50 mm. The diameter of the large spiral coil is between 30 and 125mm, and the standard seamless steel pipe is generally used, and the outer surface is polished.

The ratio of the diameter (D) of the cylindrical heat transfer element to the inner diameter (T) of the reaction vessel is between 0.5 and 0.9, which can be adjusted according to the heat transfer requirement and the installation space position.

As shown in Figure 1, in the middle part of the cylinder body 25 of the reactor device, a perforated sieve plate 8 on the side of a truncated cone is set, as shown in Figures 2 to 3, the bottom angle of the truncated cone is between 20° and 60°, so that 30° is preferable; the porosity is between 15% and 40%, preferably 25%; the diameter of the sieve holes 29 is between 5mm and 30mm, and the arrangement of the sieve holes 29 is preferably an equilateral triangle arrangement. The perforated sieve plate 8 on the side of the truncated cone can be integrated or split, as long as it is compatible with the manufacturing and installation conditions. The sieve plate can be directly welded on the wall, or indirectly connected with the wall by a support plate. There is a certain gap between the bottom of the sieve plate and the wall, which is called the liquid guide hole 30, to prevent liquid accumulation and facilitate cleaning. The size of the sieve hole varies with the size of the solid phase particles in the reaction system. If the cell or yeast fermentation is carried out, the size of the sieve hole and the liquid guide hole can be smaller. If the fermentation of mold and actinomycetes is carried out, the pore size needs to be larger. more appropriate.

As shown in Figure 4, a second ventilation pipe 2 is arranged between the outer periphery of the cylindrical heat transfer element (large spiral coil) 5 near the bottom of the reaction vessel and the wall, and the top of the second ventilation pipe 2 is evenly distributed with small ventilation holes 31 , the pore diameter is between 4-20mm, preferably 10mm under the condition of conventional low-viscosity fermentation broth, and the ratio of the total area of small holes to the cross-section of the ventilation pipe is between 0.2-0.5, preferably 0.3. Several drain holes are arranged at the bottom of the vent pipe, and the hole diameter is between 4 and 20mm.

As shown in FIGS. 5-7 , the cylindrical heat transfer element in the reaction vessel can also be a built-in honeycomb jacket, which is composed of a cylindrical bottom plate 33 , a swelling plate 34 and a cooling water inlet and outlet pipe 32 . Generally, two flat steel plates (cylindrical bottom plate 33 and bulging plate 34) are connected together by laser welding to form a welding area with a certain geometric shape, and then the bulging plate 34 in other non-welding areas is formed by the bulging forming method. Deformation, thereby forming a closed convex arc-shaped cavity jacket between two steel plates. The cooling water inlet and outlet pipe 32 can be installed on the inside or outside of the cylindrical heat transfer element, preferably installed on the inside. The surface of the cylindrical heat transfer element is polished for easy cleaning and to prevent the risk of contamination.

As shown in Fig. 1 and Fig. 8, the perforated sieve plate 8 on the side of the conical frustum of the reactor device is matched with the radial flow agitator 9 in the middle part one by one, and in this example a pair is provided. The installation position of the middle radial flow agitator 9 can be flush with the lower end surface of the cylindrical heat transfer element on the conical platform, or can be higher than the lower end surface of the cylindrical heat transfer element. At the position between the cylindrical heat transfer element and the wall above the conical platform, a third ventilation pipe 23 is installed to enhance the ventilation strength and gas-liquid dispersion efficiency of the near-wall area, while promoting circulation flow, heat transfer and mixing efficiency. The ratio of the diameter (d _M ) of the middle radial flow agitator 9 to the inner diameter (T) of the reaction vessel is between 0.15 and 0.5, preferably 0.3.

As shown in Figure 1 and Figure 8, the group spacing of cylindrical heat transfer elements is an important parameter to control fluid guidance. In the lower part of the reactor, the group spacing (C _B ) should be small, and the spacing is between 0 and 50mm , to increase the heat transfer area and at the same time to partially isolate the bubbling area 36, but when it is close to the central frustum of a cone, the distance C _M of the cylindrical heat transfer elements in the middle must be large enough, 0.4-1.6d _M , to be able to The fluid is guided to the bottom of the radial flow agitator in the middle to promote the secondary dispersion of the gas-liquid flow. Above the radial flow agitator in the middle, a multi-layer axial flow agitator can be installed, which can be upturned or downpressed, or downpressed and upturned agitator can be set from bottom to top The combined type of the device, the spacing between the cylindrical heat transfer elements (C _U ) between the two should be wider, and the spacing should be between 0.2 and 0.8d _M , so as to facilitate the gas-liquid multiphase flow in the near wall area to enter the stirring Zone 35 and generate circulating flow to enhance gas-liquid mass transfer and heat transfer process.

The stirring shaft 14 can be an integral shaft or a multi-section stirring shaft connected; it can be a solid shaft or a hollow shaft; the stirring shaft can be installed in a single-span type or a multi-point support installation.

The setting of the baffles 11 conforms to the condition of full baffles, and the number of baffles in different vertical areas in the reactor device can be the same or different. The number of baffles is between 4 and 10, and the baffles are installed inside the cylindrical heat transfer element.

Embodiment 2: reactor device

Taking a 200m ³ ventilated fermenter as an example, the effective liquid volume is about 150m ³ , adopt the scheme described in the utility model, as shown in Figure 1, the inner diameter (T) of the cylinder 25 of the reaction vessel is 4000mm, and the height of the cylinder is 14600mm; The upper head and the lower head are both elliptical heads; the outer jacket is a Φ76×3.5 semi-circular tube spirally welded on the outer surface of the container, the pitch of the semi-circular tube is 110mm, and the outer jacket is arranged from the lower end of the cylinder to the liquid level. The heat transfer area of the outer jacket is about 90m ² ; the cylindrical heat transfer element inside the reaction vessel is also used as a flow guide element, which is a tightly wound large spiral coil, using Φ76×3 seamless steel pipe, the outer surface is polished, and the spiral diameter ( D) is 3500mm, the screw pitch is 76mm, the large spiral coils are arranged coaxially, and the heat transfer area is about 358m ² , so the total heat transfer area of the reactor device is 448m ² ; The lower end surface of the group of large spiral coils is flush with the lower end surface of the cylinder, the distance (C _M ) between the large spiral coil groups corresponding to the radial flow agitator 9 in the middle of the reaction vessel is 800mm, and the top of the upper half of the reaction vessel is turned up The spacing (C _U ) between the horizontally corresponding large helical coil groups of the type agitator 12 and the downward pressure agitator 10 combination is 400mm, and the spacing (C _B ) between other large helical coil groups is 51mm; the bottom agitator 3 is BT-6 type radial flow agitator, its diameter (d _B ) is 1300mm, the middle radial flow agitator 9 is BT-6 type, its diameter (d _M ) is 1100mm, the axial flow agitator shares 4 layers, the diameter (d) of which is 1100mm, the distance (B) between the bottom agitator 3 and the bottom of the reaction vessel is 2000mm, the distance (M) between all agitators is 1750mm, and the pressure-down and up-turning agitators are both It is a four-blade propeller agitator with opposite fluid directions.

The diameter of the lower surface of the sieve plate 8 on the side of the conical _frustum is equal to the diameter (T) of the reaction vessel, and the installation position is in the middle of the reactor. The installation space requirements of the orifice plate 8 and the first intermediate bearing bracket 7, the bottom angle of the truncated cone is 30°, the diameter of the sieve hole 29 is 5mm, the porosity is 20%, the arrangement of the sieve holes is an equilateral triangle, and the truncated cone The diameter of the upper end surface is 3000mm, so the height of the truncated cone is 288.7mm. The size of the liquid guide holes 30 is 50×15, and the number is 120, which are evenly distributed on the bottom of the side of the truncated cone. The baffle is installed on the inner side of the large spiral coil, the width is 280mm, the number is 6 pieces, evenly distributed, and the height is 11000mm. The nominal diameters of the first ventilation pipe 1, the second ventilation pipe 2 and the third ventilation pipe 7 of the reactor are DN150, DN100 and DN80 respectively, the centerline diameter of the first ventilation pipe 1 is 600mm, the second ventilation pipe 2 and the second ventilation pipe The centerline diameters of the three ventilation pipes 7 are all 3750 mm, and the intake pressure of the ventilation pipes is 4 atm. Wall thickness of the reaction vessel, driving system 16, stirring shaft 14, coupling, mechanical seal, bearing support, large spiral coil support, sieve plate support on the side of the conical frustum, manhole 18, man ladder and various connecting pipes, etc. The requirements for ventilated fermenters are designed and determined.

Adopting the scheme of the utility model, the heat transfer area can reach 448m ² , the heat transfer area per unit volume is 2.99m ² /m ³ fermentation liquid, there is no stagnation area in the fermentation tank, and the uniformity of mass transfer and heat transfer is significantly better than conventional Ventilated fermenter.

Also taking the ventilated fermenter with a total volume of 200m ³ as an example, the effective liquid volume is about 150m ³ , the conventionally designed ventilated fermenter is equipped with vertical coils, the total heat transfer area is about 250m ² , and the heat transfer per unit volume The area of the fermented liquid is 1.67m ² /m ³ . At this time, the distance between the built-in coils is only 30mm, which has an obvious blocking effect on the fluid. The volume of the stagnation area (or low flow rate area) is about 18m ³ , accounting for the volume of the total liquid. Therefore, the mass transfer and heat transfer efficiency in the vertical coil area are seriously affected, resulting in uneven flow field distribution in the reactor.

Example 3: Cylindrical heat transfer element

Similar to the reactor device described in Example 2, the heat transfer element outside the reaction vessel in Example 2 was replaced with a honeycomb jacket, and the cylindrical heat transfer element inside the reaction vessel was also replaced with a honeycomb jacket. As shown in Figures 5-7, the built-in cylindrical heat transfer element is in the shape of a cylinder without any covering at the upper and lower ends, and it also serves as a heat transfer element and a flow guide element. Wherein the internal diameter of cylindrical bottom plate 33 is 3500mm, and the height of cylindrical bottom plate 33 is adjusted according to the installation position of reactor stirring device, also can refer to the height of large spiral coil in embodiment 2; The thickness of cylindrical bottom plate 33 The nominal thickness of the bulging plate 34 is not less than 1mm, preferably 1.2mm in this embodiment, the diameter of the laser welding spot is 16mm, the spacing is 75mm, and the bulging height is 6mm. The cooling water inlet and outlet pipe 32 is installed inside the honeycomb jacket, and the cylindrical bottom plate 33 is first welded with the cooling water branch pipe on the inside, then connected to the cooling water inlet and outlet pipe 32, and finally leads to the outside of the reaction vessel, preferably by welding.

In this embodiment, the heat transfer area of the honeycomb jacket outside the tank of the reaction vessel can reach 130m ² , the honeycomb jacket inside the tank is arranged coaxially, the heat transfer area is 228m ² , and the liquid volume is about 150m ³ . The volumetric heat transfer area is 2.39m ² /m ³ fermentation broth, although the heat transfer area per unit volume of this example is slightly lower than that of Example 2, it is still much higher than that of conventionally designed fermenters (1.67m ² /m ³ fermentation broth) . Secondly, since the heat transfer coefficient of the honeycomb jacket is 1.3 to 1.6 times that of the large spiral coil, the scheme of using the honeycomb jacket is still better than the large spiral coil. Third, when the honeycomb jacket is used, the surface of the cylindrical heat transfer element in the reactor is smooth, easy to clean, and can greatly reduce the risk of bacterial contamination.

The above-mentioned device form is a preferred example of the utility model, but the form of the utility model is not limited thereto, and modifications are allowed within a certain range.

Although the utility model has been disclosed as above with preferred embodiments, it is not intended to limit the utility model. Any person familiar with this technology can make various changes and modifications without departing from the spirit and scope of the utility model. modification, so the scope of protection of the utility model should be defined by the claims.

Claims (10)

1. A reactor device, characterized in that, the reactor device mainly comprises a reaction vessel, a stirring system, a heat transfer device, a flow guiding device, and an air distributor; the main body of the stirring system is stirred by multiple groups of radial flow A combination of a mixer and multiple sets of axial flow agitators, wherein the radial flow agitator includes a bottom agitator and 1 to 3 middle radial flow agitators; the heat transfer device installed inside the reaction vessel consists of multiple sets of cylinders Shaped heat transfer elements are coaxially arranged; the air distributor includes multiple groups of air pipes arranged in different spatial positions in the reaction vessel and the perforated sieve plate on the side of the truncated cone; the perforated sieve plate on the side of the truncated cone is arranged on the cylinder There are 1 to 3 in the middle of the body; the diameter of the lower end surface of the perforated sieve plate on the side of the truncated cone is equal to the diameter of the reaction vessel, and the diameter of the upper end surface is between 0.5 and 1.0D; where D is the cylindrical heat transfer element inside the reaction vessel diameter of. 2. A kind of reactor device according to claim 1, it is characterized in that, the radial flow agitator in the middle of the stirring system is matched with the perforated sieve plate on the side of the truncated cone one by one, and the radial flow agitator in the middle is in the corresponding cone directly above the perforated frit on the side of the table. 3. A reactor device according to claim 1, characterized in that, the base angle of the truncated cone is between 20° and 60°, the porosity is between 15% and 40%, and the aperture is between 5mm and 30mm. between. 4. a kind of reactor device according to claim 1, is characterized in that, the vertical distance between the conical platform upper end surface of described truncated conical side perforated sieve plate and the lower end surface of adjacent cylindrical heat transfer element on it is at Between 0.2 and 0.8d _M ; where d _M is the diameter of the radial flow agitator in the middle. 5. A kind of reactor device according to claim 1, is characterized in that, described multiple sets of ventilation pipes comprise first ventilation pipe and second ventilation pipe; Described first ventilation pipe is arranged on bottom agitator directly below; The second ventilation pipe is arranged between the outer circumference of the cylindrical heat transfer element near the bottom of the reaction vessel and the wall of the reaction vessel. 6. A reactor device according to claim 5, characterized in that small holes are evenly distributed above the first ventilation pipe, the apertures are between 4 and 20 mm, and the ratio of the total area of the small holes to the cross section of the ventilation pipe is Between 0.5 and 1.0. 7. A kind of reactor device according to claim 1, it is characterized in that, described multiple sets of ventilation pipes also comprise the 3rd ventilation pipe, described 3rd ventilation pipe is installed between the conical platform of perforated sieve plate on the side of conical frustum Between the cylindrical heat transfer element and the wall. 8. A reactor device according to claim 1, characterized in that, when the cylindrical heat transfer element is arranged in the lower half of the reactor, the distance _C between groups of the cylindrical heat transfer element Between 0 and 100mm; when close to the conical frustum of the perforated sieve plate on the side of the central frustum of the cone, the distance C _M between the cylindrical heat transfer element groups in the middle is 0.4 to 1.6d _M ; where d _M is the radial flow stirring in the middle diameter of the device. 9. A kind of reactor device according to claim 1, is characterized in that, the top of described middle radial flow agitator is provided with multilayer axial flow agitator, and the cylindrical heat transfer element between the two The group spacing C _U is between 0.2 and 0.8d _M ; where d _M is the diameter of the radial flow agitator in the middle. 10. A reactor device according to claim 1, characterized in that the ratio of the diameter of the cylindrical heat transfer element to the inner diameter of the reaction vessel is between 0.5 and 0.9.