Gas-solid countercurrent fluidization heat exchange device

Abstract

The utility model provides a gas-solid countercurrent fluidization heat exchange device. The gas-solid countercurrent fluidization heat exchange device comprises a barrel; a feeding pipe, a flow guide cone and a gas distributor are sequentially arranged in the barrel, the feeding pipe is used for conveying solid particles into the barrel, an upper conical surface is arranged at the upper end of the flow guide cone, a lower conical surface is arranged at the lower end of the flow guide cone, and the upper conical surface is used for enabling the solid particles input by the feeding pipe to disperse and slide downwards; a gas inlet pipe and a gas outlet pipe are arranged on the side wall of the barrel, the gas inlet pipe is used for conveying gas into the gas distributor, the gas distributor is used for guiding the gas to generate downward rotational flow motion, the lower conical surface is used for dispersing the returned gas flowing upwards to flow upwards, and the gas outlet pipe is used for conveying the gas subjected to heat exchange in the barrel to the next procedure; according to the device, gas and solid particles can be subjected to sufficient heat exchange, the heat exchange efficiency is greatly improved, meanwhile, countercurrent movement between the gas and the solid particles can be achieved, the gas flowing speed is increased, and the sectional area of the barrel is greatly reduced.

Description

Technical Field

[0001] The utility model relates to the technical field of gas-solid reaction treatment, and particularly relates to a gas-solid countercurrent fluidized heat exchange device. Background Art

[0002] In industrial production, a large amount of solid small particles with a certain temperature are generated. To recover the heat carried by the solid particles, a heat exchange method with gas can be adopted, and a reverse flow mode of gas phase and solid phase is used. That is, under the action of gravity, the particles move from top to bottom, and the gas moves from bottom to top. In this process, heat exchange occurs between the gas-solid two phases. When the solid particles are descending, they are subject to the downward gravity and the upward drag force exerted by the reversely moving gas. Since the magnitude of the drag force is generally positively correlated with the square of the relative velocity, as the descending speed of the particles increases, the drag force on the particles increases. When the speed increases to a certain extent, the gravity is equal to the drag force, and the speed of the solid particles no longer increases. Therefore, when the gas-solid flow adopts the above method, the speed of the gas cannot be too large, otherwise the particles will change their movement direction and be blown out with the airflow. According to relevant theoretical calculations, under normal pressure, when the gas-solid two phases move countercurrently, the gas phase speed is generally below 0.5 m / s. Since the solid phase density is much greater than the gas phase density, in order to reduce the solid phase temperature to the set temperature, the gas phase flow rate is much greater than the solid phase. Due to the limitation of the gas phase speed, the corresponding gas-solid countercurrent heat exchanger requires a very large cross-sectional area, which affects its application in industry.

[0003] Another common heat exchange method for fine particle heat exchange is fluidized bed heat exchange. In such a device, the particles to be heat-exchanged are in contact with the gas in the fluidized bed. Since the contact between the gas and the particles in the fluidized bed is sufficient, the heat exchange between the gas and the solid is sufficient. However, in such a device, the backmixing between the gas and the solid is intense, the temperature difference between the heat-exchanged gas and solid is very small, and the heat grade of the heat-exchanged gas is low, with low utilization value.

[0004] For example, Patent CN102607297B discloses a device for heat exchange between gas and solid particulate matter, and it is proposed in this technology that raw material and hot flue gas exchange heat during the opposite contact process. Since in this heat exchange process, the gas flow has been flowing and exchanging heat along its original flow direction, and since both the hot flue gas and the raw material have speeds during the flow heat exchange process, the contact time between them is very short during the opposite contact process, resulting in a very low heat exchange efficiency between the raw material and the hot flue gas. Summary of the Utility Model

[0005] In view of this, the purpose of the present utility model is to propose a gas-solid countercurrent fluidized heat exchange device to solve the problems in the prior art that in order to reduce the solid phase temperature to the set temperature, the gas phase flow rate is much greater than the solid phase, and due to the limitation of the gas phase speed, the corresponding gas-solid countercurrent heat exchanger requires a very large cross-sectional area, which affects its application in industry, and the low heat exchange efficiency between the gas phase and the solid phase.

[0006] To achieve the above object, the technical solution of the present utility model is realized as follows:

[0007] A gas-solid countercurrent fluidized heat exchange device, comprising: a cylinder body; an inlet pipe, a flow guiding cone and a gas distributor are sequentially arranged in the cylinder body from top to bottom. The inlet pipe is used for conveying solid particles into the cylinder body. The upper end of the flow guiding cone is provided with an upper conical surface, and the lower end is provided with a lower conical surface. The upper conical surface is used for dispersing and sliding down the solid particles input by the inlet pipe, increasing the contact area between the solid particles and the gas; an air inlet pipe and an air outlet pipe are arranged on the side wall of the cylinder body. The air inlet pipe is located below the gas distributor and is used for conveying gas into the gas distributor. The temperature of the solid particles input by the inlet pipe is higher than the temperature of the gas input by the air inlet pipe. The gas distributor is used for guiding the gas to form a downward swirl. The lower conical surface is used for dispersing and flowing upward the gas flowing upward. The air outlet pipe is located above the flow guiding cone and is used for conveying the gas after heat exchange in the cylinder body to the next process.

[0008] This design enables the gas distributor to form a swirling flow field in the cylinder body. The solid particles entering it are subjected to centrifugal force in addition to gravity, and the centrifugal force is much greater than gravity, which can make the relative velocity between gas and solid very large without changing the moving direction of the solid particles. Therefore, the cross-sectional area of the cylinder body can be greatly reduced. At the same time, this setting makes the gas and solid particles flow countercurrently, making the gas temperature at the air outlet pipe close to the initial temperature of the solid particles, greatly improving the heat exchange efficiency and realizing the effective recovery of the heat of the solid particles.

[0009] Further, the gas distributor is in a circular ring shape. An air outlet is arranged on the outer edge of the gas distributor. The air outlet is used for spraying gas into the cylinder body. A swirl vane is arranged at the air outlet. The swirl vane is inclined. The gas sprayed from the air outlet forms a strong swirl after passing through the swirl vane and flows around. A flow guiding plate is arranged at the upper end of the air outlet. The gas distributor is provided with a through hole. One end of the flow guiding plate close to the through hole is higher than the end far from the through hole. The flow guiding plate and the swirl vane cooperate to make the gas sprayed from the air outlet flow obliquely downward.

[0010] This design can enable the gas and solid particles to conduct sufficient heat exchange, making the gas temperature at the air outlet pipe close to the initial temperature of the solid particles, much higher than the temperature of the solid particles in the silo, greatly improving the heat exchange efficiency and realizing the effective recovery of the heat of the solid particles.

[0011] Further, a silo is arranged at the lower end of the cylinder body. The silo is used for collecting the solid particles falling along the cylinder body.

[0012] This setting facilitates the timely collection of the solid particles after heat exchange.

[0013] Furthermore, the distance between the lower end of the feed pipe and the upper end of the flow guide cone is X1, and the distance between the lower end of the flow guide cone and the upper end of the gas distributor is X2, then X1 > X2.

[0014] This design reduces the penetration of gas in the solid particle layer and improves the heat exchange efficiency.

[0015] Furthermore, the diameter of the feed pipe is X0, 7X0 ≥ X1 ≥ 3X0, 3X0 ≥ X2 ≥ X0.

[0016] It helps to reduce the wear caused by the direct impact of solid particles on the flow guide cone, makes the solid particles more evenly distributed before being dispersed by the flow guide cone, reduces the penetration resistance of gas in the solid particle layer, and improves the gas penetration efficiency and mixing effect.

[0017] Furthermore, the cone angle of the upper conical surface is α, 90° ≥ α ≥ 55°, and the cone angle of the lower conical surface is β, 45° ≥ β ≥ 30°.

[0018] This setting enables the gas to gradually accelerate when leaving the lower conical surface and better mix with the solid particles. A smaller cone angle can produce a stronger acceleration effect, promote the mixing of solid particles and gas, and avoid local accumulation or blockage.

[0019] Furthermore, the projected area of the flow guide cone on the horizontal plane is S1, and the cross-sectional area of the through hole on the horizontal plane is S2, then 1.3S2 ≥ S1 ≥ S2.

[0020] This setting can improve the heat exchange efficiency, and at the same time, avoid excessive obstruction of the gas by the flow guide cone, and promote the mixing and heat exchange of gas and solid particles.

[0021] Furthermore, the diameter of the gas distributor is D1, and the diameter of the cylinder is D2, then 0.8D2 ≥ D1 ≥ 0.6D2.

[0022] This setting can ensure the uniform distribution of gas when entering the cylinder, which helps to reduce the dead zone of gas in the cylinder and promote the contact heat exchange between gas and solid particles.

[0023] Furthermore, the height of the cylinder is h, and the inlet pipe is arranged at the position of 0.5h of the cylinder height.

[0024] This setting can force the gas to flow through a longer path inside the cylinder, improve the contact efficiency between gas and solid particles. At the same time, it also reduces the dead zone formed due to poor gas flow, helps to form a more uniform gas distribution across the entire cross-section of the cylinder, avoids the accumulation of gas at the top or bottom of the cylinder, and improves the contact and heat exchange efficiency between gas and solid particles.

[0025] Furthermore, a filter screen is provided in the air outlet pipe, and the filter screen is used to block solid particles from flowing out of the air outlet pipe.

[0026] By providing a filter screen in the air outlet pipe, solid particles can be prevented from entering downstream equipment and affecting the normal operation of the downstream equipment.

[0027] Compared with the prior art, the gas-solid countercurrent fluidized heat exchange device of the present utility model has the following advantages:

[0028] 1) It can enable full heat exchange between gas and solid particles, making the gas temperature at the air outlet pipe close to the initial temperature of the solid particles, greatly improving the heat exchange efficiency, and effectively recovering the heat of the solid particles;

[0029] 2) The gas distributor can form a swirling flow field in the cylinder. In addition to the gravitational force, the solid particles entering it are also affected by the centrifugal force. When the gas and solid particles move countercurrently, the gas flow rate can be increased, thereby greatly reducing the cross-sectional area of the cylinder. Description of the Drawings

[0030] Figure 1 It is a schematic structural diagram of the gas-solid countercurrent fluidized heat exchange device according to an embodiment of the present utility model;

[0031] Figure 2 It is a schematic dimension diagram of the gas-solid countercurrent fluidized heat exchange device according to an embodiment of the present utility model;

[0032] Figure 3 For Figure 1 It is a schematic structural diagram of the guide cone in

[0033] Figure 4 For Figure 1 It is a top view of the gas distributor in

[0034] Figure 5 For Figure 1 It is a sectional view of the gas distributor in

[0035] Figure 6 It is a schematic diagram of the gas flow in the cylinder according to an embodiment of the present utility model;

[0036] Figure 7 It is a velocity distribution diagram of the gas in the cylinder after passing through the gas distributor according to an embodiment of the present utility model;

[0037] Figure 8 It is a flow field diagram of the gas in the horizontal plane in the cylinder according to an embodiment of the present utility model;

[0038] Figure 9 It is a distribution diagram of the solid particles in the cylinder after heat exchange according to an embodiment of the present utility model;

[0039] Figure 10 This is the gas temperature distribution diagram when the gas exchanges heat with solid particles in the embodiment of the present utility model;

[0040] Figure 11 This is the solid particle temperature distribution diagram when the gas exchanges heat with solid particles in the embodiment of the present utility model.

[0041] Explanation of reference numerals:

[0042] 1, cylinder body; 2, feed pipe; 3, flow guiding cone; 31, upper conical surface; 32, lower conical surface; 4, gas distributor; 41, gas outlet; 42, swirl vane; 43, flow guiding plate; 44, through hole; 5, inlet pipe; 6, outlet pipe; 7, storage bin; 81, first direction; 82, second direction. Detailed implementation manners

[0043] In order to make the above objects, features and advantages of the present utility model more obvious and understandable, the following detailed description of the specific embodiments of the present utility model will be given with reference to the accompanying drawings.

[0044] Embodiment 1

[0045] As Figures 1-11 shown, a gas-solid countercurrent fluidized heat exchange device includes: a cylinder body 1;

[0046] Inside the cylinder body 1, a feed pipe 2, a flow guiding cone 3 and a gas distributor 4 are sequentially arranged from top to bottom. The feed pipe 2 is connected to an external material conveying pipeline and is used to convey high-temperature solid particles into the cylinder body 1. The upper end of the flow guiding cone 3 is provided with an upper conical surface 31, and the lower end is provided with a lower conical surface 32. The upper conical surface 31 is used to disperse the high-temperature solid particles input by the feed pipe 2 and then slide downwards, increasing the contact area between the solid particles and the gas;

[0047] The side wall of the cylinder body 1 is provided with an inlet pipe 5 and an outlet pipe 6. The inlet pipe 5 is located below the gas distributor 4 and is used to convey low-temperature gas into the gas distributor 4. The gas distributor 4 is used to guide the gas to form a downward swirl. The lower conical surface 32 is used to disperse the upward flowing gas and then flow upwards. The outlet pipe 6 is located above the flow guiding cone 3 and is used to convey the high-temperature gas after heat exchange in the cylinder body 1 to the next process.

[0048] Specifically, the flow guide cone 3 is integrally in a spindle-shaped structure. After the solid particles enter the cylinder 1 from the feed pipe 2, they are evenly distributed along the circumference of the device under the action of the flow guide cone 3 and move downward under the action of gravity. The gas flows downward after flowing out of the annular distributor and then flows upward through the through hole 44 in the center of the gas distributor 4. After passing through the flow guide cone 3, the flow direction of the gas deflects to contact the particles countercurrently to complete the heat exchange process. This design enables the gas and solid particles to undergo sufficient heat exchange, making the temperature of the gas at the air outlet 6 close to the initial temperature of the solid particles, greatly improving the heat exchange efficiency, effectively recovering the heat of the solid particles, and the gas distributor 4 can form a swirling flow field in the cylinder 1. When the solid particles entering it are affected by gravity, they are also affected by centrifugal force. When the gas and solid particles move countercurrently, the gas flow rate can be increased, thereby greatly reducing the cross-sectional area of the cylinder 1.

[0049] Preferably, the temperature of the solid particles input by the feed pipe 2 is higher than the temperature of the gas input by the air inlet pipe 5.

[0050] Preferably, the path of the gas flow is the first direction 81, and the path of the solid particle flow is the second direction 82.

[0051] As a preferred example of the present application, a silo 7 is provided at the lower end of the cylinder 1, and the silo 7 is used to collect and store the solid particles falling along the cylinder 1. This setting facilitates the timely collection of the solid particles after heat exchange.

[0052] Preferably, the silo 7 is provided with an automatic discharge port, and the automatic discharge port is connected to an external conveying pipeline. When the solid particles in the silo 7 reach the set weight, they can be timely transported to the outside to ensure the continuous operation of the heat exchange equipment.

[0053] As a preferred example of the present application, the gas distributor 4 is in a circular ring shape. An air outlet 41 is provided at the outer edge of the gas distributor 4, and the air outlet 41 is used to inject gas into the cylinder 1. A swirl vane 42 is provided at the air outlet 41, and the swirl vane 42 is inclined. The gas injected from the air outlet 41 forms a strong swirl after passing through the swirl vane 42 and flows in all directions. A deflector 43 is provided at the upper end of the air outlet 41. A through hole 44 is provided at the center of the gas distributor 4. One end of the deflector 43 close to the through hole 44 is higher than the end far from the through hole 44. The deflector 43 and the swirl vane 42 cooperate to make the gas injected from the air outlet 41 flow obliquely downward.

[0054] The gas distributor 4 described in this application can make the gas flow downward obliquely at a high speed with a strong swirl, collide with the side wall of the cylinder body 1 and then flow back upward. The gas flowing back passes through the through hole 44 in the center of the gas distributor 4 and flows upward to collide with the lower conical surface 32. Under the action of the lower conical surface 32, it deflects and flows downward along the side wall of the cylinder body 1 and falls into the silo 7. During this process, the upward gas and the downward solid particles are in countercurrent contact for heat exchange. This design enables the gas and the solid particles to conduct sufficient heat exchange, making the temperature of the gas at the air outlet pipe 6 close to the initial temperature of the solid particles and much higher than the temperature of the solid particles in the silo 7, greatly improving the efficiency of heat exchange and realizing the effective recovery of the heat of the solid particles.

[0055] During the heat exchange process, the gas ejected by the gas distributor 4 forms an annular flow in the horizontal section. After the solid particles come into contact with the gas, they are thrown towards the side wall of the cylinder body 1 under the action of centrifugal force. After the gas deflects through the lower conical surface 32, it flows downward along the side wall of the heat exchanger, causing the solid particles to flow downward along the side wall of the heat exchanger and be collected and stored by the silo 7. Therefore, very few solid particles flow out from the air outlet pipe 6, realizing the separation of the gas and the solid particles and facilitating the subsequent process to utilize the high-temperature gas.

[0056] As Figure 10 、 Figure 11 The temperature distributions of the gas and the solid particles shown indicate that after the solid particles are heat-exchanged, their temperatures are significantly reduced, and the temperature of the solid particles at the bottom of the cylinder body 1 is lower than the temperature at the air outlet pipe 6. Averaging the temperatures of the gas at the air outlet pipe 6 and the solid particles at the bottom of the cylinder body 1 shows that the temperature at the air outlet pipe 6 is 223 °C, and the temperature of the solid particles at the bottom of the cylinder body 1 is 182 °C. The temperature at the air outlet pipe 6 is higher than the equilibrium temperature and also higher than the temperature of the solid particles at the bottom of the cylinder body 1, achieving the purpose of countercurrent heat exchange.

[0057] As a preferred example of this application, the gas flow rate input by the inlet pipe 5, the solid particle flow rate input by the feed pipe 2, and the angle of the swirl vane 42 can all be adjusted.

[0058] The gas distributor 4 can form a swirl flow field in the cylinder body 1. The solid particles entering it are subject to not only gravity but also centrifugal force, and the magnitude of the centrifugal force can be controlled by the swirl velocity of the gas and the angle of the swirl vane 42. By adjusting the gas flow rate and the angle of the swirl vane 42, the centrifugal force received by the solid particles can be much greater than the gravity they receive. At this time, when the gas and the solid particles move in countercurrent, the gas flow rate will far exceed the flow rate when only under the action of gravity, and the relative movement direction of the solid particles and the gas will change. The gas flow rate can be accelerated to a very high speed, thus greatly reducing the cross-sectional area of the cylinder body 1. At the same time, the circulating flow in the cylinder body 1 can make the heat-exchanged solid particles flow downward along the side wall of the cylinder body 1 and be collected by the silo 7 below.

[0059] As a preferred example of the present application, the distance between the lower end of the feed pipe 2 and the upper end of the diversion cone 3 is X1, and the distance between the lower end of the diversion cone 3 and the upper end of the gas distributor 4 is X2, then X1 > X2.

[0060] Specifically, since X1 is relatively large, the solid particles flowing out of the feed pipe 2 have a certain free-fall space before being dispersed by the diversion cone 3, which helps the solid particles to be preliminarily dispersed in the vertical direction. Subsequently, the solid particles are further evenly dispersed around under the guidance of the diversion cone 3, facilitating efficient heat exchange with the gas. On the other hand, when the gas flows upward through the through-hole 44 in the center of the gas distributor 4, due to X2 being relatively small, the gas can quickly and evenly penetrate the solid particle layer, realizing efficient mixing of the gas and the solid particles. This design reduces the penetration force of the gas in the solid particle layer and improves the heat exchange efficiency.

[0061] As a preferred example of the present application, the diameter of the feed pipe 2 is X0, 7X0 ≥ X1 ≥ 3X0, 3X0 ≥ X2 ≥ X0.

[0062] Specifically, the distance X1 between the lower end of the feed pipe 2 and the upper end of the diversion cone 3 is between 3X0 and 7X0. This range allows sufficient space for the solid particles to be preliminarily dispersed and decelerated after leaving the feed pipe 2, which helps to reduce the wear caused by the direct impact of the solid particles on the diversion cone 3 and makes the distribution of the solid particles more uniform before being dispersed by the diversion cone 3; the distance X2 between the lower end of the diversion cone 3 and the upper end of the gas distributor 4 is between X0 and 3X0. This distance enables the gas to quickly and effectively penetrate the solid particle layer, reducing the penetration resistance of the gas in the solid particle layer and improving the penetration efficiency and mixing effect of the gas. At the same time, since X2 is not less than X0, this ensures a certain space between the gas distributor 4 and the solid particle layer, avoiding blockage caused by the direct impact of the gas on the solid particle layer or wear of the diversion cone 3.

[0063] As a preferred example of the present application, the cone angle of the upper conical surface 31 is α, 90° ≥ α ≥ 55°, and the cone angle of the lower conical surface 32 is β, 45° ≥ β ≥ 30°.

[0064] Specifically, the cone angle α of the upper conical surface 31 is between 90° and 55°. This range allows the solid particles to be gradually dispersed and change the flow direction on the upper conical surface 31. A larger cone angle can provide a smoother transition, reducing the impact and wear of the solid particles on the upper conical surface 31 and promoting the uniform distribution of the solid particles on the upper conical surface 31; the cone angle β of the lower conical surface 32 is between 45° and 30°. This design enables the gas to gradually accelerate and better mix with the solid particles when leaving the lower conical surface 32. A smaller cone angle can produce a stronger acceleration effect, promoting the mixing of the solid particles and the gas and avoiding local accumulation or blockage.

[0065] As a preferred example of the present application, the projected area of the flow guiding cone 3 on the horizontal plane is S1, and the cross-sectional area of the through hole 44 on the horizontal plane is S2, then 1.3S2 ≥ S1 ≥ S2.

[0066] Specifically, such a setting can enable the flow guiding cone 3 to fully guide and disperse the gas, form a certain degree of turbulence, increase the mixing degree of the gas and solid particles, improve the heat exchange efficiency, and at the same time avoid excessive obstruction of the gas by the flow guiding cone 3, and promote the mixing and heat exchange of the gas and solid particles.

[0067] As a preferred example of the present application, the diameter of the gas distributor 4 is D1, and the diameter of the cylinder body 1 is D2, then 0.8D2 ≥ D1 ≥ 0.6D2.

[0068] Specifically, when D1 is within the range of 0.6D2 to 0.8D2, it can ensure that the gas is evenly distributed when entering the cylinder body 1, which helps to reduce the dead zone of the gas in the cylinder body 1 and promote the contact heat exchange between the gas and solid particles.

[0069] As a preferred example of the present application, the height of the heat exchange device is h, and the inlet pipe 5 is arranged at the height of 0.5h of the heat exchange device.

[0070] Specifically, the inlet pipe 5 is located in the middle of the cylinder body 1, and the gas enters from the middle area, which can force the gas to flow through a longer path inside the cylinder body 1, improve the contact efficiency between the gas and solid particles. At the same time, it also reduces the dead zone formed due to poor gas flow, helps to form a more uniform gas distribution across the cross-section of the entire cylinder body 1, avoids the accumulation of gas at the top or bottom of the cylinder body 1, and improves the contact and heat exchange efficiency between the gas and solid particles.

[0071] As a preferred example of the present application, the axes of the feed pipe 2, the flow guiding cone 3, and the gas distributor 4 coincide with the axis of the cylinder body 1.

[0072] Specifically, such a design makes the distribution of solid particles and gas in the cylinder body 1 more uniform, thereby increasing the contact area between them and improving the heat exchange efficiency.

[0073] As a preferred example of the present application, the outlet pipe 6 is provided with a filter screen, and the filter screen is used to block the solid particles from flowing out of the outlet pipe 6.

[0074] Specifically, by providing a filter screen on the outlet pipe 6, it can avoid solid particles from entering downstream equipment and affecting the normal operation of downstream equipment.

[0075] As Figure 9 shown, after heat exchange, the solid particles are mainly concentrated at the bottom of the cylinder body 1. At the upper outlet pipe 6 of the cylinder body 1, the volume fraction of the solid particles is relatively low, below 0.15%.

[0076] The gas-solid countercurrent fluidized heat exchange device described in this application has the following advantages: 1) It can make the gas flow downward at a high speed with a strong swirling flow, collide with the side wall of the cylinder 1 and then flow back upward. The gas flowing back upward flows upward through the through hole 44 in the center of the gas distributor 4 and collides with the lower conical surface 32. Under the action of the lower conical surface 32, it deflects and flows downward along the side wall of the cylinder 1. During this process, the upward gas and the downward solid particles contact countercurrently for heat exchange. This design enables the gas and the solid particles to conduct sufficient heat exchange, making the gas temperature at the gas outlet 6 close to the initial temperature of the solid particles, greatly improving the efficiency of heat exchange and effectively recovering the heat of the solid particles; 2) The gas distributor 4 can form a swirling flow field in the cylinder 1. The solid particles entering it are subjected to the action of centrifugal force in addition to the gravitational force. When the gas and the solid particles move countercurrently, the gas flow rate can be increased, thereby greatly reducing the cross-sectional area of the cylinder 1.

[0077] Although the present utility model is disclosed as above, the present utility model is not limited thereto. Any person skilled in the art can make various changes and modifications without departing from the spirit and scope of the present utility model. Therefore, the protection scope of the present utility model shall be subject to the scope defined by the claims.

Claims

1. A gas-solid countercurrent fluidized heat exchange device, characterized in that: include: A cylinder (1); a feed pipe (2), a guide cone (3) and a gas distributor (4) are arranged in sequence from top to bottom in the cylinder (1); the feed pipe (2) is used to transport solid particles into the cylinder (1); the guide cone (3) is provided with an upper cone surface (31) at the upper end and a lower cone surface (32) at the lower end; the upper cone surface (31) is used to disperse and slide the solid particles input from the feed pipe (2) downward, thereby increasing the contact area between the solid particles and the gas; the side wall of the cylinder (1) is provided with an air inlet pipe (5) and an air outlet pipe (6). The gas pipe (6) is located at the lower side of the gas distributor (4) and is used to transport gas into the gas distributor (4). The temperature of the solid particles input by the feed pipe (2) is higher than the temperature of the gas input by the gas inlet pipe (5). The gas distributor (4) is used to guide the gas to form a downward vortex. The lower cone (32) is used to disperse the upward-flowing gas. The gas outlet pipe (6) is located at the upper side of the guide cone (3) and is used to transport the gas in the cylinder (1) after heat exchange to the next process.

2. The gas-solid countercurrent fluidized heat exchange device according to claim 1, characterized in that: The gas distributor (4) is in the shape of a ring. An air outlet (41) is provided at the outer edge of the gas distributor (4). The air outlet (41) is used to spray gas into the cylinder (1). The air outlet (41) is provided with a swirl plate (42). The swirl plate (42) is inclined. The gas sprayed from the air outlet (41) forms a strong swirl flow after passing through the swirl plate (42) and flows in all directions. A guide plate (43) is provided at the upper end of the air outlet (41). The gas distributor (4) is provided with a through hole (44). The end of the guide plate (43) close to the through hole (44) is higher than the end away from the through hole (44). The guide plate (43) cooperates with the swirl plate (42) to make the gas sprayed from the air outlet (41) flow obliquely downward.

3. The gas-solid countercurrent fluidized heat exchange device according to claim 1, characterized in that: A silo (7) is provided at the lower end of the cylinder (1), and the silo (7) is used to collect solid particles falling along the cylinder (1).

4. The gas-solid countercurrent fluidized heat exchange device according to claim 1, characterized in that: The distance between the lower end of the feed pipe (2) and the upper end of the guide cone (3) is X1, and the distance between the lower end of the guide cone (3) and the upper end of the gas distributor (4) is X2, then X1>X2.

5. The gas-solid countercurrent fluidized heat exchange device according to claim 4, characterized in that: The diameter of the feed pipe (2) is X0, 7X0≥X1≥3X0, 3X0≥X2≥X0.

6. The gas-solid countercurrent fluidized heat exchange device according to claim 1, characterized in that: The cone angle of the upper cone surface (31) is α, 90°≥α≥55°, and the cone angle of the lower cone surface (32) is β, 45°≥β≥30°.

7. The gas-solid countercurrent fluidized heat exchange device according to claim 2, characterized in that: The projection area of ​​the guide cone (3) on the horizontal plane is S1, and the cross-sectional area of ​​the through hole (44) on the horizontal plane is S2, then 1.3S2≥S1≥S2.

8. The gas-solid countercurrent fluidized heat exchange device according to claim 1, characterized in that: The diameter of the gas distributor (4) is D1, and the diameter of the cylinder (1) is D2, then 0.8D2≥D1≥0.6D2.

9. The gas-solid countercurrent fluidized heat exchange device according to claim 1, characterized in that: The height of the cylinder (1) is h, and the air inlet pipe (5) is arranged at a height of 0.5h of the cylinder (1).

10. The gas-solid countercurrent fluidized heat exchange device according to claim 1, characterized in that: The air outlet pipe (6) is provided with a filter screen, and the filter screen is used to prevent solid particles from flowing out of the air outlet pipe (6).

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