An energy-saving fluidized bed system

Abstract

An energy-saving fluidized bed system relates to the fluidized bed drying energy-saving technology and the finished product dust-free technology field, including a fluidized bed body, a constant speed drying zone and a speed reduction drying zone are arranged in the fluidized bed body, and an air inlet, a high humidity exhaust port, and a low humidity exhaust port are arranged on the fluidized bed body, characterized in that: the air inlet corresponding to the constant speed drying zone is connected to the constant speed air inlet system, the air inlet corresponding to the speed reduction drying zone is connected to the speed reduction air inlet system, the high humidity exhaust port is connected to an air outlet heat exchange system for heat exchange with fresh air, the outlet of the air outlet heat exchange system for heat exchange with fresh air is connected to the constant speed air inlet system or / and the speed reduction air inlet system, and the outlet of the low humidity exhaust port is connected to the constant speed air inlet system or / and the speed reduction air inlet system. The present invention can make the exhaust heat of the fluidized bed body be utilized to the maximum extent, and reduce the energy consumption of the production line.

Description

Technical Field

[0001] The invention relates to a boiling fluidized bed energy-saving technology and a finished product dust-free technology, in particular to a continuous internal heat exchange fluidized bed technology. Background Art

[0002] Fluidized bed drying technology: fresh air is treated to obtain clean air, and the temperature rises after passing through the heat exchanger to obtain hot process air. Dry cold process air can also be obtained through dehumidification. Fresh air can also be directly used as hot process air or cold process air without treatment and enter the fluidized bed air inlet chamber. After passing through the air distribution mesh plate, heat and mass exchange is carried out in the fluidized bed layer; the original wet material enters the fluidized bed, and the material is fluidized on the air distribution mesh plate under the action of hot or cold process air. The process air is in full contact with the material, which improves the efficiency of heat and mass exchange and promotes the evaporation and separation of water in the material or stable cooling; the material particles form a certain gradient from the inlet to the outlet, and pass through different fluidized bed forms. Continuous drying or batch use can be achieved; after the process air and the material have exchanged heat and mass, they come out of the fluidized bed and pass through the dust removal system, and can be directly discharged to form an open-loop circulation system, and can be connected to the inlet through a closed-loop circulation device to form a closed-loop circulation system. The dust removal system includes but is not limited to a cyclone separator, a bag dust collector, an electrostatic dust collector, a dust discharge valve, a regulating gate, temperature, humidity, pressure and other measurements, and tail gas treatment (including but not limited to a spray tower and a deodorization device). The fluidized bed includes various public forms such as existing vibrating fluidized bed, boiling fluidized bed, internal heat fluidized bed, pulsating fluidized bed, and spouted fluidized bed. The equipment composition varies according to specific needs.

[0003] According to the specific drying characteristics of the material, the fluidized bed requires different process air temperatures and humidity at different positions from the inlet to the outlet, the moisture content of the material will gradually decrease, and the material temperature usually increases from low to high and then to low, achieving economical energy consumption and excellent products. A special control system, internal heat exchange system, air intake system, and process formula can be selected to achieve an excellent combination of technology and equipment. The internal heat exchanger has a better energy-saving effect and a calcination effect, and can realize the following processes: continuous drying and cooling of solid materials and materials with high moisture absorption, continuous preparation of granules and drying of powdered raw materials, continuous drying, calcination, and cooling of crystalline wet materials, and continuous preparation of snowflake-shaped to solid granules from liquid raw materials.

[0004] Characteristics of continuous production: Because it is continuous production, the product process has good repeatability and high production efficiency; it is suitable for use in continuous drying and granulation, and the final product can be dust-free and have excellent performance; for those who do not want manual participation in the intermediate process and prevent pollution, continuous type is the best choice; low energy consumption; compact structure; because the material layer temperature can be low and the safety standard is high, it is also suitable for the treatment of heat-sensitive materials; reliable operation; high evaporation intensity, and the volume is 1 / 15 to 1 / 30 of the spray drying tower; suitable for continuous drying and granulation of sticky materials and highly hygroscopic materials; especially when the output is relatively large, compared with batch equipment, it has absolute advantages in energy consumption and quality.

[0005] During the hot air drying process of wet materials, there are mainly constant-speed drying stage and decreasing-speed drying stage. In the constant-speed drying stage, the air coming out of the fluidized bed carries away more water per unit of drying air and has a relatively high absolute humidity. After gas-solid separation, the heat is difficult to be directly recycled and can be directly discharged. In the decreasing-speed drying stage, the air coming out of the fluidized bed carries away more water per unit of drying air from high to low until it reaches the equilibrium stage with a relatively low absolute humidity. After gas-solid separation, if it is directly discharged, all the heat contained will be lost. The exhaust gas needs to be treated for environmental protection, which increases the pressure on environmental protection. The high-humidity exhaust air in the constant speed section and the front section of the decreasing-speed section of the traditional fluidized bed and the low-humidity exhaust air in the rear section of the decreasing-speed section are usually mixed together, which makes it difficult to utilize the heat contained in the exhaust air.

[0006] After the exhaust gas from traditional fluidized bed drying is separated by the dust removal system, the solid particle size obtained is small and does not meet the finished product particle size range. It usually needs to add liquid for re-dissolution and recrystallization. However, recrystallization will directly result in recrystallization losses. At the same time, the added liquid needs to be repeatedly dried, resulting in an increase in overall energy consumption. The materials collected by the cyclone separator in the traditional dust removal system still contain some materials in the finished product particle size range and excessive moisture content, so they usually need to be returned to the fluidized bed body, resulting in repeated wear of the materials in the cyclone separator, increasing the amount of fine powder in the fluidized bed, and further aggravating the above-mentioned shortcomings of reduced yield and increased energy consumption.

[0007] In the existing fluidized bed drying technology, the wet raw materials can be loose or agglomerated wet materials obtained by centrifuges, filter presses, concentration evaporators, etc. When the wet raw materials are subjected to fluidized bed drying operations, the following disadvantages often occur in the traditional fluidized bed: after the wet materials enter the fluidized bed, there is no time to dry and disperse them, resulting in agglomeration in the bed, sticking to the air distribution mesh plates and the shell wall, causing the phenomenon of fluidization destruction and dead bed. In particular, as the continuous production time increases, the air distribution mesh plates are blocked and cannot be reproduced, and even major accidents such as fire and explosion are prone to occur.

[0008] Patent document ZL200720077144.2 "An Energy-Saving Fluidized Bed" adopts a method of setting a dryer in the exhaust system and setting a replaceable desiccant in the dryer to utilize the heat energy of the exhaust gas. However, the disadvantages are that the desiccant is difficult to select, expensive, and inconvenient to replace. In addition, the desiccant is not sufficient to absorb the moisture in the exhaust gas, and the absorption is prolonged over time, and the absorption capacity becomes smaller and smaller, resulting in difficult to control production conditions and smaller and smaller fluidized bed drying capacity.

[0009] Patent document ZL201220224409.8 "An Energy-Saving Fluidized Bed" adopts the method of directly recycling a part of the exhaust gas to the process air inlet through a reflux pipe. The disadvantage is that the exhaust gas contains a large amount of moisture, which returns to the imported process air, increasing the humidity of the incoming air and reducing the drying capacity. The greater the recycling ratio, the greater the degree of reduction in the drying capacity of the production line, and even leads to an inability to dry.

[0010] Patent document ZL201720223838.6 "A Granulating Drying Energy-Saving System" has heat pipe heat exchange devices installed in the imported process air system and the exhaust system, and uses the heat energy of the exhaust gas to heat the imported process air. The disadvantage is that two sets of heat pipe heat exchange devices need to be installed, resulting in doubling of the investment, halving of the heat exchange efficiency, and doubling of the wind system resistance. The increase in wind system resistance directly determines the increase in system fan power. In addition, due to the presence of fine powder in the exhaust system, a fin-type heat exchanger cannot be used, and the size and investment of the heat pipe heat exchange device between the exhaust systems are increased. After weighing the investment cost-effectiveness, maintenance costs, and fan power operating costs, users feel that it is not cost-effective and give up. Summary of the invention

[0011] The purpose of the present invention is to propose an energy-saving fluidized bed system, which can reduce the exhaust volume of the fluidized bed tail gas, can make full use of the exhaust heat of the fluidized bed exhaust, and the outlet material has no dust flying, so as to achieve the effects of improved environmental protection of the exhaust gas, reduced energy consumption of the production line, no powder in the outlet material, increased material yield, stable and safe operation, high investment cost performance, and low maintenance and operation costs.

[0012] The technical solution to achieve the above-mentioned purpose is: an energy-saving fluidized bed system, including a fluidized bed body, a constant speed drying zone and a speed reduction drying zone are arranged in the fluidized bed body, and an air inlet, a high-humidity exhaust port and a low-humidity exhaust port are arranged on the fluidized bed body, characterized in that: the air inlet corresponding to the constant speed drying zone is connected to the constant speed air inlet system, the air inlet corresponding to the speed reduction drying zone is connected to the speed reduction air inlet system, the high-humidity exhaust port is connected to an air outlet heat exchange system for heat exchange with fresh air, the outlet of the air outlet heat exchange system for heat exchanging fresh air is connected to the constant speed air inlet system or / and the speed reduction air inlet system, and the outlet of the low-humidity exhaust port is connected to the constant speed air inlet system or / and the speed reduction air inlet system.

[0013] Beneficial effects of the present invention:

[0014] The exhaust air from the high-humidity exhaust port passes through the air outlet heat exchange system and is connected to the exhaust port. At this time, the high-humidity and high-temperature exhaust air is cooled and dehumidified through heat exchange, and is beneficial to the environmental protection treatment of subsequent exhaust gas. The fresh air is heated by heat exchange with the air outlet heat exchange system and then input into the fluidized bed body to dry the material. Usually, the heat contained in the high-humidity and high-temperature exhaust air can be utilized by 20-50%, and the heat utilization is considerable. The exhaust air from the low-humidity exhaust port has low humidity and high temperature, so it is directly input into the fluidized bed body to dry the material, and the heat utilization is close to 100%, so that the exhaust heat of the fluidized bed body can be utilized to the maximum extent, and the energy consumption of the production line is reduced.

[0015] As a preferred solution, the outlet of the low-humidity exhaust port is connected to the constant speed section air inlet system, and the outlet of the air outlet heat exchange system for exchanging fresh air is connected to the speed reduction section air inlet system. The low-humidity exhaust port still contains a certain amount of water, which has an impact on the speed reduction drying stage, and can be directly returned to the constant speed drying stage for use. In the speed reduction drying stage, the water content of the process air at the air inlet is required to be as low as possible. Using the high-humidity exhaust port's air outlet heat exchange system to heat fresh air can achieve a better drying effect.

[0016] Furthermore, in order to reduce the discharge temperature of the material and to homogenize and stabilize the material, the fluidized bed body is also provided with a cooling section fluidizing zone near the discharge port, and the air inlet corresponding to the cooling section fluidizing zone is connected to the cooling section air inlet system.

[0017] Furthermore, the upper part of the fluidized bed body is a separation chamber, and a separation chamber partition is provided in the separation chamber, which divides the separation chamber into two cavities. The high-humidity exhaust port is connected to the cavity on the side close to the feed port, and the low-humidity exhaust port is connected to the cavity on the other side.

[0018] The separation chamber partition can better isolate the exhaust from the high-humidity exhaust port and the exhaust from the low-humidity exhaust port to prevent confusion. A better way is to set the separation chamber partition to a movable adjustment type to achieve adjustable exhaust ratios between the high-humidity exhaust port and the low-humidity exhaust port.

[0019] Furthermore, in order to improve the environmental protection of the equipment and at the same time collect the materials in the exhaust of the high-humidity exhaust port and the low-humidity exhaust port and improve the material yield, the fluidized bed system also includes a first dust removal system, a second dust removal system and a conveying system. The high-humidity exhaust port is connected to the air outlet heat exchange system through the first dust removal system, and the low-humidity exhaust port is connected to the constant speed section air inlet system and / or the speed reduction section air inlet system through the second dust removal system. The conveying system is connected to the first dust removal system and the second dust removal system, and the conveying system is used to output the materials collected by the first dust removal system and the second dust removal system.

[0020] Furthermore, the first dust removal system and the second dust removal system can be arranged in the fluidized bed body or in the fluidized bed body, and both can achieve the dust removal effect.

[0021] Furthermore, in order to facilitate the granulation of materials collected by the first dust removal system and the second dust removal system, a mixing granulation system is provided at the feed port of the fluidized bed body, and the discharge end of the conveying system is connected to the feed end of the mixing granulation system, and the materials collected by the first dust removal system and the second dust removal system are conveyed to the mixing granulation system through the conveying system for growth.

[0022] Furthermore, the mixing granulation system includes a blade granulator, which includes a granulator housing and two drive motors. Two blade shafts are arranged in the granulator housing, each drive motor is connected to a blade shaft, and the speed is adjustable. A plurality of multi-leaf blades are installed on the blade shaft. That is, this blade granulator plays the role of continuously and instantly dispersing the imported raw materials and instantly making the imported wet raw materials into small particles, preventing large pieces of material in the imported raw materials or agglomeration in the fluidized bed body, reducing the agglomeration of wet materials in the fluidized bed, and reducing the dust in the fluidized bed.

[0023] The two sets of granulator blades are driven by two granulator motors, and the rotation speed is adjustable, which can form the difference of the speed of the two sets of blades, forming a better granulation effect, which is conducive to the mixed granulation of dust and wet raw materials, and the wet granulation of dust itself after being wetted. On the one hand, it can improve the dispersion effect of wet materials entering the fluidized bed and reduce the possibility of agglomeration. On the other hand, it can make the wet raw materials into small particles and prevent small particles from agglomerating into large agglomerations to obtain small granular finished products.

[0024] Furthermore, in order to make the finished product more uniform and transportable, the discharge port of the fluidized bed body is provided with an outlet material system, which includes a screener and a crusher. The screener is used to screen the material output from the fluidized bed body into large particles and medium particles. The large particles are crushed by the crusher and returned to the fluidized bed body, and the medium particles are used as finished products.

[0025] To make it more uniform, the screener can also be provided with a small particle outlet to return the small particles and a small amount of dust to the fluidized bed.

[0026] Furthermore, the conveying system can add a wetting agent during the transmission process to perform mixing or agglomeration granulation, or can granulate the dust separately and then convey it to the fluidized bed body.

[0027] Furthermore, internal heat exchangers are respectively arranged in the fluidizing chamber of the fluidized bed body, through which heat source and cold source can be introduced, and the flow of the introduced heat source and cold source can be controlled and adjusted.

[0028] Furthermore, a through-hole baffle is arranged below the feed port of the fluidized bed body to form a dry-wet material mixture layer. During feeding, the material first enters the dry-wet material mixture layer and then enters the fluidizing chamber of the fluidized bed body through the through-hole baffle.

[0029] The wet material entering the dry-wet material mixing area is first dispersed and preliminarily dried by the material in the mixing layer, and a relatively high hot air temperature can be used in this area. Sometimes, some large lumps are inevitably produced, resulting in poor fluidization. At this time, a dry-wet material mixing layer is set below the feed inlet in the fluidized bed body. The wet raw material first enters the dry-wet material mixing layer, and then enters the fluidized material layer through the through-hole baffle. Therefore, even if there are lumps, due to the effect of the through-hole baffle, the lumps in the dry-wet material mixing area cannot enter the adjacent fluidized material area, preventing adhesion to the air distribution mesh plate, especially the area with the internal heat exchanger, to avoid jamming the internal heat exchanger and adhering to the internal heat exchanger to produce lumps, resulting in poor fluidization, material friction, material accumulation and heating, and causing fire and explosion accidents. The lumps blocked in the mixing area can be slowly ground due to the effect of the fluidized material during operation, and those that cannot be ground can be regularly shut down for cleaning, thereby ensuring stability during production, thereby achieving the purpose of the present invention.

[0030] Furthermore, the fluidized bed body is composed of a plurality of fluidized beds connected to each other.

[0031] In actual working process, the heat exchange fresh air volume of high humidity exhaust port and the exhaust air volume of low humidity exhaust port are not necessarily equal to the air volume of corresponding air inlet. Inlet bypass can be set at corresponding air inlet to adjust and supplement the air volume.

[0032] To sum up, by adopting the above technical scheme of the present invention, the exhaust volume of the fluidized bed tail gas is reduced during operation, the exhaust heat of the exhaust system is utilized as much as possible, and the materials in the outlet material system are free of dust, thereby achieving the effects of improved environmental protection of exhaust gas, reduced energy consumption of the production line, no powder in the outlet material, increased material yield, stable and safe operation, high investment cost performance, and low maintenance and operating costs. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] Figure 1 It is the system principle diagram of the present invention;

[0034] Figure 2 It is a structural schematic diagram of the fluidized bed body;

[0035] Figure 3 This is the system schematic diagram of the constant speed air inlet system;

[0036] Figure 4 This is the system schematic diagram of the air inlet system in the speed reduction stage;

[0037] Figure 5 This is the system schematic diagram of the cooling section air intake system;

[0038] Figure 6 A system schematic diagram for connecting the first dust removal system, the second dust removal system and the dust conveying system;

[0039] Figure 7 It is the system principle diagram of the mixing granulation system;

[0040] Figure 8 It is a schematic diagram of the top view of the blade granulator;

[0041] Fig. 9 It is a schematic diagram of the vertical structure of a blade granulator;

[0042] Fig.10 This is the system schematic diagram of the fluidized material handling system. DETAILED DESCRIPTION

[0043] First embodiment

[0044] The following preferred configuration equipment composition can be increased or decreased according to specific needs, not just for example

[0045] like Figure 1 As shown: an energy-saving fluidized bed system, including a fluidized bed body 1, a constant speed section air inlet system 2, a speed reduction section air inlet system 3, a first dust removal system 5, a second dust removal system 6 and a conveying system 20 connected to the first dust removal system 5 and the second dust removal system 6.

[0046] like Figure 2 As shown, the fluidized bed body 1 comprises a fluidized bed shell 1.1, on which is provided an artificial feeding port 1.14, a feeding port 1.6, a discharging port 1.7, a high-humidity exhaust port 1.16, a low-humidity exhaust port 1.17, and a row of air inlets 1.21, and in the fluidized bed shell 1.1, an air inlet chamber 1.3, an air distribution mesh plate 1.2, a fluidizing chamber 1.4 and a separation chamber 1.5 are arranged in sequence from bottom to top.

[0047] Preferably, the fluidized bed body 1 may be provided with a return port 1.15 as required. The fluidized bed body 1 may adopt various existing technologies such as existing vibrating fluidized bed, boiling fluidized bed, internal heat fluidized bed, pulsating fluidized bed, spouted fluidized bed, etc. The equipment composition may be adjusted according to specific process requirements, and additions and subtractions may be made within the above composition range.

[0048] Preferably, a separation chamber partition 1.12 is provided in the middle of the separation chamber 1.5 of the fluidized bed body 1, which can better isolate the high-humidity exhaust port 1.16 and the low-humidity exhaust port 1.17. The separation chamber 1.5 is divided into two cavities by the separation chamber partition 1.12, the high-humidity exhaust port 1.16 is connected to the cavity on the side close to the feed port 1.6, and the low-humidity exhaust port 1.17 is connected to the cavity on the other side. More preferably, the separation chamber partition 1.12 can be set as a movable adjustable installation structure that can be adjusted to both sides, for adjusting the exhaust ratio of the high-humidity exhaust port 1.16 and the low-humidity exhaust port 1.17.

[0049] Preferably, an internal heat exchanger 1.11 is provided in the fluidizing chamber 1.4 of the fluidized bed body 1. A heat source or a cold source is introduced into the internal heat exchanger 1.11 as required, and flow regulation is provided for the delivery of the heat source and the cold source.

[0050] Preferably, a through-hole baffle 1.13 is arranged below the feed inlet 1.6 of the fluidized bed body 1 to form a dry-wet material mixture layer. The through-hole baffle structure is described in detail in the patent document of an internal heat exchange fluidized bed dryer (2018220840814), which will not be repeated here.

[0051] The fluidized bed shell 1.1 is divided into a constant speed drying zone 1.18 and a speed reduction drying zone 1.19 from the feed port 1.6 to the discharge port 1.7. The air inlet 1.21 corresponding to the constant speed drying zone 1.18 is connected to the constant speed air inlet system 2, and the air inlet corresponding to the speed reduction drying zone 1.19 is connected to the speed reduction air inlet system 3.

[0052] The high-humidity exhaust outlet 1.16 is connected to the outlet heat exchange system 25 for fresh air heat exchange through the first dust removal system 5, and the outlet of the heat-exchanged fresh air of the outlet heat exchange system 25 is connected to the air inlet of the constant-speed section air inlet system 2 and / or the speed reduction section air inlet system 3, and the low-humidity exhaust outlet 1.17 is connected to the air inlet of the constant-speed section air inlet system 2 and / or the speed reduction section air inlet system 3 through the second dust removal system 6; as a preferred scheme of this embodiment, that is, the scheme illustrated in this embodiment, the outlet of the low-humidity exhaust outlet 1.17 is connected to the air inlet of the constant-speed section air inlet system 2 through the second dust removal system 6, and the outlet of the heat-exchanged fresh air of the outlet heat exchange system 25 is connected to the air inlet of the speed reduction section air inlet system 3.

[0053] Preferably, a cooling section fluidizing zone 1.20 is arranged between the side of the speed reduction section drying zone 1.19 in the fluidized bed body 1 away from the constant speed section drying zone 1.18 and the discharge port 1.7, and the air inlet corresponding to the cooling fluidizing zone 1.20 is connected to the cooling section air inlet system 4.

[0054] As a preferred configuration, the air outlet heat exchange system 25 includes an induced draft fan 7, an exhaust gas heat exchanger 8, and an exhaust gas environmental protection system 9 connected to the exhaust port of the first dust removal system 5. The induced draft fan 7, the exhaust gas heat exchanger 8, and the exhaust gas environmental protection system 9 are connected in series with each other. The fresh air is transported to the speed reduction section air inlet system 3 after heat exchange with the exhaust gas heat exchanger 8. The exhaust gas heat exchanger 8 can be a shell and tube fin heat exchanger or a plate heat exchanger. The exhaust gas after heat exchange is treated by the exhaust gas environmental protection system 9 (the exhaust gas environmental protection system 9 can adopt water dust removal equipment, plasma deodorization equipment, electrostatic dust removal equipment, etc. commonly used by technical personnel in this field) and then connected to the exhaust port.

[0055] like Figure 1 As shown, in the actual working process, the exhaust volume of the high-humidity exhaust port 1.16, the exhaust volume of the low-humidity exhaust port 1.17 and the air inlet volume of the constant speed section air inlet 2 and the speed reduction section air inlet 3 are not necessarily the same. Therefore, a hot process air inlet bypass 19 is also connected to the air inlet of the constant speed section air inlet system 2 or the speed reduction section air inlet system.

[0056] In order to facilitate the granulation of the material conveyed by the conveying system 20 , a mixing granulation system 16 is arranged at the feed inlet 1 . 6 of the fluidized bed body 1 .

[0057] like Figure 7 As shown, as a preferred configuration of this embodiment, the mixing granulation system 16 includes a wet material classification device 16.1 (the wet material classification device 16.1 adopts but is not limited to a sifter), a large wet granule processing device 16.2 (the large wet granule processing device 16.2 adopts but is not limited to a dissolving tank, and the dissolving tank is used to dissolve large granules), a dry-wet material mixer 16.3, and a blade granulator 16.4; the wet material classification device 16.1 is provided with a large wet granule discharge port and a small wet granule discharge port, the large wet granule discharge port 16.1 is connected to the large wet granule processing device 16.2, the small wet granule discharge port is connected to the dry-wet material mixer 16.3, and the discharge port of the dry-wet material mixer 16.3 is connected to the feed port 1.6 of the fluidized bed body 1 through the blade granulator 16.4.

[0058] like Figure 8 , 9 As shown, the blade granulator 16.4 can achieve the effect of instantly breaking up and granulating the wet raw materials, and specifically comprises a granulator housing 16.41 and two drive motors 16.42. The upper end of the granulator housing 16.1 is provided with a feed port, and the lower end is provided with a discharge port. Two blade shafts 16.43 arranged side by side and in parallel are rotatably installed in the granulator housing 16.1. Each drive motor 16.42 is connected to a blade shaft 16.43 by transmission. A plurality of multi-leaf blades 16.44 are respectively installed on the blade shafts 16.43. The multi-leaf blades 16.44 are arranged with a plurality of blades along the circumferential direction. The multi-leaf blades 16.44 on the two blade shafts 16.436 are staggered and partially overlapped.

[0059] When the blade granulator 16.4 is working, it is driven by two driving motors 16.42, and the multi-leaf blades 16.44 rotate around the corresponding blade shafts 16.43, and the rotation speed is adjustable. The wet raw material or the dry and wet raw material enters from the feed port of the blade granulator 16.4, and is discharged from the discharge port after granulation is completed.

[0060] like Figure 1 , 10 As shown, the discharge port 1.7 of the fluidized bed shell 1.1 is equipped with an outlet material system 17. As a preferred configuration, the outlet material system 17 includes a screener 17.2 and a crusher 17.3. A conveying mechanism 17.1 is connected between the discharge port 1.7 of the fluidized bed shell 1.1 and the feed port of the screener 17.2. The conveying mechanism 17.1 conveys the material to the screener 17.2. The screener 17.2 processes the material to obtain large particles, medium particles and small particles. The large particles are crushed by the crusher 17.3 and the small particles are finely powdered and input into the fluidized bed body 1 through the return port 1.15. The outlet material system 17 can also be further equipped with a finished product conveyor 17.4, a finished product bin 17.5 and a packer 17.6. The medium particles are used as finished products and are conveyed to the finished product bin 17.5 by the finished product conveyor 17.4 and finally packaged by the packer 17.6. The composition of the outlet material system 17 is relatively flexible and diverse, for example, the screener 17.2 can be a type of two outlets, three outlets, four outlets, etc. When the material particle size requirement is general, no screening is required.

[0061] During the transmission process, the conveying system 20 can add a wetting agent to perform mixing or agglomeration granulation. The dust can also be granulated separately and then conveyed to the fluidized bed body 1, or it can enter the mixing granulation system 1. When the dust can be granulated during the transportation process, or granulated separately, the mixing granulation system 16 may not be used in the process of the present invention.

[0062] like Figure 3 As shown, as a preferred configuration of this embodiment, the constant speed section air intake system 2 includes a hot process air filter 2.1 and a hot process air intake fan 2.2 which are interconnected. The exhaust air from the low humidity exhaust port 1.17 is filtered by the second dust removal system 6 and then input into the hot process air filter 2.1 for filtration. Then, it is input into the air intake 1.21 corresponding to the constant speed section drying area 1.18 through the hot process air intake fan 2.2 and the hot process air regulating valve 2.4. As a further preferred embodiment of this embodiment, the constant speed section air intake system 2 also includes a hot process air heat exchanger 2.3 which is connected in series to the pipeline of the constant speed section air intake system. The temperature of the hot process air is further increased by the hot process air heat exchanger 2.3. A plurality of air intakes 1.21 corresponding to the constant speed section air intake system 2 can be provided, and the temperature, pressure, air volume, etc. of each air intake can be adjusted according to process requirements.

[0063] like Figure 4As shown, as a preferred configuration of this embodiment, the speed reduction section air intake system 3 includes a medium-temperature process air filter 3.1 and a medium-temperature process air intake fan 3.2 that are interconnected. The fresh air after heat exchange with the exhaust gas heat exchanger 8 is filtered by the medium-temperature process air filter 3.1 and then input into the air inlet 1.21 corresponding to the speed reduction section drying area 1.19 through the medium-temperature process air intake fan 3.2. As a further preference of this embodiment, the speed reduction section air inlet system 3 also includes a medium-temperature process air heat exchanger 3.3 connected in series to the speed reduction section air inlet system pipeline, and the medium-temperature process air heat exchanger 3.3 is connected in series to the output end of the medium-temperature process air inlet fan 3.2. A part of the medium-temperature process air output by the medium-temperature process air inlet fan 3.2 is transported to the air inlet 1.21 on the side of the cooling section fluidizing zone 1.20 corresponding to the speed reduction section drying zone 1.19 through the second medium-temperature process air regulating valve 3.5, and the other part is transported to the air inlet 1.21 on the side of the constant speed section drying zone 1.18 corresponding to the speed reduction section drying zone 1.19 through the medium-temperature process air heat exchanger 3.3 and the first medium-temperature process air regulating valve 3.4.

[0064] like Figure 5 As shown, as a preferred configuration of this embodiment, the cooling section air intake system 4 includes a cold process air filter 4.1 and a cold process air intake fan 4.3 connected to each other. After being filtered by the cold process air filter 4.1, the air is input into the air inlet 1.21 corresponding to the fluidizing area 1.20 of the cooling section through the cold process air intake fan 4.3 and the cold process air regulating valve 4.5. As a further improvement of this embodiment, the cooling section air intake system 4 also includes a cold process air temperature and humidity regulating device 4.2 and a cold process air heat exchanger 4.4 connected in series to the pipeline of the cooling section air intake system 4. The cold process air temperature and humidity regulating device 4.2 is used to adjust the temperature and humidity of the cold process air. The cold process air heat exchanger 4.4 is connected in series to the output end of the cold process air intake fan 4.3 to re-cool the air output by the cold process air intake fan 4.3 to offset the temperature increase of the intake air by the cold process air intake fan 4.3.

[0065] like Figure 6 As shown, as a preferred configuration of this embodiment, the second dust removal system 6 includes a first cyclone dust collector 6.1 and a first bag dust collector 6.2, the inlet end of the first cyclone dust collector 6.1 is connected to the low-humidity exhaust port 1.17, the outlet is connected to the first bag dust collector 6.2, and the outlet of the first bag dust collector 6.2 is connected to the inlet of the hot process air filter 2.1.

[0066] As a preferred configuration of this embodiment, the first dust removal system 5 includes a second cyclone dust collector 5.1 and a second bag dust collector 5.2, the inlet end of the second cyclone dust collector 5.1 is connected to the high-humidity exhaust port 1.16, the outlet is connected to the second bag dust collector 5.2, and the outlet of the second bag dust collector 5.2 is connected to the induced draft fan 7.

[0067] like Figure 6 As shown, examples of common optional components of the conveying system 20 include: a gas-dust separator 10 and a dust conveying pipe 11. The air outlet of the gas-dust separator 10 can be connected to the air outlet of the first dust removal system 5. The dust conveying pipe 11 is arranged behind the bottom dust outlets of the first bag-type dust collector 6.2 and the second bag-type dust collector 5.2. One end of the dust conveying pipe 11 is connected to the feed port of the gas-dust separator 10, and the other end is connected to a dust conveying fan 12. A heater 13 is also connected in series to the outlet end of the dust conveying fan 12 for heating the conveying air to prevent the material from absorbing moisture and sticking to the pipe. The dust outlets at the bottom of the first bag-type dust collector 6.2 and the second bag-type dust collector 6.1 are respectively connected to the dust conveying pipe 11.

[0068] The ash outlets of the first cyclone dust collector 6.1 and the second cyclone dust collector 5.1 are respectively connected to dust conveyors 14, ash discharge valves 15 are respectively connected between the dust conveyors and the ash outlets of the first cyclone dust collector 6.1 and the second cyclone dust collector 5.1, and the discharge ends of the dust conveyors 14 are respectively connected to dry and wet material mixers 16.3.

[0069] Working process of the present invention:

[0070] The fluidized bed body 1 has three types of process air, namely, constant speed section air inlet, speed reduction section air inlet and cold process air inlet. The constant speed section air inlet is equipped with a hot process air inlet bypass. Each process air passes through the air inlet chamber 1.3 and the air distribution mesh plate 1.2 and enters the fluidizing chamber 1.4 to exchange heat and mass with the material, and then is input into the second dust removal system 6 and the first dust removal system 5 for dust removal.

[0071] In order to facilitate the collection and granulation of materials in the dust conveying system 20, a mixing and granulating system 16 is provided. The wet raw materials are granulated by the mixing and granulating system 16 and then enter the feed port 1.6 of the fluidized bed body 1. Specifically, the wet raw materials are classified by the wet material classification device 16.1, and the large particles enter the large wet particle processing device 16.2 for processing. The qualified wet materials and the dry materials conveyed by the conveying system 20 enter the dry-wet material mixer 16.3 for mixing, and then enter the blade granulator 16.4 for granulation and then enter the fluidized bed body 1, which can achieve the effect of instantly breaking up and granulating the wet raw materials, and the materials are fluidized under the action of various process air;

[0072] After the process air and the material have exchanged heat and mass, they come out of the fluidized bed and enter the first dust removal system 5 and the second dust removal system 6 respectively. The second dust removal system 6 removes dust, and the exhaust port of the second dust removal system 6 is connected to the inlet of the constant speed air inlet system 2, which can reduce the exhaust gas volume by nearly half. At the same time, all the heat contained in the second dust removal system 6 can be utilized, the environmental protection of the exhaust gas is improved, and the energy consumption of the production line is reduced. The exhaust air of the first dust removal system 5 can be directly discharged.

[0073] The materials separated by the first dust removal system 5 and the second dust removal system 6 are transported to the mixing granulation system 16 by the conveying system 20 for growing and then enter the fluidized bed body 1 without adding water for re-dissolution, so that the materials in the outlet material system are free of dust, the material yield is improved, the powder amount in the fluidized bed body is reduced, and the operation is stable and safe.

[0074] The present embodiment is also provided with an outlet material system 17. The output material of the fluidized bed shell 1.1 is first conveyed to the sifter 17.2 by the conveying mechanism 17.1, and then processed by the sifter 17.2 to obtain large particles, medium particles and small particles. The large particles are crushed by the crusher 17.3 and the fine powder of the small particles are input into the fluidized bed body 1 through the return port 1.15. The medium particles are used as finished products and are conveyed to the finished product bin 17.5 by the finished product conveyor 17.4, and finally packaged by the packager 17.6.

[0075] Second embodiment

[0076] The difference between the second embodiment and the first embodiment is that the fluidized bed body in the first embodiment is composed of a plurality of fluidized beds connected to each other.

[0077] The terms in the above implementation modes and arrangements of the present invention are all prior art.

Claims

1. A fluidized bed system, comprising a fluidized bed body, a constant speed drying zone and a speed reduction drying zone are arranged in the fluidized bed body, an air inlet, a high humidity exhaust port, and a low humidity exhaust port are arranged on the fluidized bed body, characterized in that: The air inlet corresponding to the constant speed drying zone is connected to the constant speed air inlet system, the air inlet corresponding to the speed reduction drying zone is connected to the speed reduction air inlet system, the high humidity exhaust port is connected to the air outlet heat exchange system for exchanging heat with fresh air, the outlet of the air outlet heat exchange system for exchanging heat with fresh air is connected to the speed reduction air inlet system, and the outlet of the low humidity exhaust port is connected to the constant speed air inlet system; The fluidized bed body is also provided with a cooling section fluidizing zone near the discharge port, and the air inlet corresponding to the cooling section fluidizing zone is connected to the cooling section air inlet system; The fluidized bed system further includes a first dust removal system, a second dust removal system and a conveying system, wherein the high-humidity exhaust port is connected to the air outlet heat exchange system through the first dust removal system, and the low-humidity exhaust port is connected to the speed reduction section air inlet system through the second dust removal system, and the conveying system is connected to the first dust removal system and the second dust removal system, and the conveying system is used to output the materials collected by the first dust removal system and the second dust removal system; The constant speed section air intake system includes a hot process air filter and a hot process air intake fan connected to each other. The exhaust air from the low humidity exhaust port is dusted by the second dust removal system and then input into the hot process air filter for filtration. Then, it is input into the air intake corresponding to the constant speed section drying area through the hot process air intake fan and the hot process air regulating valve. The constant speed section air intake system also includes a hot process air heat exchanger connected in series to the pipeline of the constant speed section air intake system, and the temperature of the hot process air is further increased by the hot process air heat exchanger. The deceleration section air intake system includes a medium-temperature process air filter and a medium-temperature process air intake fan which are interconnected. The fresh air after heat exchange with the tail gas heat exchanger is filtered through the medium-temperature process air filter and then input into the air inlet corresponding to the deceleration section drying zone through the medium-temperature process air intake fan. The deceleration section air intake system also includes a medium-temperature process air heat exchanger connected in series to the pipeline of the deceleration section air intake system. The medium-temperature process air heat exchanger is connected in series to the output end of the medium-temperature process air intake fan. A part of the medium-temperature process air output by the medium-temperature process air intake fan is transported to the air inlet corresponding to the deceleration section drying zone on the side close to the cooling section fluidizing zone through the second medium-temperature process air regulating valve, and the other part is transported to the air inlet corresponding to the deceleration section drying zone on the side close to the constant speed section drying zone through the medium-temperature process air heat exchanger and the first medium-temperature process air regulating valve. The cooling section air intake system includes a cold process air filter and a cold process air intake fan which are connected to each other. After being filtered by the cold process air filter, the air is input into the air inlet corresponding to the fluidizing area of ​​the cooling section through the cold process air intake fan and the cold process air regulating valve. The cooling section air intake system also includes a cold process air temperature and humidity regulating device and a cold process air heat exchanger which are serially connected to the cooling section air intake system pipeline. The cold process air temperature and humidity regulating device is used to regulate the temperature and humidity of the cold process air. The cold process air heat exchanger is serially connected to the output end of the cold process air intake fan and is used to re-cool the air output by the cold process air intake fan to offset the temperature increase of the intake air by the cold process air intake fan. The upper part of the fluidized bed body is a separation chamber, and a movable separation chamber partition is provided in the separation chamber. The exhaust ratio of the high-humidity exhaust port and the low-humidity exhaust port can be adjusted through the separation chamber partition. The separation chamber is divided into two cavities by the separation chamber partition. The high-humidity exhaust port is connected to the cavity on the side close to the feed port, and the low-humidity exhaust port is connected to the cavity on the other side.

2. A fluidized bed system according to claim 1, characterized in that: The feed inlet of the fluidized bed body is provided with a mixing granulation system, and the discharge end of the conveying system is connected with the feed end of the mixing granulation system.

3. A fluidized bed system according to claim 2, characterized in that: The mixing granulation system includes a blade granulator, which includes a granulator housing and two drive motors. Two blade shafts are arranged in the granulator housing. Each drive motor is connected to a blade shaft and has an adjustable speed. A plurality of multi-leaf blades are installed on the blade shaft.

4. A fluidized bed system according to claim 1, characterized in that: The outlet of the fluidized bed body is provided with an outlet material system, which includes a screener and a crusher. The screener is used to screen the material output from the fluidized bed body into large particles and medium particles. The large particles are crushed by the crusher and returned to the fluidized bed body, and the medium particles are used as finished products.

5. A fluidized bed system according to claim 1, characterized in that: The conveying system adds wetting agents during the transmission process to perform mixing or agglomeration and granulation.

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