CN215063241U - Energy-saving fluidized bed system - Google Patents

Abstract

The utility model provides an energy-conserving fluidized bed system, relates to fluidized bed drying energy-saving technology and finished product dustless technical field, including the fluidized bed main part, be provided with constant speed section drying area and deceleration section drying area in the fluidized bed main part, be provided with air intake, high wet air exit, low wet air exit in the fluidized bed main part, its characterized in that: the air inlet corresponding to the constant-speed section drying area is connected with a constant-speed section air inlet system, the air inlet corresponding to the speed reduction section drying area is correspondingly connected with a speed reduction section air inlet system, the high-humidity air outlet is connected with an air outlet heat exchange system for exchanging heat with fresh air, the outlet of the fresh air exchanged by the air outlet heat exchange system is connected with the constant-speed section air inlet system or/and the speed reduction section air inlet system, and the outlet of the low-humidity air outlet is connected with the constant-speed section air inlet system or/and the speed reduction section air inlet system. The utility model discloses the heat of airing exhaust that can make the fluidized bed main part can utilize to the utmost extent, and the production line energy consumption reduces.

Description

Energy-saving fluidized bed system

Technical Field

The utility model relates to a boiling fluidized bed energy-saving technology and finished product dustless technical field, in particular to continuous type internal heat transfer fluidized bed technical field.

Background

Fluidized bed drying technology: fresh air is treated to obtain clean air, the temperature of the clean air rises after passing through a heat exchanger to obtain hot process air, dry cold process air can also be obtained through dehumidification, the fresh air can also be directly used as the hot process air or the cold process air without being treated and enters an air inlet chamber of the fluidized bed, and heat and mass exchange is carried out in the fluidized bed after passing through an air distribution screen plate; the original wet material enters the fluidized bed, the material forms fluidization on the air distribution net plate under the action of hot or cold process air, the process air is fully contacted with the material, the heat and mass exchange efficiency is improved, and the moisture in the material is promoted to be evaporated and separated or stably cooled; the material particles form a certain gradient from an inlet to an outlet, and can be continuously dried or used in batches through different fluidized bed forms; the process air and the materials are subjected to heat and mass exchange, then come out of the fluidized bed and pass through a dust removal system, and can be directly emptied to form an open-circuit circulating system, and can be connected to an inlet through a closed-circuit circulating device to form a closed-circuit circulating system, the dust removal system comprises a cyclone separator, a bag-type dust collector, an electrostatic dust collector, a dust discharging valve, an adjusting door, a temperature, humidity, pressure and the like, and tail gas treatment (including a spray tower and a smell removal device), the fluidized bed comprises various disclosed forms such as the existing vibrating fluidized bed, a boiling fluidized bed, an internal heating fluidized bed, a pulsating fluidized bed, a spouted fluidized bed and the like, and the equipment composition is different according to specific needs.

According to the specific drying characteristics of the materials, the fluidized bed has different process air temperatures and humidities from an inlet to an outlet, the required process air temperatures and humidities at different positions are different, the water content of the materials can be gradually reduced, the material temperature is usually from low to high and then low, economic energy consumption and excellent products are realized, a special control system, an internal heat exchange system, an air inlet system and a process formula can be selected and matched, the excellent combination of the technology and equipment is realized, the energy-saving effect of the internal heat exchanger is good, the calcining effect is realized, and the following processes can be realized: the continuous drying and cooling process of solid material and moisture absorbing material, the continuous pelletizing and stoving process of powdered material, the continuous drying, calcining and cooling process of wet crystallized material, and the continuous pelletizing process of liquid material.

The continuous production is characterized in that: because of continuous production, the product has good process repeatability and high production efficiency; the method is suitable for continuous drying and granulating, and the final product can be dustless and has excellent performance; for the situation that manual participation in the intermediate process is not expected and pollution is prevented, a continuous mode is the best choice; the energy consumption is low; the structure is compact; because the temperature of the material layer can be low, the safety standard is high, and the method is suitable for processing heat-sensitive materials; the operation is reliable; the evaporation intensity is high, and the volume is 1/15-1/30 of a spray drying tower; the method is suitable for continuous drying and granulation of viscous materials and materials with strong moisture absorption; especially when the output is larger, compared with batch type equipment, the method has the absolute advantages of energy consumption and quality.

In the process of hot air drying, the wet material mainly comprises a constant-speed drying stage and a speed-reducing drying stage, in the constant-speed drying stage, the air from the fluidized bed has more water and higher absolute humidity which are taken away by the air for unit drying, and after gas-solid separation, the heat is difficult to directly recycle and can be directly emptied; in the speed reduction drying stage, the air from the fluidized bed and the moisture taken away by the air for unit drying are from high to low until zero reaches a balance section, the absolute humidity is lower, the contained heat is completely lost if the air is directly emptied after gas-solid separation, the emptied tail gas needs to be subjected to environmental protection treatment, the environmental protection pressure is increased, the high-humidity exhaust of the front section of the constant speed section and the speed reduction section of the traditional fluidized bed and the low-humidity exhaust of the rear section of the speed reduction section are usually mixed together, and the heat contained in the exhausted air is difficult to utilize.

After gas discharged by the traditional fluidized bed drying is separated by a dust removal system, the obtained solid has small particle size, does not conform to the particle size range of finished products, usually needs to be added with liquid for redissolution and recrystallization treatment, but the recrystallization directly has recrystallization loss, and the added liquid needs to be dried repeatedly, so that the whole energy consumption is increased; the materials collected by the cyclone separator in the traditional dust removal system still contain partial finished product particle size range materials and the water content exceeds the standard, and the materials are generally required to return to the fluidized bed body, so that the materials in the cyclone separator are repeatedly abraded for many times, the fine powder content in the fluidized bed is increased, and the defects of yield reduction and energy consumption increase are aggravated again.

In the prior art of fluidized bed drying, the wet raw material upper process can be loose or lump wet material obtained by a centrifuge, a filter press, a concentration evaporator and other modes, and when the wet raw material is subjected to fluidized bed drying operation, the defects frequently occurring in the traditional fluidized bed are adopted: after the wet material enters the fluidized bed, the wet material is not dried and dispersed in time, so that the wet material is agglomerated in the bed, the air distribution screen plate is pasted and the shell wall is damaged to cause fluidization, and the bed is dead.

Patent document ZL200720077144.2 "an energy-saving fluidized bed" adopts a method of installing a dryer in an exhaust system and installing a replaceable desiccant in the dryer to utilize the heat energy of exhausted tail gas, but has the disadvantages that the desiccant is difficult to select, expensive and inconvenient to replace, and the desiccant is not enough to absorb the moisture in the exhaust tail gas, the absorption capacity is gradually reduced along with the time from the beginning, so that the production condition is difficult to control, and the drying capacity of the fluidized bed is gradually reduced.

Patent document ZL201220224409.8 "an energy-saving fluidized bed" adopts a mode of directly recycling part of the exhausted tail gas to the inlet of the process air through a return pipe, and has the disadvantages that the exhausted tail gas contains a large amount of water and returns to the inlet process air, so that the inlet air humidity is increased, the drying capacity is reduced, and the larger the recycling ratio is, the larger the reduction degree of the drying capacity of the production line is, and even the exhaust tail gas cannot be dried.

Patent document ZL201720223838.6 "a pelletization drying energy-saving system", in which heat pipe heat exchangers are disposed in an inlet process air system and an exhaust system, and the inlet process air is heated by heat energy of tail gas, and has the disadvantages that two sets of heat pipe heat exchangers are required, which results in one time investment, one time heat exchange efficiency reduction, one time air system resistance increase, and the increase of air system resistance directly determines the increase of system fan power, and users feel that the heat pipe heat exchangers are not cost-effective and give up after balancing cost performance, maintenance cost, and fan power operating cost because of the existence of micro powder in the exhaust system, the fin heat exchanger cannot be used, and the size and investment of the heat pipe heat exchanger between the exhaust systems are increased.

SUMMERY OF THE UTILITY MODEL

The utility model aims at providing an energy-conserving fluidized bed system can reduce fluidized bed tail gas displacement, can utilize the evacuation heat that the fluidized bed was aired exhaust as far as possible, and the export material does not have the dust and flies upward, reaches evacuation tail gas feature of environmental protection and improves, production line energy consumption reduces, the export material does not have powder, the material yield improves, the effect of operation safety and stability, investment cost performance is high, the effect of maintenance and working costs low.

The technical scheme for realizing the purpose is as follows: the utility model provides an energy-conserving fluidized bed system, includes the fluidized bed main part, is provided with constant speed section drying area and deceleration section drying area in the fluidized bed main part, is provided with air intake, high wet air exit, low wet air exit in the fluidized bed main part, its characterized in that: the air inlet corresponding to the constant-speed section drying area is connected with a constant-speed section air inlet system, the air inlet corresponding to the speed reduction section drying area is correspondingly connected with a speed reduction section air inlet system, the high-humidity air outlet is connected with an air outlet heat exchange system for exchanging heat with fresh air, the outlet of the fresh air exchanged by the air outlet heat exchange system is connected with the constant-speed section air inlet system or/and the speed reduction section air inlet system, and the outlet of the low-humidity air outlet is connected with the constant-speed section air inlet system or/and the speed reduction section air inlet system.

The utility model has the advantages that:

the exhaust of the high-humidity exhaust outlet is connected to the exhaust port through the air-out heat exchange system, the high-humidity high-temperature exhaust realizes the effects of cooling and humidity reduction through heat exchange, and is beneficial to the environmental protection treatment of subsequent tail gas, the fresh air and the air-out heat exchange system are subjected to heat exchange and temperature rise and then are input into the fluidized bed main body to dry the material, the contained heat of the high-humidity high-temperature exhaust can be utilized by 20-50% generally, the heat utilization is considerable, the exhaust humidity of the low-humidity exhaust outlet is low, the temperature is high, therefore, the exhaust heat is directly input into the fluidized bed main body to dry the material, the heat utilization is close to 100%, the exhaust heat of the fluidized bed main body can be utilized to the maximum degree, and the energy consumption of a production line is reduced.

As a preferred scheme, an outlet of the low-humidity air outlet is connected with the constant-speed section air inlet system, and an outlet of heat exchange fresh air of the air outlet heat exchange system is connected with the speed reduction section air inlet system. The low-humidity air outlet still contains a certain amount of water, and has influence on the deceleration drying stage, and can directly return to the constant-speed drying stage for utilization.

Furthermore, in order to reduce the discharge temperature of the materials and the homogenization and stabilization effects of the materials, the fluidized bed main body is also provided with a cooling section fluidization area close to the discharge hole, and an air inlet corresponding to the cooling section fluidization area is connected with a cooling section air inlet system.

Furthermore, the upper part in the fluidized bed main body is a separation chamber, a separation chamber partition plate is arranged in the separation chamber, the separation chamber is divided into two cavities through the separation chamber partition plate, the high-humidity air outlet is connected with the cavity close to one side of the feed inlet, and the low-humidity air outlet is communicated with the cavity on the other side.

The air exhaust of the high-humidity air outlet and the air exhaust of the low-humidity air outlet can be better isolated through the separating chamber partition plate, disorder is prevented, and the separating chamber partition plate is set to be in a movable adjusting mode, so that the air exhaust proportion of the high-humidity air outlet and the low-humidity air outlet can be adjusted.

Further, for improve equipment's feature of environmental protection, realize simultaneously that the material is collected and improve the material yield in airing exhaust to high wet air exit, low wet air exit, fluidized bed system still includes first dust pelletizing system, second dust pelletizing system and conveying system, high wet air exit is through first dust pelletizing system connection air-out heat transfer system, low wet air exit is through second dust pelletizing system connection constant speed section air inlet system or/and deceleration section air inlet system, conveying system is connected with first dust pelletizing system and second dust pelletizing system, and conveying system is used for the material output of collecting first dust pelletizing system and second dust pelletizing system.

Further, the first dust removal system and the second dust removal system can be arranged in the fluidized bed main body and can also be arranged in the fluidized bed main body, and both the first dust removal system and the second dust removal system can play a dust removal effect.

Further, in order to facilitate granulation of the materials collected by the first dust removal system and the second dust removal system, a mixing granulation system is arranged at a feed inlet of the fluidized bed main body, a discharge end of the conveying system is connected with a 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 to grow.

Further, the mixing and granulating system comprises a blade type granulator, the blade type granulator comprises a granulator shell and two driving motors, two blade shafts are arranged in the granulator shell, each driving motor is connected with one blade shaft and can adjust the rotating speed, and a plurality of multi-blade type blades are arranged on the blade shafts. This kind of blade formula granulator promptly plays in succession the dispersed import raw materials in the twinkling of an eye, makes the wet raw materials of import into the effect of tiny granule in the twinkling of an eye, prevents to have the bold material in the import raw materials or get into the fluidized bed body in the caking, reduces the wet material and agglomerates in the fluidized bed, reduces the effect of dust in the fluidized bed.

Two sets of granulator blades adopt two granulator power drives to the rotational speed is adjustable respectively, can form two sets of blade speed differentiation, forms better pelletization effect, is favorable to the mixed pelletization of dust and wet raw materials, the wet granulation of dust self after moist. On the one hand, the dispersion effect of wet materials entering the fluidized bed can be improved, the agglomeration possibility is reduced, and on the other hand, the function of making wet raw materials into small particles is achieved, the small particles are prevented from agglomerating to form large agglomerates, so that finished products of the small particles are obtained.

Further, for off-the-shelf homogenization more and transport, the discharge gate of fluidized bed main part is provided with export material system, and export material system is including sieving ware and breaker, and the sieving ware is used for sieving the material of fluidized bed body output for large granule, well granule, and the large granule is got back to the fluidized bed after the breaker is broken originally internally, and well granule is as the finished product.

For more uniformity, the screen may be further provided with a small particle outlet to return the small particles and a small amount of dust together into the fluidized bed.

Furthermore, the conveying system can be added with a wetting agent during the conveying process to carry out mixing or agglomeration granulation work, and can also independently convey the granulated dust into the fluidized bed main body.

Furthermore, the internal heat exchangers are respectively arranged in the fluidizing chambers of the fluidized bed main body, so that a heat source and a cold source can be introduced, and the flow of the introduced heat source and cold source can be controlled and adjusted.

Furthermore, a through hole blocking net is arranged below a feed inlet of the fluidized bed main body to form a dry and wet material mixed material layer, and materials firstly enter the dry and wet material mixed material layer and then enter a fluidizing chamber of the fluidized bed main body through the through hole blocking net during feeding.

The wet material entering the dry and wet material mixture area is firstly dispersed and primarily dried by the material of the mixture layer, and the area can adopt higher hot air temperature, sometimes big lumps can be inevitably generated to cause poor fluidization, at the moment, the dry and wet material mixture layer is arranged below the feed inlet in the fluidized bed body, the wet raw material firstly enters the dry and wet material mixture layer and then enters the fluidized material layer through the through hole blocking net, so even if lumps exist, the lumps of the dry and wet material mixture area can not enter the nearby fluidized material area because of the effect of the through hole blocking net, the adhesion of the air distribution net plate, especially the area with the inner heat exchanger can be prevented, the problems of poor fluidization, material friction, material self accumulation and temperature rise and fire explosion accidents caused by the lumps generated by the inner heat exchanger and the adhesion inner heat exchanger can be avoided, and the lumps blocked in the mixture area can not be generated due to the effect of the fluidized material in the working process, Can slowly grind, can not grind can regularly shut down the clearance to stability when guaranteeing production, thereby reach the utility model discloses the purpose.

Further, the fluidized bed main body is composed of a plurality of fluidized beds connected with each other.

In the actual working process, the heat exchange fresh air quantity of the high-humidity air outlet and the air quantity of the low-humidity air outlet are not necessarily equal to the air quantity of the corresponding air inlet, and an air inlet bypass can be arranged at the corresponding air inlet to adjust the supplementary air quantity.

To sum up, adopt above the utility model discloses technical scheme, the during operation has reduced fluidized bed tail gas displacement, has utilized exhaust system's evacuation heat as far as possible, and the material of export material system does not have the dust and flies upward, reaches evacuation tail gas feature of environmental protection and improves, production line energy consumption reduces, the export material does not have powder, material yield improves, the operation is stable safe, investment cost performance is high, the effect of maintaining and working costs is low.

Drawings

FIG. 1 is a schematic diagram of the system of the present invention;

FIG. 2 is a schematic structural view of a fluidized bed body;

FIG. 3 is a system schematic diagram of a constant velocity section air inlet system;

FIG. 4 is a schematic diagram of a system of a speed reduction section air inlet system;

FIG. 5 is a system schematic diagram of a cooling zone air intake system;

FIG. 6 is a schematic diagram of the system in which the first dust removal system and the second dust removal system are connected to the dust conveying system;

FIG. 7 is a system schematic of a hybrid granulation system;

FIG. 8 is a schematic top view of a blade pelletizer;

FIG. 9 is a schematic elevation view of a blade granulator;

fig. 10 is a system schematic of a fluidized material handling system.

Detailed Description

First embodiment

The following preferred configurations of equipment components are increased or decreased according to specific needs, and are not merely exemplary

As shown in fig. 1: an energy-saving fluidized bed system comprises a fluidized bed main 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 with the first dust removal system 5 and the second dust removal system 6.

As shown in fig. 2, the fluidized bed body 1 includes a fluidized bed housing 1.1, the fluidized bed housing 1.1 is provided with 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 the fluidized bed housing 1.1 is provided with an air inlet chamber 1.3, an air distribution screen plate 1.2, a fluidizing chamber 1.4, and a separation chamber 1.5 in sequence from bottom to top.

Preferably, the fluidized bed body 1 can be further provided with a material return port 1.15 as required, the fluidized bed body 1 can adopt various existing technologies such as an existing vibrating fluidized bed, a boiling fluidized bed, an internal heating fluidized bed, a pulsating fluidized bed, a spouted fluidized bed and the like, the equipment composition can be adjusted according to specific process requirements, and the composition range is increased or decreased.

Preferably, the middle part of the separation chamber 1.5 of the fluidized bed body 1 is provided with a separation chamber partition plate 1.12, so that the high-humidity exhaust port 1.16 and the low-humidity exhaust port 1.17 can be better separated, the separation chamber 1.5 is separated into two cavities through the separation chamber partition plate 1.12, the high-humidity exhaust port 1.16 is connected with the cavity on one side close to the feed port 1.6, and the low-humidity exhaust port 1.17 is communicated with the cavity on the other side. More preferably, the separating chamber partition 1.12 can be arranged into a movable adjusting type mounting structure with the position adjustable towards two sides, and is used for adjusting the air exhaust ratio of the high-humidity air outlet 1.16 and the low-humidity air outlet 1.17.

Preferably, an internal heat exchanger 1.11 is arranged in a 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 according to requirements, and flow regulation is arranged in cooperation with the transportation of the heat source and the cold source.

Preferably, a through hole baffle net 1.13 is arranged below the feed inlet 1.6 of the fluidized bed body 1 to form a dry and wet material mixed layer, and the structure of the through hole baffle net is described in detail in a patent document of an internal heat exchange fluidized bed dryer (2018220840814), and is not described in detail herein.

A fluidized bed shell 1.1 is internally divided into a constant-speed section drying area 1.18 and a speed reduction section drying area 1.19 from a feeding port 1.6 to a discharging port 1.7 side in sequence, an air inlet 1.21 corresponding to the constant-speed section drying area 1.18 is connected with a constant-speed section air inlet system 2, and an air inlet corresponding to the speed reduction section drying area 1.19 is correspondingly connected with a speed reduction section air inlet system 3.

The high-humidity air outlet 1.16 is connected with an air outlet heat exchange system 25 for exchanging heat with fresh air through a first dust removal system 5, an outlet of heat exchange fresh air of the air outlet heat exchange system 25 is connected with an air inlet of the constant-speed section air inlet system 2 or/and the speed reduction section air inlet system 3, and the low-humidity air outlet 1.17 is connected with an air inlet of the constant-speed section air inlet system 2 or/and the speed reduction section air inlet system 3 through a second dust removal system 6; as a preferable solution of this embodiment, that is, an exemplary solution of this embodiment, an outlet of the low-humidity exhaust port 1.17 is connected to an air inlet of the constant-speed section air intake system 2 through the second dust removal system 6, and an outlet of the heat-exchange fresh air of the air-out heat exchange system 25 is connected to an air inlet of the speed-reduction section air intake system 3.

Preferably, a cooling section fluidizing zone 1.20 is further arranged between one side of the speed reduction section drying zone 1.19 in the fluidized bed main body 1, which is far away from the constant speed section drying zone 1.18, and the discharge port 1.7, and an air inlet corresponding to the cooling fluidizing zone 1.20 is connected with a cooling section air inlet system 4.

As a preferred configuration, the air-out heat exchange system 25 includes an induced draft fan 7 connected to the air outlet of the first dust removal system 5, a tail gas heat exchanger 8, and a tail gas environmental protection system 9, the induced draft fan 7, the tail gas heat exchanger 8, and the tail gas environmental protection system 9 are connected in series, fresh air and the tail gas heat exchanger 8 exchange heat and then are conveyed to the speed reduction section air inlet system 3, the tail gas heat exchanger 8 can be a tube fin type heat exchanger or a plate type heat exchanger, and the like, and the tail gas after heat exchange is treated by the tail gas environmental protection system 9 (the tail gas environmental protection system 9 can adopt water dust removal equipment, plasma odor removal equipment, electrostatic dust removal equipment, and the like commonly used by those skilled in the art) and then is received at the air exhaust port.

As shown in fig. 1, in the actual working process, the air discharge amount of the high-humidity air outlet 1.16 and the air discharge amount of the low-humidity air outlet 1.17 are not necessarily equal to the air intake amounts of the constant-speed section air intake 2 and the speed reduction section air intake 3, so that the hot process air intake bypass 19 is further connected to the air intake of the constant-speed section air intake system 2 or the speed reduction section air intake system.

In order to facilitate the granulation of the material conveyed by the conveying system 20, a mixing and granulating system 16 is arranged at the feed opening 1.6 of the fluid bed body 1.

As shown in fig. 7, as a preferred configuration of the present embodiment, the mixing and granulating system 16 includes a wet material classifying device 16.1 (the wet material classifying device 16.1 adopts but is not limited to a screen), a large wet granule processing device 16.2 (the large wet granule processing device 16.2 adopts but is not limited to a melting tank, the melting tank is used for dissolving large granules), a dry and wet material mixer 16.3, a blade type granulator 16.4; the wet material grading equipment 16.1 is provided with a large wet particle discharge port and a small wet particle discharge port, the large wet particle discharge port 16.1 is connected with large wet particle processing equipment 16.2, the small wet particle discharge port is connected with a dry and wet material mixer 16.3, and the discharge port of the dry and wet material mixer 16.3 is connected with a feed port 1.6 of the fluidized bed main body 1 through a blade type granulator 16.4.

As shown in fig. 8 and 9, the blade type granulator 16.4 can achieve the effect of instantly breaking up and instantly granulating wet raw materials, and specifically includes a granulator housing 16.41 and two driving motors 16.42, the granulator housing 16.1 is provided with a feed inlet at the upper end and a discharge outlet at the lower end, two blade shafts 16.43 arranged in parallel side by side are rotatably installed in the granulator housing 16.1, each driving motor 16.42 is in transmission connection with one blade shaft 16.43, a plurality of multi-bladed blades 16.44 are respectively installed on the blade shafts 16.43, a plurality of blades are circumferentially arranged on the multi-bladed blades 16.44, and the multi-bladed blades 16.44 on the two blade shafts 16.436 are staggered and partially overlapped.

When the blade type granulator 16.4 works, the two driving motors 16.42 drive the multi-blade type blades 16.44 to rotate around the corresponding blade shafts 16.43 respectively, the rotating speeds of the multi-blade type blades are adjustable respectively, wet raw materials or dry and wet raw materials enter from a feeding hole of the blade type granulator 16.4, and the wet raw materials or the dry and wet raw materials are output from a discharging hole 53 after granulation is finished.

As shown in fig. 1 and 10, the discharge port 1.7 of the fluidized bed housing 1.1 is provided with an outlet material system 17, as a preferred configuration, the outlet material system 17 includes a screen 17.2 and a crusher 17.3, a conveying mechanism 17.1 is connected between the discharge port 1.7 of the fluidized bed housing 1.1 and a feed port of the screen 17.2, the conveying mechanism 17.1 conveys the material to the screen 17.2, the material is processed by the screen 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 conveyed into the fluidized bed main body 1 through a return port 1.15, the outlet material system 17 can be further provided with a finished product conveyor 17.4, a finished product bin 17.5 and a wrapper 17.6, the medium particles are used as finished products and conveyed to the finished product bin 17.5 through the finished product conveyor 17.4, and finally the finished products are wrapped by the wrapper 17.6. The composition of the outlet material system 17 is flexible and various, for example, the screen 17.2 can be in the form of two outlets, three outlets, four outlets, etc. When the material has a general particle size requirement, sieving is not required.

Conveying system 20 can add the wetting agent in the transmission process, mixes or reunion pelletization work, also can be alone carry fluidized bed main part 1 with the dust pelletization after in, also can get into and mix pelletization system 1, when the dust can the granulation in the conveying process, or when having the pelletization alone, mix pelletization system 16 and be in the utility model discloses also can not adopt in the technology.

As shown in fig. 3, as a preferred configuration of this embodiment, the constant-speed section air inlet system 2 includes a hot process air filter 2.1 and a hot process air inlet machine 2.2 connected to each other, and the exhaust air of the low-humidity exhaust port 1.17 is dedusted by the second dedusting system 6, then is input to the hot process air filter 2.1 for filtering, and then is input to the air inlet 1.21 corresponding to the constant-speed section drying area 1.18 through the hot process air inlet machine 2.2 and the hot process air adjusting valve 2.4. As a further preferred feature of this embodiment, the constant-speed section air inlet system 2 further includes a thermal process air heat exchanger 2.3 serially connected to the pipeline of the constant-speed section air inlet system, the temperature of the thermal process air is further increased by the thermal process air heat exchanger 2.3, a plurality of air inlets 1.21 corresponding to the constant-speed section air inlet system 2 may be provided, and the temperature, pressure, air volume, and the like of each air inlet may be adjusted according to process requirements.

As shown in fig. 4, as a preferred configuration of this embodiment, the speed-reduction section air inlet system 3 includes an intermediate-temperature process air filter 3.1 and an intermediate-temperature process air inlet machine 3.2 that are connected to each other, and fresh air after heat exchange with the tail gas heat exchanger 8 is filtered by the intermediate-temperature process air filter 3.1 and then is input into an air inlet 1.21 corresponding to the speed-reduction section drying zone 1.19 through the intermediate-temperature process air inlet machine 3.2. As a further preferable feature of this embodiment, the speed-reducing section air inlet system 3 further includes an intermediate-temperature process air heat exchanger 3.3 serially connected to the pipeline of the speed-reducing section air inlet system, the intermediate-temperature process air heat exchanger 3.3 is serially connected to the output end of the intermediate-temperature process air inlet machine 3.2, a part of the intermediate-temperature process air output by the intermediate-temperature process air inlet machine 3.2 is delivered to the air inlet 1.21, which is close to the cooling section fluidizing area 1.20 and corresponds to the speed-reducing section drying area 1.19, through the second intermediate-temperature process air regulating valve 3.5, and the other part of the intermediate-temperature process air is delivered to the air inlet 1.21, which is close to the constant-speed section drying area 1.18 and corresponds to the speed-reducing section drying area 1.19, through the intermediate-temperature process air heat exchanger 3.3 and the first intermediate-temperature process air regulating valve 3.4.

As shown in fig. 5, as a preferred configuration of this embodiment, the cooling zone 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, and the air is filtered by the cold process air filter 4.1, and then is input into an air inlet 1.21 corresponding to the cooling zone fluidizing zone 1.20 through the cold process air intake fan 4.3 and a cold process air regulating valve 4.5. As a further improvement of this embodiment, the cooling section air inlet system 4 further includes a cold process air temperature and humidity adjusting device 4.2 and a cold process air heat exchanger 4.4 connected in series to the pipeline of the cooling section air inlet system 4, where the cold process air temperature and humidity adjusting device 4.2 is used to adjust the temperature and humidity of the cold process air, and the cold process air heat exchanger 4.4 is connected in series to the output end of the cold process air inlet machine 4.3 and is used to recool the air output by the cold process air inlet machine 4.3 to offset the temperature rise of the cold process air inlet machine 4.3 on the inlet air.

As shown in fig. 6, as a preferred configuration of this embodiment, the second dust removing system 6 includes a first cyclone dust collector 6.1 and a first bag-type dust collector 6.2, an inlet end of the first cyclone dust collector 6.1 is connected to a low-humidity exhaust outlet 1.17, an air outlet is connected to the first bag-type dust collector 6.2, and an air outlet of the first bag-type dust collector 6.2 is connected to an air inlet of the hot process air filter 2.1.

As a preferable configuration of this embodiment, the first dust removal system 5 includes a second cyclone 5.1 and a second bag-type dust remover 5.2, an inlet end of the second cyclone 5.1 is connected to the high-humidity air outlet 1.16, an air outlet is connected to the second bag-type dust remover 5.2, and an air outlet of the second bag-type dust remover 5.2 is connected to the induced draft fan 7.

As shown in fig. 6, a common optional composition example of the conveying system 20 is: including gas-dust separator 10, dust conveyer pipe 11, the air outlet of first dust pelletizing system 5 can be connected to the air outlet of gas-dust separator 10, dust conveyer pipe 11 sets up behind the bottom play dirt mouth of first sack cleaner 6.2, second sack cleaner 5.2, and the one end of dust conveyer pipe 11 is connected with the feed inlet of gas-dust separator 10, the other end is connected with dust conveying fan 12, and dust conveying fan 12's exit end has still concatenated heater 13 for carry the wind heating, avoid material moisture absorption to stick with paste the pipe, the play dirt mouth of first sack cleaner 6.2, second sack cleaner 6.1 bottom is connected with dust conveyer pipe 11 respectively.

The dust outlets of the first cyclone dust collector 6.1 and the second cyclone dust collector 5.1 are respectively connected with a dust conveyor 14, dust discharging valves 15 are respectively connected between the dust conveyor and the dust outlets of the first cyclone dust collector 6.1 and the second cyclone dust collector 5.1, and the discharge ends of the dust conveyor 14 are respectively connected with a dry and wet material mixer 16.3.

The utility model discloses a working process:

the fluidized bed main body 1 is provided with three kinds of process air of constant-speed section air inlet, speed reduction section air inlet and cold process air inlet, wherein the constant-speed section air inlet is provided with a hot process air inlet bypass, each process air enters the fluidizing chamber 1.4 through the air inlet chamber 1.3 and the air distribution screen plate 1.2 to perform heat and mass exchange with materials, and then is input into the second dust removal system 6 and is dedusted by the first dust removal system 5.

In order to be more beneficial to material collection and granulation of the dust conveying system 20, the mixing and granulating system 16 is arranged, wet raw materials are granulated through the mixing and granulating system 16 and then enter the feeding hole 1.6 of the fluidized bed body 1, specifically, the wet raw materials are classified through the wet material classifying equipment 16.1, large particles enter the large wet particle processing equipment 16.2 for processing, qualified wet materials and dry materials conveyed by the conveying system 20 enter the dry and wet material mixer 16.3 for mixing, then enter the blade type granulator 16.4 for granulation and then enter the fluidized bed body 1, the effects of instant scattering and instant granulation of the wet raw materials can be achieved, and the materials are fluidized under the action of each process air;

the process air and the material are discharged from the fluidized bed after heat and mass exchange, and respectively enter the first dust removal system 5 and the second dust removal system 6, the second dust removal system 6 removes dust, an air outlet of the second dust removal system 6 is connected to an inlet of the constant-speed section air inlet system 2, nearly half of exhaust tail gas volume can be reduced, simultaneously, the heat contained in the second dust removal system 6 is fully utilized, the environmental protection of the exhaust tail gas is improved, the energy consumption of a production line is reduced, and the exhaust air of the first dust removal system 5 can be directly exhausted.

The materials separated by the first dust removing system 5 and the second dust removing system 6 are conveyed to the mixing granulation system 16 under the action of the conveying system 20 to grow up and then enter the fluidized bed main body 1 without being added with water for redissolution, so that the materials of the outlet material system are free of dust flying, the material yield is improved, the powder amount in the fluidized bed main body is reduced, and the operation is stable and safe.

The embodiment is also provided with an outlet material system 17, the output material of the fluidized bed shell 1.1 is firstly conveyed to a screen 17.2 through a conveying mechanism 17.1, then is processed by the screen 17.2 to obtain large particles, medium particles and small particles, the large particles are crushed by a crusher 17.3 and then are conveyed into the fluidized bed main body 1 through a material returning port 1.15 together with small particle fine powder, the medium particles are used as finished products and conveyed to a finished product bin 17.5 through a finished product conveyor 17.4, and finally are packaged through a packaging machine 17.6.

Second embodiment

The second embodiment differs from the first embodiment in that: the fluidized bed body in the first embodiment is composed of a plurality of fluidized beds connected to each other.

The terminology used in the above embodiments and arrangements of the invention is prior art.

Claims (10)

1. The utility model provides an energy-conserving fluidized bed system, includes the fluidized bed main part, is provided with constant speed section drying area and deceleration section drying area in the fluidized bed main part, is provided with air intake, high wet air exit, low wet air exit in the fluidized bed main part, its characterized in that: the air inlet corresponding to the constant-speed section drying area is connected with a constant-speed section air inlet system, the air inlet corresponding to the speed reduction section drying area is correspondingly connected with a speed reduction section air inlet system, the high-humidity air outlet is connected with an air outlet heat exchange system for exchanging heat with fresh air, the outlet of the fresh air exchanged by the air outlet heat exchange system is connected with the constant-speed section air inlet system or/and the speed reduction section air inlet system, and the outlet of the low-humidity air outlet is connected with the constant-speed section air inlet system or/and the speed reduction section air inlet system.

2. The energy-saving fluidized bed system according to claim 1, wherein: the fluidized bed main body is also provided with a cooling section fluidization area close to the discharge hole, and an air inlet corresponding to the cooling section fluidization area is connected with a cooling section air inlet system.

3. The energy-saving fluidized bed system according to claim 1, wherein: the upper part in the fluidized bed main body is a separation chamber, a separation chamber partition plate is arranged in the separation chamber, the separation chamber is divided into two cavities by the separation chamber partition plate, a high-humidity air outlet is connected with the cavity close to one side of the feed inlet, and a low-humidity air outlet is communicated with the cavity on the other side.

4. A fluid bed system according to claim 1, wherein: the fluidized bed system further comprises a first dust removal system, a second dust removal system and a conveying system, the high-humidity air outlet is connected with the air outlet heat exchange system through the first dust removal system, the low-humidity air outlet is connected with the constant-speed section air inlet system or/and the speed reduction section air inlet system through the second dust removal system, the conveying system is connected with the first dust removal system and the second dust removal system, and the conveying system is used for outputting materials collected by the first dust removal system and the second dust removal system.

5. A fluid bed system according to claim 4, wherein: the feed inlet of fluidized bed main part is provided with the mixed pelletization system, conveying system's discharge end is connected with the feed end of mixed pelletization system.

6. A fluid bed system according to claim 5, wherein: the mixed granulating system comprises a blade type granulator, the blade type granulator comprises a granulator shell and two driving motors, two blade shafts are arranged in the granulator shell, each driving motor is connected with one blade shaft and can adjust the rotating speed, and a plurality of multi-blade blades are arranged on the blade shafts.

7. The energy-saving fluidized bed system according to claim 1, wherein: the discharge gate of fluidized bed main part is provided with export material system, and export material system is including sieving ware and breaker, and the sieving ware is used for sieving the material of fluidized bed body output for large granule, well granule, and the large granule returns to the fluidized bed after the breaker is broken originally internally, and well granule is as the finished product.

8. The energy-saving fluidized bed system according to claim 4, wherein: the conveying system can be added with a wetting agent during the conveying process to carry out mixing or agglomeration granulation.

9. The energy-saving fluidized bed system according to claim 1, wherein: the fluidizing chambers of the fluidized bed main body are respectively provided with an internal heat exchanger; the through hole blocking net is arranged below the feed inlet of the fluidized bed main body to form a dry and wet material mixed material layer, and during feeding, materials firstly enter the dry and wet material mixed material layer and then enter the fluidizing chamber of the fluidized bed main body through the through hole blocking net.

10. The energy-saving fluidized bed system according to claim 1, wherein: the fluidized bed main body is formed by connecting a plurality of fluidized beds.

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