CN203593422U - Conveying system for powder with activation function - Google Patents

Abstract

The utility model discloses a conveying system for powder with an activation function. The conveying system comprises a material bin, a discharging port at the bottom of the material bin is connected with the feeding end of a vertical disc feeder, and the discharging end of the vertical disc feeder is connected with a material inlet of a fluidized bed activation device. The top of the fluidized bed activation device is provided with an activation device outlet connected to a dosing point, and the position, located below the material inlet, of the middle of the fluidized bed activation device is provided with a bed material feeding device. The lower portion of the fluidized bed activation device is provided with an air distribution device which is connected with a conveying air outlet of a conveying air preheating device through an air inlet. The bottom of the fluidized bed activation device is provided with a dreg discharging device.

Description

A delivery system for powder with activation function

technical field

The utility model relates to a material conveying system, in particular to a powder conveying system with an activation function.

Background technique

Incineration treatment of solid waste such as domestic garbage and hazardous waste has the advantages of complete harmlessness, high reduction, and high heat recovery and utilization rate. It is one of the technologies that best embodies the three principles of waste treatment. It has been widely used in developed countries and regions. Since the end of the 1990s, waste incineration technology has also developed rapidly in my country, but it cannot be ignored that the incineration method of domestic waste has also brought about secondary pollution, of which dioxins are the most important a class of pollutants.

Dioxin calcium-based blocking technology is an efficient control technology for the emission of dioxin-like substances during the incineration process of domestic garbage and hazardous waste. By adding a small amount of calcium-based blocker to a specific temperature range in the incinerator and the flue gas cooling stage after the incinerator, the synthesis reaction of dioxins during the incineration process and the post-incineration cooling process can be effectively inhibited. Therefore, the dioxin calcium-based blocking technology is the total discharge control technology of dioxin-like substances.

At present, the conventional powder material conveying technology mostly adopts the method of pre-stage quantitative feeding + post-stage conveying. Among them, the commonly used methods of quantitative feeding are screw conveyor, star feeder, disc feeder, etc. Depending on the conveying distance and the characteristics of the conveying destination, mechanical conveying and pneumatic conveying can be selected. This is a very mature and reliable conveying technology, but for some special materials and some specific working conditions, there are many difficult problems to overcome.

In most applications, the added powder materials are required to have good activity, mainly including uniform particle size (avoid agglomeration, particle size as small as possible), sufficient specific surface area, and as little impurity content as possible (such as water), etc. . But with the existing conventional conveying system, it is difficult to ensure that the above requirements are met. For most powder materials, especially fine powder materials with small particle size, they will be compacted and agglomerated when they are stored in the silo and transported by the quantitative feeder; some hygroscopic materials are stored or conveyed by pneumatic force It will absorb moisture in the ambient air, resulting in damp deterioration, and will intensify compaction and agglomeration.

Moreover, powdery materials that have a certain degree of cohesiveness or have been dampened and deteriorated are also easy to stick and adhere to the conveyor. In light cases, accurate quantitative transportation cannot be achieved, and in severe cases, the conveying system will be blocked.

Especially for special powdery materials such as dioxin calcium-based blockers, it is required that when transported to the dosing point, the material can maintain a median particle size of less than 70 μm, a specific surface area greater than 15m2/g, and a moisture content of less than 5%. If the existing conventional delivery system is adopted, it is far from reaching the requirements.

To sum up, in the conventional powder material conveying system, during the storage and transportation process, the activity of the material is easily reduced, and it does not have the ability to restore its activity. For some cohesive materials, it is difficult to achieve quantitative, continuous and stable transportation. For special materials such as dioxin calcium-based blockers, it is far from meeting the requirements for their transportation.

Therefore, in order to solve the above problems, it is very necessary to develop a powder delivery system with advanced technology, activation function and quantitative, continuous and stable operation.

Utility model content

The purpose of the utility model is to provide a powder conveying system with an activation function.

In order to achieve the above purpose, the powder conveying system provided by the utility model includes:

A silo 1, the discharge port 102 at the bottom is connected to the feed end 201 of the vertical disc feeder 2, and the discharge end 203 of the vertical disc feeder 2 is connected to the material of the fluidized bed activation device 3 The inlet 304 is connected;

The top of the fluidized bed activation device 3 is provided with an activation device outlet 305 connected to the dosing point; the middle part of the fluidized bed activation device 3 is located below the material inlet 304 and is provided with a bed material adding device 306; The lower part of the air distribution device 302 is provided, and the air distribution device 302 is connected to the delivery air outlet 402 of the delivery air preheating device 4 through the air inlet 301; the bottom of the fluidized bed activation device 3 is a slag discharge device 303.

Wherein, a stirring device 101 is provided above the discharge port 102 at the bottom of the silo 1, and the stirring blades of the stirring device are set at 1-3 stages, and the rotating speed of the stirring blades of the stirring device is 0.2-5 revolutions per minute.

Wherein, the vertical disc feeder 2 is provided with a feeding impeller 202 comprising 4 to 8 independent chambers, each chamber is separated by a vertical vertical plate, and the vertical disc feeder 2 passes through the feeding impeller 202 The rotation of the feed end 201 is conveyed to the discharge end 203 and discharged into the material inlet 304 of the fluidized bed activation device 3, and the vertical disc feeder 2 can be adjusted by controlling the speed of the feed impeller 202 Delivery volume. When the feeding impeller 202 rotates to the side of the discharge end 203 , it extends out of the shell of the vertical disc feeder 2 and into the material inlet 304 of the fluidized bed activation device 3 .

Wherein, the material inlet 304 of the fluidized bed activation device 3 is located within the range of 400-800 mm from the upper interface of the dense phase area in the fluidized bed activation device 3 .

The delivery method of the powder provided by the utility model:

Under the agitation of the stirring device 101, the powder in the silo 1 enters the feed end 201 of the vertical disc feeder 2 through the bottom discharge port 102, and is discharged from the discharge end 203 under the action of the feed impeller 202 The connected material inlet 304 enters the fluidized bed activation device 3 , and the delivery rate of the vertical disc feeder 2 is adjusted by controlling the speed of the feeding impeller 202 .

The conveying air enters the conveying air preheating device 4 from the conveying air inlet 401 and after being heated up, enters the fluidized bed activation device 3 through the air inlet 301 connected to the conveying air outlet 402 .

The bed material enters the fluidized bed activation device 3 through the bed material adding device 306, and the powder is activated and transported to the dosing point under the action of breaking the bed material and the fluidization of the conveying wind.

Wherein, the rotation speed of the stirring blades of the stirring device 101 is 0.2-5 revolutions per minute.

Wherein, the bed material added to the fluidized bed activation device 3 should satisfy that the median particle size is 5 to 30 times the particle size of the powder, and the true density is 1.8 to 2.5 grams/cubic centimeter.

Among them, the average flow velocity of gas in the fluidized bed activation device 3 is 1.2-15 m/s, the temperature of the gas and powder at the outlet 305 of the activation device is not lower than 80°C, and the relative humidity is less than 50%.

The utility model adopts a fluidized bed activation device to add bed materials into the fluidized bed activation device, and at the same time combines a vertical disc feeder, and controls the preheating degree of the conveying air to make the conveying air and materials leave the fluidized bed The temperature and relative humidity when activating the device are controlled within a certain range. The content of the above-mentioned utility model makes the retarder delivery system with activation function have the following advantages compared with the original conventional material delivery system:

a. In the process of storage and transportation of materials such as powder, the phenomenon of cohesion, agglomeration and compaction of materials occurs under the action of various factors such as self-accumulation and extrusion of the conveying device. For hygroscopic materials, this phenomenon is more prominent and seriously affects their activity. The utility model adopts a fluidized bed activation device, so that the powder with the above-mentioned problems can form a strong turbulent flow in the fluidized bed activation device due to the air flow, bed material and materials, and the material agglomerates are completely broken up and restored to fine particles. Improve the reactivity of materials such as blockers.

b. Since the conveying air has been preheated, it can more effectively remove the adsorbed moisture in the material, and further improve the activity of powder and other materials.

c. On the basis of quantitative delivery, the vertical disc feeder makes full use of the flow field in the fluidized bed activation device, so that it has a self-cleaning effect on the feeding impeller and the small chamber. It completely avoids problems such as sticking and clogging that existed in the original conveying device when conveying materials.

d. Also due to the self-cleaning effect, the feeding impeller and the small chamber are always kept clean, which also improves the accuracy of quantitative delivery. The problem of gradual reduction of the conveying volume of the original conveying device is avoided.

e. The stirring device installed in the silo can fully prevent the powder from bridging and arching in the silo, and at the same time can improve the fullness of the material in the vertical disc feeder.

In a word, compared with the original conventional material delivery system, the utility model has the advantage of restoring the original activity of the material while realizing the quantitative, continuous and stable delivery of the powder. Moreover, it also solves the problems of material cohesion and blockage in the conveying device, improves the operation reliability and reduces the operation cost.

Description of drawings

FIG. 1 is a schematic diagram of the overall structure of an embodiment of the blocking agent delivery system with activation function of the present invention.

Fig. 2 is a partial structural schematic diagram of the silo and the stirring device of the embodiment of the retarder delivery system with activation function of the present invention.

Fig. 3 is a partial structural diagram of the vertical disc feeder of the embodiment of the retarder delivery system with activation function of the present invention.

Explanation of the main components in the accompanying drawings:

1 silo, 101 stirring device, 102 bottom discharge port;

2 vertical disc feeder, 201 feed end, 202 feed impeller, 203 discharge end;

3 fluidized bed activation device, 301 air inlet, 302 air distribution device, 303 slag discharge device, 304 material inlet, 305 activation device outlet, 306 bed material adding device;

4 conveying air preheating device, 401 conveying air inlet, 402 conveying air outlet;

5 thermal instruments, 501 conveying air flow meter, 502 bed differential pressure gauge of fluidized bed activation device, 503 inlet conveying air thermometer of fluidized bed activation device, 504 outlet conveying air thermometer of fluidized bed activation device.

Detailed ways

The utility model solves many problems existing in the conventional material conveying system. Through the fluidized bed activation device, combined with the vertical disc feeder, the conveying system can realize quantitative, continuous and stable conveying of materials. Especially for special materials such as dioxin calcium-based blockers that are easy to absorb moisture and are easy to bond, it has the ability to restore activity. The following description is based on powdered dioxin calcium-based blockers as an example.

The conveying system of the present utility model includes: a silo 1, a vertical disc feeder 2 and a thermal instrument 5; wherein the silo 1 has a bottom discharge port 102; the vertical disc feeder 2 has a discharge port End 203 and feed end 201 connected to bottom discharge port 102.

It also includes a fluidized bed activation device 3 and a conveying air preheating device 4; wherein the fluidized bed activation device 3 has an air inlet 301, an air distribution device 302, a slag discharge device 303, a material inlet 304, an activation device outlet 305 and a bed material Join device 306 .

The conveying air preheating device 4 has a conveying air inlet 401 and a conveying air outlet 402; the retarder enters the fluidized bed activation device 3 through the material inlet 304 connected to the discharge end 203, and the conveying air enters the conveying air from the conveying air inlet 401. After the preheating device 4 is heated and heated, it enters the fluidized bed activation device 3 through the air inlet 301 connected with the delivery air outlet 402; the bed material enters the fluidized bed activation device 3 through the bed material adding device 306; Under the action of breaking the group of the material and the fluidization of the conveying wind, it is activated and transported to the dosing point of the retarder.

The silo 1 is also provided with a stirring device 101; and the stirring blades of the stirring device are provided with 1-3 stages.

Preferably, the stirring blades of the stirring device 101 are arranged in two stages, and the distance between the bottom of the lowest stage stirring blade and the bottom surface of the silo 1 is less than 100 mm.

Preferably, the rotation speed of the stirring blades of the stirring device 101 is 0.2-5 revolutions per minute.

The vertical disc feeder 2 also has a feeding impeller 202 comprising 4 to 8 independent chambers, each of which is separated by a vertical vertical plate, and the vertical disc feeder 2 passes through the feeding impeller 202. Rotate, the material entering the feed end 201 is delivered to the discharge end 203 and discharged, and the delivery rate of the vertical disc feeder 2 can be adjusted by controlling the speed of the feed impeller 202 .

Preferably, when the small chamber contained in the feeding impeller 202 is rotated to the discharge end 203 side, it can fully stretch out the housing of the vertical disc feeder 2, and stretch into the fluidized bed activation device 3, and the material therein Under the triple action of gravity, conveying air/fluidizing air blowing and bed material scouring, all can enter the fluidized bed activation device 3, and at the same time, the small chamber will be thoroughly cleaned without accumulating materials.

Preferably, the rotation speed of the feeding impeller 202 is 2-20 rotations per minute.

Preferably, the position of the material inlet 304 of the fluidized bed activation device 3 should be within the range of 400-800 mm from the upper interface of the dense phase area in the fluidized bed activation device 3 .

Preferably, the bed material added to the fluidized bed activation device 3 should meet the requirements that the median particle size is 5 to 30 times the retarder particle size, and the true density is 1.8 to 2.5 g/cm3.

The average flow velocity of the gas in the fluidized bed activation device 3 is 1.2-15 m/s, the temperature of the gas and retarder at the outlet 305 of the activation device is not lower than 80°C, and the relative humidity is less than 50%.

In order to make the above purpose, features and advantages of the utility model more obvious and understandable, the utility model will be further described in detail below in conjunction with the accompanying drawings and specific embodiments.

Please refer to the accompanying drawings. The conveying system of the present utility model includes: a silo 1, a vertical disc feeder 2 and a thermal instrument 5; wherein the silo 1 has a bottom discharge port 102; the vertical disc feeder 2 has a discharge port end 203 and the feed end 201 connected to the bottom discharge port 102;

It also includes a fluidized bed activation device 3 and a conveying air preheating device 4; wherein the fluidized bed activation device 3 has an air inlet 301, an air distribution device 302, a slag discharge device 303, a material inlet 304, an activation device outlet 305 and a bed material Adding device 306; conveying wind preheating device 4 has conveying wind inlet 401 and conveying wind outlet 402; Retardant enters fluidized bed activation device 3 through material inlet 304 connected with discharge end 203, and conveying wind enters fluidized bed activation device 3 from conveying wind inlet 401 enters the conveying air preheating device 4 and after being heated up, enters the fluidized bed activation device 3 through the air inlet 301 connected with the conveying air outlet 402; the bed material enters the fluidized bed activation device 3 through the bed material adding device 306; The retarder is activated and transported to the retarder dosing point under the action of breaking the bed material and the fluidization of the conveying wind.

Moreover, the silo 1 is also provided with a stirring device 101 , the stirring blades of the stirring device are arranged in two stages, and the bottom of the lowest-stage stirring blade is 50 mm away from the bottom surface of the silo 1 . The rotational speed of the stirring blades of the stirring device 101 is 0.2-5 revolutions per minute.

And, vertical disc feeder 2 also has the feeding impeller 202 that comprises six independent chambers, is separated by a vertical vertical plate between each chamber, and vertical disc feeder 2 passes through the feeding impeller 202 Rotate, the material entering the feed end 201 is delivered to the discharge end 203 and discharged, and the delivery rate of the vertical disc feeder 2 can be adjusted by controlling the speed of the feed impeller 202 . The small chamber that the feeding impeller 202 comprises can fully stretch out the housing of the vertical disk feeder 2 when rotating to the discharge end 203 side, and stretches into the fluidized bed activation device 3, and the material therein is transported under gravity and Under the triple action of wind/fluidizing wind blowing and bed material scouring, all can enter the fluidized bed activation device 3, and at the same time, the small chamber will be thoroughly cleaned without accumulating materials. The rotating speed of the feeding impeller 202 is 2 to 20 revolutions per minute, and the rotating speed can be adjusted by a speed regulating device.

Moreover, the material inlet 304 of the fluidized bed activation device 3 is located at 600 mm from the upper interface of the dense phase area in the fluidized bed activation device 3 . The median particle size of the bed material added to the fluidized bed activation device 3 is 10 times the particle size of the retarder, and the true density is about 2.3 g/cubic centimeter. The average flow velocity of the gas in the fluidized bed activation device 3 is 2.5 m/s, the temperature of the gas and retarder at the outlet 305 of the activation device is 90°C, and the relative humidity is about 20%.

In addition, thermal instruments are set up to monitor various key parameters of the retarder delivery system. It mainly includes: delivery air flowmeter 501, fluidized bed activation device bed differential pressure gauge 502, fluidized bed activation device inlet delivery air thermometer 503 and fluidized bed activation device outlet delivery air thermometer 504.

The retarder in the silo 1 falls into the vertical disc feeder 2 through the discharge port 102 at the bottom. Stirring the materials in the bin 1 by the stirring blades of the stirring device 101 can prevent the blocker from bridging and arching, and at the same time can ensure the fullness of the materials in the vertical disc feeder 2 . The vertical disc feeder 2 is a volumetric material conveying device. The retarder enters the small chamber of the feeding impeller 202 from the feed end 201. When the chamber rotates to the discharge end 203, the retarder is discharged. The conveying amount can be controlled by adjusting the rotating speed of the feeding impeller 202 .

Retardant and other materials enter the fluidized bed activation device 3 through the material inlet 304, and are rapidly mixed with the conveying air and the bed material. The fine-grained material will directly move to the outlet 305 of the activation device under the action of the conveying wind, and at the same time, the moisture adsorbed in the retarder is also desorbed into the conveying wind. The agglomerated materials in the previous storage and transportation process cannot be directly taken away by the conveying wind due to their large particle size, and will fall down into the dense phase area of the fluidized bed activation device 3 . In the dense-phase area, due to the presence of a large amount of bed material and the state of strong turbulent flow, the agglomerated material will be ground, broken up, and restored to fine particles, and will be carried by the conveying wind to the outlet 305 of the activation device. The moisture adsorbed in the air is also desorbed into the conveying air. By controlling the velocity of the conveying air in the fluidized bed activation device 3 , only retarder particles with a particle size smaller than a certain value can be taken out of the outlet 305 of the activation device. Particles with a particle size larger than this specific value will remain in the bed and be continuously ground and broken up. The particle size of the bed material fed into the fluidized bed activation device 3 is just controlled within a reasonable range, and is always kept in the dense phase region.

At the junction of the vertical disc feeder 2 and the fluidized bed activation device 3, when the small chamber of the feeding impeller 202 is forwarded to the discharge end 203, the housing of the vertical disc feeder 2 can be fully stretched out. into the fluidized bed activation device 3, and the materials in it can all enter the fluidized bed activation device 3 under the triple action of gravity, conveying wind/fluidization wind blowing and material scouring, and the small chamber will be thoroughly cleaned at the same time, and will not Stockpile of materials.

The conveying air required by the conveying system is preheated through the conveying air preheating device 4, and the degree of preheating depends on the moisture content and heat capacity of materials such as retarders. During operation, the temperature of the conveying air at the outlet 305 of the activation device and the relative humidity of the conveying air are used as references for control.

The key parameters of the conveying system are monitored by thermal instruments, and the operating parameters of each equipment are adjusted by feedback. The bed differential pressure of the fluidized bed activation device is used to characterize the bed material concentration in the fluidized bed activation device 3 to determine whether it is necessary to add bed material through the bed material adding device 306; the delivery air flow rate is used to characterize the fluidized bed activation device 3 The conveying air flow rate within the flow rate needs to be adjusted according to the target particle size of the blocker; the conveying air temperature at the outlet of the fluidized bed activation device is a control value, and the preheating of the conveying air preheating device 4 needs to be adjusted according to different conveying air flows degree (that is, the temperature of the conveying air at the inlet of the fluidized bed activation device), so as to ensure that the temperature of the conveying air at the outlet of the fluidized bed activation device is always higher than the set value.

To sum up, the blocker delivery system with activation function of the utility model has the advantage of restoring the original activity of the materials while realizing the quantitative, continuous and stable delivery of the blocker and other materials. Moreover, it also solves the problems of material cohesion and blockage in the conveying device, improves the operation reliability and reduces the operation cost.

A kind of retarder delivery system with activation function provided by the utility model has been introduced in detail above, and the principle and implementation of the utility model have been explained by using specific cases in the utility model, and the description of the above examples is only used To help understand the method of the utility model and its core idea; at the same time, for those of ordinary skill in the art, according to the idea of the utility model, there will be changes in the specific implementation and scope of application. In summary, The content of the description of the utility model should not be interpreted as a limitation of the utility model.

Claims (6)

1. a powder delivery system with mobilizing function, is characterized in that, comprising:

One feed bin, its bottom discharging mouth is connected with the feed end of vertical disc feeder, and the discharge end of vertical disc feeder is connected with the material inlet of fluid bed activating apparatus;

The top of fluid bed activating apparatus is provided with and is connected to the activating apparatus outlet adding a little;

The middle part of fluid bed activating apparatus is positioned at the below that is provided with material inlet and is provided with a bed material adding apparatus;

The bottom of fluid bed activating apparatus is provided with air-distribution device, and this air-distribution device connects the conveying wind outlet of carrying wind preheating device by ventilation inlet;

The bottom of fluid bed activating apparatus is slag-draining device.

2. powder delivery system according to claim 1, is characterized in that, the bottom discharging mouth top of feed bin is provided with mixing device, and the stirring vane of this mixing device arranges 1～3 grade.

3. powder delivery system according to claim 2, is characterized in that, the stirring vane rotating speed of mixing device is that per minute 0.2～5 turns.

4. powder delivery system according to claim 1, it is characterized in that, vertical disc feeder is provided with the feed rotor that comprises 4～8 independent cells, between each cell, separated by vertical riser, vertical disc feeder is by the rotation of feed rotor, the mass transport that feed end is entered is to discharge end and be expelled in the material inlet of fluid bed activating apparatus, and by controlling the operational throughput of feed rotor speed adjustment vertical disc feeder.

5. powder delivery system according to claim 4, is characterized in that, feed rotor stretches out the housing of vertical disc feeder in the time rotating to discharge end one side, stretches in the material inlet of fluid bed activating apparatus.

6. according to the powder delivery system described in claim 1 or 4, it is characterized in that, the material inlet of fluid bed activating apparatus is positioned at interface 400～800mm scope on fluid bed activating apparatus emulsion zone.

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