KR980008334A - Partition separation type charging separator - Google Patents

Abstract

The present invention relates to a particle separation charger type separator. More specifically, the present invention comprises a triboelectrification unit capable of triboelectrically charging a powder according to the particle size of the powder by a centrifugal separation method, and an electrostatic separation unit having a slidable structure, whereby a large amount of briquettes in coal fly ash The present invention relates to a rotatable separating device which can be separated into a plurality of rotors. An inlet 101 for supplying coal fly ash is formed at the upper end of the granular separation charger of the present invention, and a powder recovery hopper 43 for separating and recovering the separated fly ash and briquettes at the lower end. A plurality of contact charging plates fixed to the rotating shaft 24 and having a largest pore are installed on the upper end of the rotating shaft 24 and a pore size is sequentially reduced to the lower portion thereof, A contact charging matrix plate 23 which is stacked on the rotating shaft 24 and a contact charging matrix plate 23 which is installed on the upper end of the rotating shaft 24 to feed the coal fly ash supplied from the separating device inlet 101 to the contact charging matrix plate 23 A contact charging matrix plate rotating motor 22 for rotating the contact charging matrix plate 23 and a moving magnet plate rotating motor 22 for moving the contacted charged particles by the contact charging matrix plate 23, And a coal fly ash discharge port 26 for discharging the fly ash charged in contact with the electrostatic separator 30 to the electrostatic separator 30 at one side of the contact charging matrix plate 23 A frictional charging unit 20 for making contact with the fly ash by negative centrifugal force and negative fly ash by positively separating the powder supplied from the separator inlet 101, An electrode plate 33 having an inlet 31 communicating with the coal flyash 26 of the triboelectrification unit 20 and a slider structure whose upper portion is raised from the lower portion to be inclined, And a separate partition plate (32) for providing a moving and separating space for separating the powder, a guide plate (32) for guiding the complete separation of the main body from the lower part of the separate plate, A powder separator for preventing the above- And a vibrator for vibrating the electrode plate 33 and the separated support plate 32 formed at the lower portion of the plate so that the coal fly ash supplied from the contact charging unit 20 and the non- The electrostatic separation portion 30 is integrally formed.

Description

Partition separation type charging separator

FIG. 1 is an overall process flow diagram illustrating a coal seperation process according to the present invention; FIG.

FIG. 2 is a schematic vertical cross-sectional view of the particle separation charger type separator of the present invention. FIG.

FIG. 3 is an enlarged cross-sectional view of the contact charging matrix plate of FIG. 2;

Fig. 4 is a cross-sectional view of the electrostatic separation portion of Fig. 2, Fig. 4 (A) is a cross-sectional view taken along the horizontal direction of the separation supporting plate, Fig. 2 is a sectional view of the outlet side of the electrostatic separator according to the BB line of Fig. 2; Fig.

DESCRIPTION OF THE REFERENCE NUMERALS

10: Powder supply device 20: Friction charging part

21: contact charging plate guiding portion 22: contact charging magnet plate rotating motor

23: contact charging matrix plate 24:

30: electrostatic charge separator 32:

33: electrode plate 34: vibrator

35: Powder separator 40: Powder collecting part

41: coal fly ash collection pipe 42: unburned carbon recovery pipe

50: powder blower air blower 60:

70: fly ash reservoir 100: ash separator

The present invention relates to a particle separation charger type separator. More specifically, the present invention comprises a frictional charging unit capable of frictionally charging a powder according to the particle size of the powder by a centrifugal separation method, and an electrostatic separation unit having a slidable structure, wherein a large amount of briquettes in the fly ash To a separator which can be separated with high efficiency.

Various types of separators have been used for the separation of uncracked coal, which separates impurities from coal fly ash, and the coal refining process.

Among them, coal fly ash generated before and after combustion of coal can be said to be very useful. When recovering pure coal fly ash with less than 3% unburned carbon content, it can be effectively used for concrete admixture, lightweight construction material and embankment .

Generally, in the case of bituminous coal, the amount of fly ash is about 6 to 20%, but the amount of coal fly ash in Korea is about 40 to 60%. In addition, the coal fly ash produced in Korea contains about 7 to 14% of unburned carbon. In order to obtain the pure coal fly ash as described above, it is absolutely necessary to separate and recover unburned carbon in the coal refining process and coal fly ash.

However, most of the advanced fly ash separation processes developed until recently are wet processes designed to be used in coal production plants. Therefore, in order to commercially use the refined fly ash product according to the conventional fly ash separation process, dehydration and drying of the fly ash product are indispensably required. Therefore, this additional processing has made it difficult to economically produce coal fly ash, thus obstructing the industrial application of the above-mentioned advanced technologies.

Meanwhile, unlike the conventional wet separation and purification process, in the dry separation purification process, the coal fly ash is contacted with the inner surface of the friction charger in the friction charger to charge fly ash particles, It is a method of separating according to polarity.

In the case of the separation process of the powder mixture, the triboelector using the copper as the material and the electric field separation method are selected.

US Pat. No. 4,172,028 discloses an electrostatic separation apparatus capable of electrostatic separation of fine particles by vibration. However, in the above-described conventional electrostatic separation apparatus, the electrodes are arranged long in the lower portion, And since the powder is moved from the upper part to the lower part, it is difficult to increase the capacity of the powder processing apparatus in the case of a large amount of powder, resulting in poor economical efficiency. In addition, since most of the friction charger is used in the form of a matrix using copper as a material, not only the shape of the friction charger can be deformed, but also there is a possibility that it will corrode even a small amount of moisture.

SUMMARY OF THE INVENTION It is, therefore, an object of the present invention to provide a method and apparatus for separating fine coal from fly ash by a dry separation process with high efficiency, The present invention is to provide a particle separation charger type separator which can be economically treated at the same time.

In order to accomplish the above object, the present invention provides a separator for separating coal fly ash collected from an electrostatic precipitator and supplied by a powder feeder, And a contact charging plate having the largest pore is attached to the upper end of the case. The contact charging plate is fixed to a rotating shaft in a case of a rotating separator provided with a separating / recovering unit for separating and collecting separated fly ash and briquettes. A contact charging matrix plate in which a plurality of contact charging plates are stacked and formed in such a manner that the size of the pores is sequentially decreased to a lower portion, and a contact charging matrix plate attached to the upper end of the rotating shaft, A contact charging plate guide portion for guiding the contact charging plate, A movable passage for moving the rack span between the rotary driving means and the contact charging matrix plate and a moving passage for moving the powder charged by the contact charging matrix plate, and a discharge passage for discharging the fly ash from the electrostatic separation unit to the electrostatic separation unit And a frictional charging unit for charging the coal fly ash by negative centrifugal force and negative briquetting by positive centrifugal force, respectively, while separating the powder supplied from the inlet of the rotary separator, (-) electrode vertically arranged at the center while having an inlet communicated with a coal fly ash outlet of a triboelectrification unit and a slider structure having an upper portion sloped upward from the lower portion, and a negative electrode formed on both sides of the negative electrode (+) Electrode and a (+) electrode on both sides of the (-) electrode of the electrode plate and a A separation support plate provided vertically upward and spaced from the side ends of the (-) electrode and the (+) electrode at a predetermined interval in the horizontal direction to provide a moving and separating space for separating the powder, A powder separator extending horizontally from the lower end of the separator plate to a level above the separator plate to induce complete separation of the powder from the lower portion of the separator bottom plate to prevent mixing of the powder, And a vibrator connected to the electrode plate and the separator plate and vibrating the electrode plate and the separator plate so as to separate the powder attached to the electrode plate while moving the powder, Formed integrally with the static electricity separating portion for electrostatic separation of coal fly ash supplied from the contact charging portion and the briquettes And a gong.

The triboelectrification type electrostatic separation method used in the circuit breaker of the present invention is a method of separating and recovering a material by using a difference in work function, which is a unique electrical characteristic of each material. At this time, it is very important to selectively electrify the materials to be separated. Examples of the method for charging the material for this purpose include a corona discharge type, an electrostatic induction type, a contact type and a friction charging type. In the case of separating a mixture of fly ash having a high electric resistance and unburned carbon having a low electric resistance, contact and friction charging are effective methods.

However, when the particle size distribution range of the powder during the triboelectric charging of the powder is large, the triboelectric charge efficiency is increased, whereas the coarse particles exhibit poor charging efficiency. That is, the fine particles having a small particle size at the time of triboelectric charging move to the lower part of the powder having a large particle size distribution, and the contact surface area with the entire large surface is triboelectrified while the contact surface area with which the coarse particles can contact relatively is reduced. In order to solve the above-mentioned problems, in the present invention, contact charging is induced according to the particle size of the powder, and an electric field is efficiently formed in the electrode separating part composed of a single device as the charged powder, thereby effectively recovering coal fly ash do.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, the structure and effect of the particle separation charging type separator according to the present invention will be described in detail with reference to the accompanying drawings.

FIG. 1 is an overall process flow diagram showing the separation process of coal fly ash according to the present invention.

As shown in FIG. 1, coal fly ash collected in an electrostatic precipitator (not shown) is introduced into the separator 100 of the present invention by the vibration of the vibrator 2 in the electrostatic precipitator hopper 2.

The coal fly fed from the powder feeder 10 to the rotatable separator inlet 3 of the present invention descends to the contact charging matrix plate 23 in the frictional electrification portion 20 and is rotated by the rotation of the contact charging plate 23 And continues to make contact charging while passing through the moving passage 25 by centrifugal force to enter the electrostatic separation unit 30 through the frictional charging unit discharge port 26. [

The charged coal fly ash and the unburnt coal supplied through the inlet 31 of the electrostatic separation unit 30 are separated by the electric field applied to the electrode plate 33 in the electrostatic separation unit 30, The recovered coal fly ash is returned to the coal fly ash reservoir (70) by the pressurization of the air blower through a fly ash feed pipe (not shown), and the recovered unburned carbon Is transferred to the briquette storage 60 through the briquetting transfer pipe (not shown).

FIG. 2 is a schematic longitudinal sectional view of the particle separation charger type separator of the present invention. FIG.

As shown in FIG. 2, an inlet 101 for supplying coal fly ash is formed at the upper end of the particle separation charger type separator of the present invention, and a powder recovery unit for separating and recovering separated fly ash and non- A contact charging plate having the largest pore is fixed to the rotating shaft 24 in the case of the rotating separation shaft 24 provided with the separating and recovering unit 40 including the hopper 43, A contact charging matrix plate 23 in which a plurality of contact charging plates are stacked and laid down so that the contact charging plates 23 are sequentially stacked on the rotating shaft 24; A contact charging plate guide portion 21 for guiding the contact charging plate 23 to the charging matrix plate 23, a contact charging matrix plate rotating motor 22 for rotating the contact charging matrix plate 23, 23) A moving passage 25 for moving the contacted charged powder to the electrostatic separation unit 30 and a charged fly ash extending from the electrostatic separation unit 30 on one side of the contact charging matrix plate 23 to the electrostatic separation unit 30 For separating the powder supplied from the separating device inlet 101 and separating the powder from the fly ash by the centrifugal force to bring the fly ash to the negative charge and the unburnt charge to the positive charge An electrode plate 33 having an inlet 31 communicating with the coal flyash outlet 26 of the friction charging unit 20 and a slider structure having an upper portion inclined upward from the lower portion, A separation supporting plate 32 laid vertically upwards at a predetermined distance from the lower end of the electrode plate 33 to provide a moving and separating space for separating the powders and a separating plate 32 for separating the powder from the lower part of the separating supporting plate Powder to induce and prevent mixing of powders And a vibrator (not shown) for vibrating the electrode plate 33 and the separate support plate 32, which are formed at the bottom of the separate support plate, An electrostatic separation unit 30 for electrostatic separation of fly ash and unburnt coal supplied from the unit 20 is integrally formed.

In the lower part of the rotary separator of the present invention, a powder blowing air blower 50 for conveying the separated powders to the flyash reservoir 70 and the non-briquette storage 60 is installed.

In the rotary separator of the present invention, the frictional electrification unit 20 is integrally provided with the electrostatic separation unit 30 to prevent the discharge of the mobile phase charge and induce the contact electrification by the particle size to improve the charging efficiency. At this time, the powder is moved to the outside of the contact charging plate 23 by the centrifugal force resulting from the rotation of the contact charging matrix plate 23 made of the alloy plate, and the contact charging is performed. At this time, in the contact charging matrix plate 23, a plurality of contact charging plates having pores of 4 × 4 mm in the uppermost portion and 100mesh in the lowermost portion are provided in order to induce charging according to the size of the powder particles, Charged particles were charged at the upper part and moved to the lower part as the fine particles were charged. Therefore, the separating contact charge of the coarse particles and the fine particles is induced, thereby improving the separation efficiency in the electrostatic separator. In the case of the electrostatic separation unit 30, by providing the electrode plate 33 with an inclination of 30 to 45 degrees, the charged coal fly ash is moved from the upper part to the lower part by the vibration and the continuous separation is induced, A separation plate 32 and a powder separator (not shown) are provided to prevent mixing.

2, the fly ash flows into the separating device inlet 101 and is slightly inclined in the horizontal direction through the contact charging plate guiding portion 21, which is a portion for guiding fly ash to the contact charging plate 23. As shown in FIG. To the contact charging matrix plate (23). The fly ash moved to the contact charging plate 23 stays on the contact charging plate on the upper side and the contact charging plate on the lower side when the particle size is small.

At this time, the rotation speed of the contact charging plate 23 operates at a low speed in order to prevent the fly ash from being scattered deeply and to increase the residence time of the fly ash, and even when the rotation speed is high due to the high apparent density, In order to prevent the fly ash from moving to the upper contact charging plate, the contact charging plate 23 is preferably formed to be inclined downward by about 10 to 15 degrees from the horizontal. The contact charging plate 23 has a matrix structure. In order to prevent clogging of the pores due to the powder, a plurality of contact charging plates 23 are arranged in the vertical direction with increasing distance to the lower end of the contact charging plate 23 Perform air blowing periodically. In order to prevent corrosion of the contact charging plate 23, an alloy plate of Cu 60, Fe 20, and Ni 20 is preferably used as the contact charging plate.

The charged powder moves to the outside due to the centrifugal force in accordance with the rotation of the contact charging batten span 23 and is continuously contacted with the wall surface of the copper alloy plate along the external moving passage 25, And moves to the triboelectrification part discharge port 26 to enter the electrostatic separation part 30.

Thereafter, the charged fly ash and unburnt carbon that have entered the electrostatic separation unit 30 are separated and collected by the electrode plate 33 while being moved downward along the vibrating separating support plate 32, and then separated and collected by the vibration, Is returned to the powder recovery hopper 43 of the powder recovery unit 40 and is transported to the respective powder reservoirs 60 and 70 by the air blower 50.

FIG. 3 is an enlarged cross-sectional view of the contact charging matrix plate of FIG. 2;

3, as the contact charging plate 23 of the present invention moves from the uppermost contact charging plate 23a having the largest pore to the lower portion thereof, the pore size becomes smaller, Only the fine particles reach the fine particles 23j due to the movement of the particles due to the centrifugal force and the separation effect due to the net, and the charge amount becomes large due to the contact charging between the most powder particles and the contact charging plate. It has been found that the fine particles are difficult to collect and separate due to the particle interference between the fine powder particles in a general electrostatic separation apparatus. According to the constitution of the present invention, since the contact surface area of the powder is increased and the charge amount in the case of particle size separation charging becomes large, .

FIG. 4 is a schematic cross-sectional view of the electrostatic separation portion of FIG. 2, and FIG. 4 (A) and FIG. 4 And Fig. 4 (C) is a cross-sectional view at the outlet side of the electrostatic separator according to the BB line of Fig. 2.

As shown in FIG. 4, the electrostatic separation unit 30 of the present invention includes a plate-shaped (-) electrode 33b having a slider structure whose upper portion is raised from the lower portion and inclined, (-) electrodes 33b and (-) electrodes 33b of the electrode plate 33. The electrode plate 33 includes plate electrodes 33a formed on both sides of the negative (-) electrode 33b, (-) electrode 33b and (+) electrode 33a, which are vertically upwardly installed a certain distance from the lower end of the electrode plate 33 between the positive electrode 33a on both sides of the electrode 33b, A separation plate 32 which is spaced apart from the side ends at a predetermined interval in the horizontal direction and which provides a moving and separating space for separation of the powder and a separating plate 32 which is horizontally and horizontally arranged on the separating plate 32, And extends from the lower end of the separation plate 32 to a predetermined interval above the separation plate 32, A powder separator 35 for inducing the separation and preventing mixing of the powders and the electrode plate 33 connected to the separator plate 32 and formed below the separator plate 32, And a vibrator 34 for vibrating the electrode plate 33 and the separation plate 32 to separate the powder attached to the electrode plate 33 at the same time.

At this time, as shown in FIG. 4 (A), (+) electrodes 33a for collecting charged fly ash on both sides of the (-) electrode 33b for collecting the (+) charged unburned carbon, The distance between the (-) electrode 33b and the (+) electrode 33a and the (-) electrode 33b on the other side is made smaller. That is, since the separation amount of the lower part of the charged powder is lowered by collecting the upper part of the charged powder, the separation efficiency of the powder can be increased by narrowing the electrode distance toward the lower part.

As shown in FIG. 4 (B), the (-) electrode 33b forms an electric field on both sides, and the separation plate 32 has a width of about 1/5 to 2/5 So that the powder that has fallen below the separation plate 32 is collected and separated at the lower end of the separation plate 32. At this time, the (-) electrode 33b is connected to the ground 37.

In the case of the charged powder, the powder charged with the centrifugal force due to the rotation of the contact charging plate 23 of the frictional electrification part 20 is charged into the electrostatic separation part 30, The powder is collected until the inner and outer resistances of the powder are equal to each other, and then the remaining powder is continuously separated while moving down along the vibrating separating plate 32. At this time, the shaded portion in the drawing shows a portion that narrows inward while moving below the electrode plate 33. On the other hand, the powder collected and separated on the electrode plate 33 is discharged to the coal flyash collection pipe 41 and the unburned carbon recovery pipe (not shown) provided below the space between the electrode plate 33 and the separation plate 32 by the vibration of the vibrator 34 42).

As shown in FIG. 4 (C), in order to prevent the powders not separated from the final lower part of the center of the (+) electrode plate 33a and the (-) electrode plate 33b from remaining, A powder separator 35 is provided on the separation plate 32 so as to extend from the lower end of the separation plate 32 horizontally to the above electrode plate 33 to the upper 1/4 to 1/6 of the separation plate 32. [ . This is to induce complete separation of the powder at the lower part of the separation plate 32 and to prevent mixing of the powder at the lower part of the separation plate 32 when recovering the powder.

Further, it is preferable that the distance between the separate support plate 32 and the side ends of the electrode plates 33a and 33b varies depending on the component content of the powder. That is, when the unburned carbon content in the fly ash is 30% or less, the distance between the separation plate 32 and the (-) electrode 33b: the separation plate 32 and the (+) electrode 33a is kept at 1: 3 . When the unburned carbon content is 30% or more, the distance ratio is set to 1: 1.

On the other hand, the fly ash collected in the electrode plate 33 is separated into the coal fly ash recovery pipe 41 and the unburned carbon is separated and recovered in the unburned carbon recovery pipe 42. At this time, in order to prevent the powder separated by the electrode plate 33 from accumulating, it is preferable that the interval between the electrode plate 33 and the separation plate 32 is set so as to become larger toward the bottom.

In order to prevent efficient collection of fine particles and scattering of dust in the electrostatic separation unit 30, the movement of the charged powder due to the pressurization of air is eliminated, and the electrode plate 33 and the separation plate 33, (32), and dust attached to the electrode plate (33) is separated and recovered.

As shown in FIG. 4A, the (-) electrode 33b is provided in the middle of the positive electrode 33a and the separator plate 32 is made of an insulating material such as acryl Prevents electric field formation. The distance between the separating support plate 32 and the electrode plate 33 increases while moving to the lower portion and the distance between the (-) electrode 33b and the (+) electrode 33a decreases toward the lower portion This is because, as the distance of the electrode plate is shortened, the strength of the electric field becomes large, so that the undoped powder can be easily collected from the bottom. Also, since the amount of recovered water is increased in proportion to the amount of collected water, the area of the recovered water is also increased. In addition, by providing the powder separator 35 on the lower part of the separation plate 32, mixing of powders in the lower part can be prevented and the powder separation efficiency can be increased.

In the rotary separator of the present invention having the above-described configuration, the electrostatic separation unit 30 and the frictional electrification unit 20 are formed as a single unit, the centrifugal separation system is used as the frictional electrification system, 30), a slide structure is used. When a powder is contacted or triboelectrically charged, a substance having a low affinity for electrons loses electrons (+), while a substance having a high affinity for electrons gets electrons (-) charged, . ≪ / RTI > In other words, the briquettes move to the negative polarity with the positive telephone and the fly ash moves with the negative polarity to the positive polarity.

In the case of the centrifugal separator type frictional electrification unit 20, the fly ash flowing into the upper center of the contact charging matrix plate 23 moves to the lower portion of the contact charging matrix plate 23 according to the particle size, The slidable static electricity applying section 30 under the triboelectrification section 20 has the same area of the coal fly ash collecting electrode and the unburned coal collecting electrode and the interval between the flat plate electrode 33b and the positive electrode 33a Is a device system that controls the intensity of an electric field, which is formed to be stronger toward the bottom, to the gap distance and voltage by constituting the upper end to be 15 cm and the lower end to be 10 cm.

The fly ash charged by the (-) charge by the triboelectrification unit 20 reaches the (+) electrode 33a and the charge in the fly ash is gradually discharged. Therefore, the fly ash layer When the thickness of the fly ash layer becomes thick, it is separated and removed from the collecting pole by vibration and drops to the hopper. The reason why the area of the (-) electrode 33a is relatively the same is that the current flowing between the positive electrodes is made constant and the surface area of the microbial coal is increased.

As an example of the configuration of the apparatus, the interval between the electrodes is set to 15 cm at the upper portion and 10 cm at the lower portion, and an electric field is formed before and after the electrode plates are provided on both sides of the (-) pole. At this time, the applied voltage shows optimum efficiency at 35 to 40 kV, and the electric field between the electrodes is 2 to 5 kV / cm. The above-described structure is a system for forming a strong electric field by reducing the electric resistance in the electrode and the unburnt layer when the content of unburned carbon in the fly ash is 13% or more, and facilitating the conduction of current to the fly ash collector electrode.

Hereinafter, the size and the processing capacity of the particle separation and separation type separator according to the present invention will be described by way of examples.

[Example]

In the case of the friction charging section 20, as shown in FIG. 3, ten contact charging matrix plates 23 having a radius of 40 cm are installed vertically. At this time, the size of the contact charging matrix plate 23 is 23a: 4x4mm, 23b: 3x3mm, 23c: 2x2mm, 23d: 1x1mm, 23e: 50mesh, 23f: 60mesh, 23g: 70mesh, 23h: 80mesh, 23i: 90mesh, and 23j: 100mesh are used, and they are installed at an inclination of 10 to 15 degrees with respect to the horizontal direction to prevent scattering of fine particles, And the clogging of the torsion net was prevented. The vertical intervals between the contact charging matrix plates 23 were set to 1 cm from 23a to 23d and 1.5 cm from 23e to 23j, respectively.

On the other hand, in the case of the electrostatic separation unit 30, the (+) coal aspiration collecting electrode 33a is (4) flat plate electrodes 20 cm long and 100 cm long, (-) micro briquette collecting electrode 33b was installed at a flat size of 20 cm in width and 100 cm in length. In addition, the vibrating separator plate 32 is installed at a slope of 35 degrees from the horizontal, thereby increasing the retention speed of the powder in the electrostatic separator, thereby enhancing the separation efficiency of the powder. The inclination of the powder collecting tubes (41, 42) was adjusted by a slope of 80 ° so that gravity could be recovered properly. A powder separator 35, which is a triangular tetrahedron, is provided from the lower end of the separation plate 32 to the lower 1/6 point to prevent the powder not separated from the lower portion from remaining. In addition, the gap between the electrode plate 33 and the separator plate 32 is formed to be equal to 1 cm at the powder inlet of the upper part, but is made larger as it goes downward. In the lower portion of the electrode plate 33, the gap between the (+) electrode plate 33a and the separation plate 32 is 3.5 cm, the (-) electrode plate 33b and the separation plate 32) was set to be 1.5 cm. In order to facilitate separation and recovery of the powder from the lower end of the separation plate 32, the separation plate 32 is provided at a point 1/5 upward from the lower end of the electrode plate 33. Electrode spacing induced different electric field intensities at the upper 15 cm and the lower 10 cm.

The electrostatic separation of the mobile phase of the present invention exhibits an electric field strength of 2.5 to 4 kV / cm at an application voltage of 40 kV and an electrode gap of 15 cm at the top and 10 cm at the bottom. This increases the intensity of the electric field as it goes down. The maximum efficiency appears at a voltage of 40 kV, which can be maintained without excessive sparking, and a high electric field increases the force of the particles to increase the speed of movement of the particles. The gravity acting on the aggregate particles in the powder flow between the electrodes of the slide type electrostatic separation unit is generally negligible as compared with the electric force and the viscous force. However, the powder separated and recovered by the attachment and vibration of the particles, So that continuous separation is achieved. On the other hand, the apparent density of the moving phase of the inlet is 0.4 to 0.6 g / cm 3, the apparent density of the mobile phase at the coal fly ash outlet is 0.34 to 0.53 g / cm 3, It was easy to predict that it was captured.

The electrostatic separation apparatus of the present invention was operated at a treatment capacity of 3.5 to 4 ton / hr, and the unburned carbon in the fly ash was 13% or more, and the operating conditions for the separation efficiency of 95% or more were as follows:

Friction charging part: Friction charging part Contact rotation speed of charging plate: 60 to 90 rpm, Retention time in friction charging part: 5 to 12 seconds (depending on particle size), Friction charging amount: 1.92 × 10 ^-3 C / kg, particles discharged from the lower part of the outlet: -1.5 × 10 ^-3 C / kg

Electrostatic separation unit: (+) Flat plate electrode: 20 cm long, 100 cm long, (-) Flat electrode: 20 cm wide, 100 cm long Applied voltage: 40 kV, : The height of the upper 15 cm, the lower 10 cm, the electric field intensity: 2.5 to 4 kV / cm, the slope of the electrode: 30 ° to 45 °, the slope of the powder recovery tube: 80 °, the apparent density of the mobile phase at the inlet: 0.4 to 0.6 g / , The apparent density of mobile phase at the coal fly ash exit: 0.34-0.53g / ㎤.

In the electrostatic separation apparatus of the present invention, since the frictional electrification unit and the electrostatic separation unit are integrally formed, the apparatus can be downsized, and the contact charging is performed in accordance with the separation of the particles in the frictional electrification unit. have.

In addition, since the electrode plate can be dropped by 10 cm or more, the treatment capacity of the powder can be increased, and when the conventional electrode plate is installed in parallel vertically, the separated coal fly ash and unburnt carbon are mixed at the bottom of the electrode plate, Whereas in the present invention, the electrode plate is inclined at an angle of 30 to 45 ° and a powder separator is provided on the separated support plate, thereby overcoming the problems of the prior art described above.

The above-described separator of the present invention can be widely applied not only to purification of iron sulfide (FeS ₂ ) in coal but also to separation of a mixture such as separation of minerals which may be charged. Particularly, it is useful for a briquette separation process for separating impurities from coal fly ash and a coal refining process. Further, with the electrostatic separation apparatus of the present invention, it is possible to recover the pure coal fly ash having the unburned carbon content of about 3% or less before and after the combustion of the coal, so that it can be used as a concrete admixture, a lightweight construction material and an embankment.

As described in detail above, the granular separation charging type separator according to the present invention can separate fine briquettes in coal fly ash by a dry separation process with high efficiency, and can efficiently and economically treat a large amount of fly ash with a small apparatus It is confirmed that it can do.

Claims (7)

An apparatus for separating coal fly ash collected from an electrostatic precipitator and supplied by a powder feeder, comprising an inlet for supplying fly ash to the upper end of the fly ash separated from coal briquettes A plurality of contact charging plates, which are fixed to the rotating shaft and have a largest pore and which are sequentially reduced in the lower portion of the contact charging plate, A contact charging plate guide portion attached to the upper end of the rotating shaft to guide the fly ash supplied from the inlet of the separating device to the contact charging matrix plate; A contact charging matrix plate rotating drive means, and a contact charging matrix plate, And a coal fly ash outlet for discharging the fly ash charged in contact with the electrostatic separation unit to the electrostatic separation unit at one side of the contact charging matrix plate, A friction charging unit for contact charging the coal fly ash by centrifugal force and negative briquetting by positive centrifugal force while separating the powders separated by the centrifugal force, an inlet communicating with the coal fly ash outlet of the above friction charging unit, (-) electrode arranged vertically at a center with a slider structure formed to be sloped upward, and a plate-shaped (+) electrode formed at a predetermined interval on both sides of the (-) electrode, (-) electrode and a (+) electrode on both sides of the (-) electrode, and is arranged vertically upward by a certain distance from the lower end of the electrode plate, A separation plate provided at a predetermined interval in the horizontal direction to provide a moving and separating space for separating the powder; and a separator provided on the separator plate horizontally and horizontally from the lower end of the separator plate, A powder separator extending from the lower part of the separation plate to induce complete separation of the powder from the lower part of the separation plate and preventing mixing of the powder, And a vibrator for vibrating the electrode plate and the separating plate so as to separate the powder attached to the electrode plate. The electrostatic chuck for electrostatic separation of the coal fly ash from the contact charging unit by the electric field formation, And the separating part is integrally formed. The particle separation charger as set forth in claim 1, wherein the plurality of contact charging plates are inclined at an angle of 10 to 15 degrees in a horizontal direction. The size separating and charging type separating device according to claim 1, wherein the plurality of contact charging plates are vertically spaced from each other to a lower end of the contact charging plate. The separator according to claim 1, wherein an alloy plate of Cu 60, Fe 20, and Ni 20 is used as the plurality of contact charging plates. The apparatus of claim 1, wherein an interval between the electrode plate and the separation plate is increased toward the bottom of the electrode plate. [3] The method according to claim 1, wherein the gap between the (-) electrode of the electrode plate and the (+) electrode spaced apart from the positive electrode by a predetermined distance decreases toward the bottom of the electrode plate Separation device of granular separation type. The apparatus as claimed in claim 1, wherein a distance ratio between the separation plate and the electrode plate is varied depending on the content of the powder. ※ Note: It is disclosed by the contents of the first application.