JP2013139005A - Dry separation method and dry separator - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a dry separation method capable of attaining the continuous separation of separation objects at a low cost and in an environmentally friendly manner.SOLUTION: This dry separation method includes supplying separation objects into a solid/gas fluidized bed where powder is fluidized, introducing gas dispersed in the solid/gas fluidized bed, and separating the separation objects by using the apparent density of the solid/gas fluidized bed, wherein the recovery rate of the separation objects is changed according to the specific gravity difference of the separation objects. In a preferred embodiment of this dry separation method, when the specific gravity of separation of the solid/gas fluidized bed is Dp, the separation object that has a specific gravity outside a range of Dp±0.2 is recovered at a faster speed than the separation object that has a specific gravity within the range of Dp±0.2.

Description

  The present invention relates to a dry separation method and a dry separation apparatus.

  Industrial products composed of various materials, mineral resources, and industrial wastes contain various different components. Such separation for each component is necessary for refining mineral resources, recycling resources, and the like.

  To date, wet separation methods and dry separation methods are mainly known as separation methods.

  For example, as a dry separation method, a fluidized bed is formed by injecting gas into powder as a fluidizing medium, and coal particles are injected into the solid-gas fluidized bed to float coal particles with a density smaller than the apparent density of the fluidized bed. There is known a dry coal separation method in which large density coal particles are settled and separated (Patent Document 1).

JP2000-61398

  However, the dry separation method has problems such as high apparatus cost and low efficiency. In addition, the wet separation method has problems such as environmental pollution due to waste liquid treatment, and it cannot be used where water resources are small, and requires a waste liquid treatment or a drying step after separation.

  In addition to the target component, most of the cases where the separation target contains impurities. However, a method for continuously recovering the target component while removing the impurities has not been known so far.

  In the wet separation method, the separation specific gravity is relatively easy to prepare during operation, whereas in the dry separation method, it is not always easy.

  Then, this invention is providing the dry-type separation method and dry-type separation apparatus which can isolate | separate a separation target continuously, and are low-cost and environmentally friendly. Another object of the present invention is to provide a dry separation method and a dry separation apparatus that can adjust the separation specific gravity during operation.

  The inventors noticed that a solid-gas fluidized bed obtained by fluidizing powder has properties similar to liquids having characteristics such as density and viscosity, and in particular, objects having various densities in the fluidized state. As a result of examining the behavior of the present invention, the present inventors have found a dry separation method and a dry separation apparatus of the present invention.

  That is, in the dry separation method of the present invention, an object to be separated is introduced into a solid-gas fluidized bed in which powder is fluidized, a gas dispersed in the solid-gas fluidized bed is introduced, and an appearance of the solid-gas fluidized bed is obtained. A dry separation method for separating an object to be separated using density, wherein a recovery speed of the object to be separated is changed according to a difference in specific gravity between the objects to be separated.

  In a preferred embodiment of the dry separation method of the present invention, when the separation specific gravity of the solid-gas fluidized bed is Dp, the separation object having a specific gravity outside the range of Dp ± 0.2 is Dp ± 0.2. It collect | recovers at a speed | rate faster than the said isolation | separation target object which has specific gravity in the range of these.

  In a preferred embodiment of the dry separation method of the present invention, when the separation specific gravity of the fluidized bed is Dp, the separation object having a specific gravity outside the range of Dp ± 0.1 is Dp ± 0.1. It collect | recovers at a speed | rate faster than the said isolation | separation target object which has specific gravity in the range of these.

  In a preferred embodiment of the dry separation method of the present invention, the gas is introduced through a gas dispersion plate made of a porous material.

  In a preferred embodiment of the dry separation method of the present invention, the porous material is a punching plate.

  In a preferred embodiment of the dry separation method of the present invention, the powder is fluidized by blowing air from the lower part of the solid-gas fluidized bed.

Further, in a preferred embodiment of the dry separation method of the present invention, it is characterized in that air blowing is performed under a condition of air permeability of 5.0 (cm ³ / s) / cm ² or less.

Further, in a preferred embodiment of the dry separation method of the present invention, when the superficial velocity is u ₀ and the minimum fluidization superficial velocity of the powder is u _mf , u ₀ / u _mf is in the range of 1-4. It is characterized by performing ventilation.

  In a preferred embodiment of the dry separation method of the present invention, the apparent density of the solid-gas fluidized bed is set between the maximum density and the minimum density of each component in the separation object to be separated. To do.

  In a preferred embodiment of the dry separation method of the present invention, the powder is composed of unibeads, glass beads, zircon sand, polystyrene particles, steel shot, silica sand, alumina sand, and a powder having a density comparable to these. At least one selected from the group.

  Further, in a preferred embodiment of the dry separation method of the present invention, the separation object is automobile shredder dust, home appliance shredder dust, and other industrial waste, general waste, ore coal, rare earth, And

  In a preferred embodiment of the dry separation method of the present invention, the ores are iron ore, nickel ore, copper ore, limestone, or rare metal-containing ore.

  In a preferred embodiment of the dry separation method of the present invention, the average particle size of the powder is 30 to 500 μm.

  Also, in a preferred embodiment of the dry separation method of the present invention, the components constituting the solid-gas fluidized bed are introduced, then the separation object is introduced, and then the components constituting the solid-gas fluidized bed are introduced. Thus, the separation object is put into between the components constituting the solid-gas fluidized bed.

  In a preferred embodiment of the dry separation method of the present invention, the powder is a mixed medium of at least two kinds.

  In a preferred embodiment of the dry separation method of the present invention, the powders have different particle sizes.

  In a preferred embodiment of the dry separation method of the present invention, the powder is composed of a magnetic powder and a non-magnetic powder.

  Further, the dry separation apparatus of the present invention is a solid-gas fluidized bed formed by powder, a separation object charging means for charging a separation object, and the separation object is separated and floated by the solid-gas fluidized bed. The first and / or second recovery means, comprising: a first recovery means for recovering levitated matter; and a second recovery means for recovering the sediment which is separated and settled by the solid-gas fluidized bed. The means has a mechanism for changing the recovery speed of the separation object according to the specific gravity difference of the separation object.

  Further, in a preferred embodiment of the dry separation apparatus of the present invention, the first and / or second recovery means is outside the range of Dp ± 0.2 when the separation specific gravity of the solid-gas fluidized bed is Dp. The separation object having a specific gravity of 1 is recovered at a higher speed than the separation object having a specific gravity within the range of Dp ± 0.2.

  Further, in a preferred embodiment of the dry separation apparatus of the present invention, when the first and / or second recovery means has a separation specific gravity of the fluidized bed as Dp, a specific gravity outside the range of Dp ± 0.1. The separation object having a specific gravity is recovered at a faster rate than the separation object having a specific gravity within a range of Dp ± 0.1.

  In a preferred embodiment of the dry separation apparatus of the present invention, the recovery directions for recovering the separation target of the first and / or second recovery means are different from each other.

  Further, in a preferred embodiment of the dry separation apparatus of the present invention, it is further characterized by having dust collection and recovery means for recovering dust collected when the separation object is separated and recovered.

  In a preferred embodiment of the dry separation apparatus of the present invention, the first and / or second recovery means recovers the powder together with the floated material and / or sediment.

  In a preferred embodiment of the dry separation apparatus of the present invention, the solid-gas fluidized bed further includes a separation means for separating the floated material and the sediment.

  Moreover, in a preferred embodiment of the dry separation apparatus of the present invention, the first and / or second recovery means recovers the floated material and / or sediment by a recovery container provided in the solid-gas fluidized bed. It is characterized by doing.

  In a preferred embodiment of the dry separation apparatus of the present invention, the first and second recovery means are based on a suction mechanism.

  Further, in a preferred embodiment of the dry separation apparatus of the present invention, it further comprises a specific gravity measuring means for measuring the specific gravity of the powder and a separating means for separating at least two kinds of powders in the solid-gas fluidized bed. It is characterized by that.

  Further, in a preferred embodiment of the dry separation apparatus of the present invention, the setting means for setting the separation specific gravity of the solid-gas fluidized bed, and the powder mixing ratio based on the separation specific gravity set by the setting means. It has a mixing ratio calculating means for calculating, and a powder supplying means for supplying the powder into the solid-gas fluidized bed based on the mixing ratio calculated by the mixing ratio calculating means.

  According to the present invention, there are advantageous effects that the apparatus cost is low, the efficiency is high, the waste liquid treatment and the drying process after separation are unnecessary, and there is almost no influence on the environment.

  Further, according to the present invention, since it is so-called dry separation, it can be used even in a place where water resources are small.

The schematic diagram in one embodiment of the device which isolate | separates a separation target object is shown. The schematic diagram in one embodiment of the present invention which collects the ingredient of a separation subject is shown. The schematic diagram in one embodiment of the present invention which collects the ingredient of a separation subject is shown. The schematic diagram in one embodiment of the present invention which collects the ingredient of a separation subject is shown. The schematic diagram in one embodiment of the present invention which collects the ingredient of a separation subject is shown. The schematic diagram in one embodiment of the present invention which collects the ingredient of a separation subject is shown. The schematic diagram in one embodiment of the present invention which collects the ingredient of a separation subject is shown. The schematic diagram in one embodiment of the present invention which collects the ingredient of a separation subject is shown. The schematic diagram in one embodiment of the present invention which collects the ingredient of a separation subject is shown. The schematic diagram in one embodiment of the present invention which collects the ingredient of a separation subject is shown. The schematic diagram in one embodiment of the present invention which collects the ingredient of a separation subject is shown. The schematic diagram in one embodiment of the present invention which collects the ingredient of a separation subject is shown. An example of a selection process is shown. The schematic of the automatic specific gravity preparation apparatus in one embodiment of this invention is shown.

  The principle of separation of the present invention will be described as follows. That is, powder is fluidized, and the separation target is mainly used by utilizing a powder fluidization medium similar to liquid specific gravity sorting, in other words, a solid-gas fluidized bed (hereinafter also simply referred to as fluidized bed). It separates according to density. In the present invention, in addition to this, it is one of the features that the separation target is recovered by changing the recovery speed of the separation target in accordance with the specific gravity difference of the separation target. As described above, the separation target can be quickly recovered by changing the recovery speed of the separation target based on the specific gravity difference of the separation target. In other words, when the specific gravity of the separation target and the separation specific gravity of the fluidized bed are separated from each other, the separation is relatively easy, and even if the fluidized bed becomes somewhat unstable, the recovery is easy. Can be quickly separated and collected by increasing the collection speed, but if the specific gravity of the separation object and the separation specific gravity of the fluidized bed are close to each other, the collection speed is slowed down to stabilize the fluidized bed. Carefully collect the objects to be separated. In this way, it is possible to separate the floated material and the sediment with high accuracy while considerably preventing the harmful effects of contamination.

  That is, as a result of studying how to achieve a large amount of a separation-treated product having a large capacity (for example, a processing capacity of 50 t / hr to 200 t / hr), the present inventors have found that We considered collecting fast and slow ones with separate discharge systems. According to the inventor's previous knowledge, an ideal fluidized bed can be realized in a batch apparatus, but in an actual apparatus, a recovery mechanism moves in the fluidized bed. Leads to. When moving beyond a certain speed, the sorting accuracy can be extremely reduced. Conversely, it has been found that the separation accuracy is not greatly disturbed even if the discharger speed in the fluidized bed is increased to some extent in the region where the separation speed is high.

  Therefore, it has been found that those that are separated immediately after feeding can increase the discharge capacity by increasing the speed of the discharge mechanism. On the other hand, it is desirable that the separation accuracy is within a range that does not disturb the separation accuracy. From the above, it has been found that it is possible to increase the sediment discharge capacity and the processing capacity, and the present invention has been completed based on such knowledge.

  Here, in this specification, the apparent density of a fluidized bed and the separation specific gravity are used as similar terms, but each has a different definition. The apparent density is literally the apparent density of the fluidized bed itself, whereas the separation specific gravity indicates how much specific gravity is separated as a result of separation into two products.

  In the specific gravity separation industry, the specific gravity (Dp) is the specific gravity that should generally rise up, but the ratio of misdistribution to sediment is 50%. Also in this specification, it is used in such a meaning. In this case, Dp can also be displayed as D50. Therefore, as a result, the apparent density and the separation specific gravity of the fluidized bed may coincide, but usually do not coincide.

  In practice, the apparent density of the fluidized bed is adjusted so as to achieve the target separation specific gravity. Analyze the results of actual separation to determine the separation specific gravity. As a method of obtaining, a distribution rate curve is created, and a specific gravity corresponding to a distribution rate of 50% can be set as a separation specific gravity. That is, with D50, that is, the specific gravity corresponding to the distribution ratio: 50% can be set as the separation specific gravity Partition Density or Separation Density. The creation of the allocation rate curve is also introduced in the following examples.

  In a preferred embodiment of the dry separation method of the present invention, when the separation specific gravity of the solid-gas fluidized bed is Dp, the separation object having a specific gravity outside the range of Dp ± 1, preferably Dp ± 0.5 is used. , Dp ± 1, preferably at a faster rate than the separation object having a specific gravity in the range of Dp ± 0.5. Further, in a preferred embodiment of the dry separation method of the present invention, when the separation specific gravity of the solid-gas fluidized bed is Dp, the separation object having a specific gravity outside the range of Dp ± 0.2 is Dp ± 0. 2. Collect at a faster rate than the separation object having a specific gravity in the range of 2. That is, it is a case where separation occurs when the specific gravity of what should sink is Dp + 0.2 or more and the specific gravity of what should float is Dp−0.2 or less. In this case, strictly speaking, it is not a 100% separation, but is an effective condition when it is desired to suppress misdistributions to each other to 5% or less. That is, this is an embodiment in which the amount of the object to be settled strays into the levitated matter is 5% or less, and conversely, the amount of the levitated object strays into the sediment is also suppressed to 5% or less.

  In a preferred embodiment of the dry separation method of the present invention, when the separation specific gravity of the fluidized bed is Dp, the separation object having a specific gravity outside the range of Dp ± 0.1 is Dp ± 0.1. Is collected at a faster rate than the separation object having a specific gravity within the range of That is, it is a case where it separates when the specific gravity of what should sink is Dp + 0.1 or more and the specific gravity of what should float is Dp-0.1 or less. In this case, strictly speaking, it is not 100% separation, but is an effective condition when it is desired to suppress misdistribution to each other to 25% or less. That is, this is an embodiment in which it is desired to suppress the amount of what is to sink to the levitated object to 25% or less, and conversely to suppress the amount of the levitated object to be lost to the sediment.

  Further, in the present invention, the specific gravity difference between the one to be settled and the one to be floated is 0.2 or more (the separation specific gravity is 0.1 or more larger than the specific gravity of the one to be levitated, or 0. It has been found that when it is smaller than 1), it tends to float or sink relatively quickly. Therefore, this value can be used as one separation criterion. In addition, within the range of Dp ± 0.1, when the specific gravity difference between the sedimentation and the floatation is 0.1 or less, even if Dp is set to the middle, the specific gravity difference with Dp is There is a tendency that the possibility that the amount of straying into the mutual product becomes 25% or more becomes high. Therefore, in order to separate with higher accuracy, separation with the fluidized bed stabilized is ideal. That is, it is necessary to devise measures such as reducing the collection speed. It can be set as appropriate according to the desired separation object and the separation accuracy of the separation object.

  In addition, although it cannot generally be said according to conditions, such as the powder to be used and the separation object to be separated, generally, the sedimentation separation rate is considered as follows. That is, the separation speed is basically defined by the specific gravity difference between the object size and Dp. It can be considered that the sedimentation speed is fast if the specific gravity of the floating object and the sedimentation object of the separation object is Dp ± 0.1 or more, and moderate if it is Dp ± 0.1 to 0.05. This also means that it is necessary to consider the stabilization of the fluidized bed, in particular, when the specific gravity of the levitated matter and the subsidence of the separation target is Dp ± 0.1 to 0.05.

  In addition, the solid-gas fluidized bed is intended to have a property similar to a liquid by fluidizing powder.

  First, the concept of separation by a solid-gas fluidized bed will be described below. When a gas is sent to the powder and fluidized by floating, the fluidized bed made of the powder exhibits the same behavior as the liquid. Therefore, the apparent density ρfb of the fluidized bed is expressed by the following equation.

ρfb = Wp / Vf = (1-εf) ρp
Here, Wp is the powder weight of the fluidizing medium, Vf is the volume during fluidization, εf is the porosity during fluidization, and ρp is the powder density of the fluidizing medium.

  When the separation object of density ρs is mixed in the fluidized bed having such an apparent density ρfb, the separation object component of ρs <ρfb floats on the upper part of the fluidized bed, and the separation object component of ρs> ρfb is It settles in the lower part of the fluidized bed. The separation object component of ρs = ρfb floats in the middle part of the fluidized bed. Using this fact, the specific gravity of the separation object is selected.

  In this way, it is possible to separate each component in the separation object. As a result, the separated components can be easily recycled.

  The separation object that can be separated in the present invention is not particularly limited. The separation object is characterized by automobile shredder dust, home appliance shredder dust, and other industrial waste, general waste, ore coal, and rare earth. In addition to various mineral resources and industrial products, examples of separation objects include shredder dust, waste, minerals, agricultural products, plastics, metals, and the like.

  Moreover, in a preferred embodiment, as the separation object, ores are iron ore, nickel ore, copper ore, limestone, or rare metal-containing ore.

  Various mineral resources include ores such as silica and wax, raw coal mined from coal mines, and shredder dust includes those from household waste, automobiles, home appliances, etc. be able to. In addition, although the separation target object derived from either may be used in this way, when the separation target object is dirty, it is preferable to separate it after washing. This is because, according to the separation method of the present invention, the components of the separation object are mainly separated by the difference in specific gravity, so that the specific gravity may vary if the separation object is dirty.

  In a preferred embodiment, the gas is introduced through a gas dispersion plate made of a porous material. Preferably, the porous material is a punching plate.

  In an embodiment of the dry separation method of the present invention, when purifying the separation object having a density larger than the apparent density of the solid-gas fluidized bed, the initial input position of the separation object is set to the intermediate point of the fluidized bed. It is preferable to set to the upper side. This means that if the object to be purified contains the object to be purified, and the object to be purified has a density greater than the apparent density of the solid-gas fluidized bed, the object to be separated including the object to be purified. If the initial position of the material is set above the midpoint of the solid-gas fluidized bed, noise (dust) other than what is to be purified remains at the top, and only the material to be purified is placed at a lower level with higher purity. This is because they can be separated.

  Similarly, when the material to be purified has a density smaller than the apparent density of the solid-gas fluidized bed, the initial position of the separation object containing the material to be purified is set below the midpoint of the solid-gas fluidized bed. In this case, noise (garbage) other than what is desired to be purified remains at the lower part, and only what is desired to be purified can be separated to the upper side with higher purity.

  In the present invention, continuous separation for each component is performed, for example, by changing the apparent density of the solid-gas fluidized bed or by arranging two or more solid-gas fluidized beds in series. Can do.

In order to change the apparent density of the solid-gas fluidized bed, the value of u ₀ / u _mf described later is changed, the powder used for the solid-gas fluidized bed is changed, or the particle size of the powder is changed, This can be done by changing the mixing ratio of the mixed powder.

Since the change in the apparent density depends on the type of the separation object, the apparent density is not necessarily decreased if the value of u ₀ / u _mf is increased. On the other hand, when a powder having a high density used in the solid-gas fluidized bed is used, the apparent density of the solid-gas fluidized bed generally tends to increase. Further, when the particle size of the powder is increased, the apparent density tends to increase. Accordingly, if the apparent density is changed in consideration of these, continuous separation of each component becomes possible.

  In a preferred embodiment of the dry separation method of the present invention, the powder can be fluidized by blowing air from the lower part of the solid-gas fluidized bed. This is because more components can be separated. However, it is not intended to be limited to blowing from the lower part. For example, components having a relatively low specific gravity can be separated even if crosswinds are sent. When a component with a clearly low specific gravity is present, separation is possible with high efficiency because of a large scattering distance even in a crosswind. Therefore, after removing components having a low specific gravity by air classification using cross wind as a pretreatment for solid-gas fluidized bed selection, each component of the remaining separation target may be removed.

  When a component having a low specific gravity exists as an impurity in addition to the target component in the separation target, the impurity can be removed by the same procedure.

And in this invention, ventilation can be performed on the conditions whose air permeability is 5.0 (cm < ³ > / s) / cm < ² > or less. This is because stabilization of ups and downs can be achieved by controlling air permeability. Although not particularly limited depending on the object to be separated, the air permeability is 5.0 (cm ³ / s) / cm ² or less, preferably 3.0 (cm ³ / s) / cm ² or less, more preferably 1.0 (cm ³ / S) / cm ² or less.

In the present invention, when the superficial velocity is u ₀ and the minimum fluidization superficial velocity of the powder is u _mf , u ₀ / u _mf is one factor for controlling the separation. This is because, for example, by adjusting the superficial velocity, two components having very close density differences can be easily removed, and conversely, the superficial velocity can be increased for separating components having large density differences. This is because it can be separated in a short time.

  Generally, when the superficial velocity is set to be equal to or higher than the minimum fluidization superficial velocity and close to the minimum fluidization superficial velocity, the density distribution of the components of the separation object floating in the solid-gas fluidized bed becomes narrow, and the superficial velocity is reduced. When further increased, the density distribution of the components of the separation object floating in the solid-gas fluidized bed widens.

  Therefore, the present invention has an advantage that two components (two objects) having a small density difference, which has been conventionally difficult to separate, can be separated. In order to finely control the superficial velocity in this way, it is possible to use a material having low air permeability in the portion where the air in the lower part of the solid-gas fluidized bed is dispersed.

When components are roughly separated, the components can be basically separated into three types: levitation, position in the middle layer, and sedimentation. However, in the end, it is often the case that components with a small density difference that are difficult to separate are separated, so that the density distribution of the components located in the middle layer is made as small as possible so that the components float or settle. If the above u ₀ / u _mf is used, separation with higher separation accuracy and recovery rate can be performed.

The value of u ₀ / u _mf can be in the range of 1 to 4, for example. This is because a stable solid-gas fluidized bed can be formed within such a range. However, the present invention is not limited to this range, and the value of u ₀ / u _mf may be 4 or more when components having large density differences are rapidly separated.

When fluidizing a single powder, when separating components with a small density difference, the value of u ₀ / u _mf should be as close to 1 as possible, depending on the powder used. Is preferred. The value of u ₀ / u _mf can be 1 to 1.5, preferably 1 to 1.2, and more preferably 1 to 1.1.

When a plurality of powders are fluidized, it is preferable to carry out under a u ₀ / u _mf value such that the plurality of powders are mixed substantially uniformly. This is because the apparent density decreases toward the upper part of the solid-gas fluidized bed and the apparent density increases toward the lower part when the mixture is not substantially uniformly mixed. This is because the distribution tends to increase.

  In a preferred embodiment of the dry separation method of the present invention, the apparent density of the solid-gas fluidized bed is set between the maximum density and the minimum density of each component in the separation object to be separated. To do.

  Also, the type of powder is not particularly limited by the type of separation object to be separated, for example, powder, unibeads, glass beads, zircon sand, polystyrene particles, sand, steel shot, silica sand, alumina sand, And at least one selected from the group consisting of powders having similar densities.

  The average particle diameter of the powder to be used is not particularly limited, but from the viewpoint of fluidizing the powder at a relatively low superficial velocity and suppressing aggregation of the powder due to adhesion. 700 μm, preferably 30 to 500 μm.

  Also, in a preferred embodiment of the dry separation method of the present invention, the components constituting the solid-gas fluidized bed are introduced, then the separation object is introduced, and then the components constituting the solid-gas fluidized bed are introduced. Thus, the separation object is put into between the components constituting the solid-gas fluidized bed.

  Each component of the separation object separated as described above can be finally collected by an appropriate method by floating or sinking.

  Next, a dry separation method for adjusting the separation specific gravity during operation will be described. In order to arbitrarily change the separation specific gravity, for example, the powder may be at least two kinds of mixed media. It is desirable that the mixed medium (mixed powder) can be easily “separated” and “mixed” based on the difference in characteristics of each medium.

  Usually, each medium needs to be mixed appropriately without segregation, but a mixed medium can be made relatively easily in consideration of the particle size and specific gravity. However, it is usually difficult to separate a once mixed medium into a medium (powder) before mixing. On the other hand, in the present invention, separation and mixing can be successfully performed by utilizing properties of powder, for example, properties such as particle size and magnetism.

  That is, in a preferred embodiment of the dry separation method of the present invention, the powders have different particle sizes. For example, when two types of powders are used and the powders having different particle sizes are used, the two types can be separated and mixed according to the difference in particle size, for example, by sieving.

  For example, the condition is that the two types of media have different particle sizes and at least no common particle size. Then, both media can be separated by sieving. Specifically, for example, if a mixed medium of silica sand + iron powder is used, it is possible to cope with a mixed medium apparent specific gravity of 1.3 to 4.4.

  At the same time, when used as a mixing medium, the particle size distribution of silica sand is 300-100 μm, whereas the particle size distribution does not overlap if the iron powder is 50-70 μm. Accordingly, in the case of silica sand and iron powder, the mixed medium can be separated into two mediums by classification (sieving) between 100 μm and 70 μm, for example, 80 μm.

  In a preferred embodiment of the dry separation method of the present invention, the powder is composed of a magnetic powder and a non-magnetic powder.

  That is, one of the two media constituting the powder must be a magnetic material and the other must be a non-magnetic material. Then, both media can be separated by magnetic force. Silica sand is not a magnetic material, but iron powder is a magnetic material.

  Therefore, if paying attention to such a difference in properties of the powder, the mixed medium can be easily separated into two mediums. As described above, a medium (powder) once mixed can be separated into the original simple substance based on the difference in powder properties such as the particle size of the medium or magnetism.

  Next, the dry separation apparatus of the present invention will be described. The dry separation apparatus according to the present invention includes a solid-gas fluidized bed formed of powder, a separation object charging means for charging a separation object, and a levitated object in which the separation object is separated and floated by the solid-gas fluidized bed. And a second recovery means for recovering the sediment that has been separated by the solid-gas fluidized bed and settled, and the first and / or second recovery means comprises: And a mechanism for changing the recovery speed of the separation object in accordance with the specific gravity difference of the separation object.

  Regarding the solid-gas fluidized bed, the description in the dry separation method of the present invention described above can be referred to. The separation object input means is not particularly limited as long as the separation object can be input. In some cases, in order to stir the separation target, it may be fed through a stirring means such as a stirrer. Further, the first collecting means for collecting the floated material is not particularly limited as long as the floated material can be collected. Further, the second collecting means for collecting the sediment is not particularly limited as long as the sediment can be collected. Further, the mechanism for changing the recovery speed is not particularly limited as long as the recovery speed of the separation target can be changed according to the specific gravity difference of the separation target.

  The powder may be fed by a powder feeding means for feeding one or more powders, and a solid-gas fluidized bed is formed by the powders fed by the one or more powder feeding means. May be.

  Further, in a preferred embodiment of the dry separation apparatus of the present invention, the first and / or second recovery means is outside the range of Dp ± 0.2 when the separation specific gravity of the solid-gas fluidized bed is Dp. The separation object having a specific gravity of 1 is recovered at a higher speed than the separation object having a specific gravity within the range of Dp ± 0.2. Regarding the separation specific gravity Dp of the solid-gas fluidized bed, the description of the separation specific gravity in the dry separation method of the present invention described above can be referred to.

  Further, in a preferred embodiment of the dry separation apparatus of the present invention, when the first and / or second recovery means has a separation specific gravity of the fluidized bed as Dp, a specific gravity outside the range of Dp ± 0.1. The separation object having a specific gravity is recovered at a faster rate than the separation object having a specific gravity within a range of Dp ± 0.1.

  In a preferred embodiment of the dry separation apparatus of the present invention, the recovery directions for recovering the separation target of the first and / or second recovery means are different. By making the collection directions different, it becomes possible to reduce the bias of the granular medium by the discharger.

  Further, in a preferred embodiment of the dry separation apparatus of the present invention, there is further provided a dust collection / recovery means for collecting dust collected when the separation object is separated and collected. As a result, more accurate separation without impurities is possible.

  Further, in a preferred embodiment of the dry separation apparatus of the present invention, the first and / or second recovery means can be easily recovered because both the floated material and the sediment and the powder are clearly different in particle size. From the viewpoint that the floated material and sediment and the powder are separated and the powder can be circulated in the fluidized bed, the powder can be recovered together with the floated material and / or sediment.

  In a preferred embodiment of the dry separation apparatus of the present invention, the solid-gas fluidized bed further includes a separation means for separating the floated material and the sediment. By the separation means, it becomes possible to efficiently separate and collect the floated material and the sediment.

  Moreover, in a preferred embodiment of the dry separation apparatus of the present invention, the first and / or second recovery means recovers the floated material and / or sediment by a recovery container provided in the solid-gas fluidized bed. It is characterized by doing. Even with the collection container, it is possible to efficiently separate and collect the floated material and the sediment. If the collection container is sieved, powder, sediment, floated material, etc., depending on the purpose, for example, powder only, sediment only, floated material, or powder and sediment, powder It is possible to separate and recover the body and levitated matter or the like.

  In a preferred embodiment of the dry separation apparatus of the present invention, the first and second recovery means are based on a suction mechanism. The suction mechanism is not particularly limited as long as the floated material or the like can be collected.

  Note that the relationship between the size of the separation object and the processing capacity is as follows. That is, the particle diameter to be treated in the specific gravity separation technique using a fluidized bed is preferably as follows according to the actual apparatus performance.

  That is, the object to be separated is flat, such as plastics (away from the sphere, in other words, resistant to separation), etc. The target particle diameter is preferable, and more preferably 10 to 35 mm <the processing target particle diameter. Further, for example, in the case of a material having a relatively large sphericity (that is, a material having low resistance when separated) such as coal, iron ore, etc., 8 mm <the particle diameter to be treated is preferable, and more preferably, 8 ˜50 mm <treatment target particle diameter. Further, for example, in the case of metal (aluminum, copper, etc.), 2 mm <the particle diameter to be treated is preferable, and more preferably 2 to 50 mm <the particle diameter to be treated. This is due to the following reason. That is, the separation accuracy improves as the range of the particle diameter of the processing object is narrower. In addition, it can be said that the narrower one is better because the adjustment of the wind speed and layer thickness of the fluidized bed can be optimized to match the particle diameter. On the other hand, if it is narrowed, several size ranges must be processed separately (processing according to granularity), which increases the device cost. Accordingly, from such a viewpoint, it is an economical design to make the size range as wide as possible within the range satisfying the separation accuracy.

  Next, one embodiment of the dry separation apparatus of the present invention will be described with reference to the accompanying drawings. FIG. 1 is a diagram showing the ups and downs of an object in a solid-gas fluidized bed. 1 is an object lighter than the apparent density of the fluidized bed. 2 is a solid-gas fluidized bed. 3 is an object heavier than the apparent density of the fluidized bed. 4 is a separation tank. Reference numeral 5 denotes a gas dispersion plate. As is apparent from this figure, it can be seen that in the fluidized state of the powder, the object can be separated by the apparent density of the solid-gas fluidized bed.

  An example of the separation procedure is as follows. Glass beads, uni-beads, zircon sand, polystyrene particles, etc., which are fluidization media, are charged into the separation tank, and uniformly into the separation tank 4 from the lower surface of the separation tank 4 through the gas dispersion plate 5. Gas is fed and the powder is fluidized to form a fluidized bed. Therefore, when the separation object is introduced from the upper surface opening of the separation tank 4, the separation object component having a density higher than that of the powder to be used is settled. FIG. 2 shows a schematic diagram in one embodiment of the present invention for recovering the components of the separation object. In FIG. 2, 6 is a discharger A, 7 is a discharger C, 8 is a discharger E, 9 is a discharger B, 10 is a discharger D, 11 is a flow direction of floated material (or sediment), 12 is a sinker The direction in which the object (or levitated material) A flows, 13 is the direction in which the sediment (or levitated material) B flows, 14 is the direction in which the sediment (or levitated material) C flows, and 15 is the direction in which the sediment (or levitated material) E flows. The direction of flow, 16 indicates the direction of flow of sediment (or levitated matter) D, respectively. 11 is described as the direction in which the floated material flows. The levitated material moves in the upper layer of the fluidized bed according to the direction of arrow 11. At this time, the levitated material can be collected manually or automatically as appropriate. The sediment (Sinks A to E) can be discharged by the dischargers A to E, respectively. In this embodiment, from the viewpoint of reducing the bias of the fluid medium by the discharger, the collection of sediment or floated material by the discharger is collected in different directions. The collection speed of the sediment by the dischargers A to E can be changed depending on the specific gravity of the separation object, and is collected by changing the collection speed of the separation object according to the specific gravity difference of the separation object. It is possible. For example, various separation objects are included, and among them, those having a specific gravity outside the range of the separation specific gravity Dp ± 0.2 of the fluidized bed can be collected at a high speed. When the separation difference is large, separation is possible even if the fluidized bed is unstable, and it is possible to aim at shortening of the separation time by collecting such a separation object earlier at a high speed. If the collection speed of Sink: A to Sink: E is a variable speed in each of the sediment dischargers A to E, it can be collected according to the difference in specific gravity. Further, the division of the discharger can be determined based on the properties (specific gravity distribution) and separation specific gravity of the processed product. Further, the discharger speed can be optimized based on the properties (specific gravity distribution) of the processed product.

  The fluidized bed thickness can be optimized based on the separation difficulty of the processed product. Since the stability (uniformity) tends to decrease as the fluidized bed thickness increases, it is possible to increase the thickness in the case of easy separation. By doing so, the discharger speed can be increased, and as a result, the processing capacity can be increased. On the other hand, when the degree of separation difficulty is high, it is desirable to make the thickness of the fluidized bed as small as possible within the range in which the ejector functions.

  Although not shown, the air chamber also has an optimum size based on the medium used and the fluidized bed thickness in order to blow air through the dispersion plate to form a uniform fluidized bed.

  In FIG. 2, the flow of the float is described as 11 and the flow of the sediment as 12, 13, 14, 15, and 16, but the reverse, that is, the sediment flow is 11 and the float flow. May be 12, 13, 14, 15, 16.

  FIG. 3 shows a schematic diagram (when the apparatus is viewed from the horizontal direction) in one embodiment of the present invention for recovering the components of the separation object. In FIG. 3, 17 indicates the direction in which the float (or sediment) flows, and 18 indicates the direction in which the sediment (or float) flows. This indicates a normal type device among so-called scraper type continuous devices. The separation accuracy is increased by moving the floating and sinking materials in opposite directions. This type can also be collected by changing the collection speed in accordance with the specific gravity difference of the separation target.

  FIG. 4 shows a schematic diagram (when the apparatus is viewed from above) in one embodiment of the present invention for recovering the components of the separation object. In FIG. 4, 19 indicates the direction in which the float (or sediment) flows, and 20 indicates the direction in which the sediment (or float) flows. This indicates a power up type of so-called scraper type continuous device. This optimizes the sediment discharger speed according to the separation product properties and separation specific gravity. The sinking material discharge direction is a direction perpendicular to the floating material discharging direction, and the deviation of the granular medium by the discharging machine is reduced, so that the adjacent sinking material discharging machine discharge directions can be alternated. This type can also be collected by changing the collection speed in accordance with the specific gravity difference of the separation target.

  FIG. 5 shows a schematic diagram (when the apparatus is viewed from above) in one embodiment of the present invention for recovering the components of the separation object. In FIG. 5, 19 is the direction in which the float (or sediment) flows, 21 is the power unit (motor), 22 is the transmission, 23 is the fluidized bed, 24 is the direction in which the sediment (or float) flows, Each is shown. Among the so-called scraper type continuous devices, those of Power up & Eco Type are shown. In this type, if the power unit Motor / transmission device VVVF inverter control is attached to each of the divided sediment dischargers, it leads to cost increase, so one set of Motors is installed on both sides of the fluidized bed sorter, and each discharger The speed is adjusted by a mechanical transmission (continuously variable or Gear Change system). This type can also be collected by changing the collection speed in accordance with the specific gravity difference of the separation target.

  FIG. 6 shows a schematic view of one embodiment of the separation apparatus of the present invention. It is an apparatus related to a so-called continuous separation system. For example, it is possible to remove vinyl chloride from automobile shredder dust (mixed plastic) and recover low-chlorine plastic. As the powder, cinnabar (separation specific gravity 1.3) can be used.

  In FIG. 6, 1 is an object lighter than the apparent density (or separation specific gravity Dp) of the fluidized bed, 2 is a solid-gas fluidized bed, 3 is an object heavier than the apparent density (or separation specific gravity Dp) of the fluidized bed, 31 is a raw material stirrer, 32 is a float carrier, 33 is a float collector, 34 is a float ejector, 35 is a sediment conveyor, 36 is a sediment ejector, 37 is an air chamber, 38 is exhaust, 39 is a raw material supply, Each is shown.

  In order to simplify the description in FIG. 6, a series of flows will be first described for the case where sand is used as the powder of the solid-gas fluidized bed and plastic is used as the separation target. The separation object is supplied by the 39 raw material supply. In this embodiment, the separation object input means is input by a cylindrical means 39 such as a raw material supply chute. The separation object is optionally stirred and supplied by the raw material stirrer 31. Of the supplied separation object (for example, plastic), the floated material moves according to the arrow by the floated material transporter 32 such as a belt conveyor. The moved float is collected by a first collection means for collecting the float, for example, the float collection machine 33 and discharged to the float discharge machine 34. The floated material discharger can be discharged out of the apparatus by a conveying means such as a belt conveyor.

  On the other hand, of the supplied separation object, the sediment is moved by the sediment conveyor 35 such as a belt conveyor in the direction of the arrow, and the second collection means for collecting the sediment, for example, sediment discharge Collected and discharged through machine 36. The sediment discharger can also be discharged out of the apparatus by a conveying means such as a belt conveyor. In this example, the mechanism for changing the collection speed of the separation object in accordance with the specific gravity difference of the separation object can change the collection speed of the sediment and / or the floating object by changing the rotation speed of the belt conveyor. Can be changed.

  A solid-gas fluidized bed can be formed by blowing air from the air chamber 37 in the figure. The air chamber 37 is composed of a plurality of chambers and forms a stable fluidized bed.

  Moreover, although it is with exhaust_gas | exhaustion 38 here, this may be a dust collector, for example. This is because the fine powder in the fluidized medium jumps out of the fluidized bed and generates dust during fluidization, so that the fine powder produced is collected.

  In the embodiment of FIG. 6, the so-called bidirectional type recovery means described above is used, but by incorporating the above-described embodiments of FIGS. 2, 4, and 5, the specific gravity difference of the separation object Accordingly, the apparatus may be a device that employs a mechanism for collecting the separation object by changing the collection speed of the separation object. In the figure, for example, the flow of the belt conveyor may be made such that the flow direction of the sediment is orthogonal to the flow direction of the floated material. One or more multiple collection means may be provided.

  FIG. 7 shows a schematic diagram in one embodiment of the present invention for recovering the components of the separation object. It is a so-called batch type. For example, it is suitable for separating household appliance shredder dust (mixed plastic). Vinyl chloride can be separated and removed with high accuracy. As the powder, glass beads, polystyrene beads, or a mixture thereof can be used. In this case, the separation specific gravity is 0.6 to 1.1.

  This is because the components constituting the solid-gas fluidized bed are introduced by introducing the components constituting the solid-gas fluidized bed, then the separation object, and then the components constituting the solid-gas fluidized bed. This is an example of a specific apparatus that realizes dry separation, which is characterized by putting the separation object in between.

  In FIG. 7, 41 is a medium hopper (1), 42 is a raw material hopper, 43 is a medium hopper (2), 44 is a cutting device, 45 is a fluid tank, 46 is a dust collector, 47 is a rotary distribution valve, and 48 is a flow rate. 49, blower, 50, float collection machine, 51, sediment collection machine, 52, lower layer medium input, 53, raw material input, 54, upper layer medium input, 55, fluidized separation, 56, floated material suction, 57 Indicates sediment aspiration, respectively.

  In the example of the apparatus of FIG. 7, a series of flows will be described. In this example, a raw material hopper 42 is illustrated as the separation object input unit. First, a lower layer powder medium is charged by a medium hopper (1) 41 which is an example of a powder charging means. You may throw in via the cutting device 44. Next, the separation object is introduced by the raw material hopper 42. Next, the upper layer powder (medium) is charged by the medium hopper 43. Through the rotary distributor valve 47 from the blower 49 through the flow meter 48, the optimum air is blown according to the separation object, and the fluidized bed 45 is formed. At this time, since the fine powder in the fluidized medium jumps out of the fluidized bed during the fluidization by the dust collector 46, dust may be collected. Next, the blowing is stopped by the rotation of the 47 distributing valve, and the fluidized bed is stopped and fluidized to stop and become a fixed bed. Here, the levitated matter is collected by the levitated matter collecting apparatus 50 having the suction mechanism 56. Similarly, the sediment is collected by the sediment collection device 51 having the suction mechanism 57. Depending on the specific gravity difference of the separation object, it can be collected by changing the collection speed of the float collection device or sediment collection device.

  FIG. 8 shows a schematic diagram in one embodiment of the present invention for recovering the components of the separation object. This is an example of a so-called batch separation system. For example, it is suitable for separation of automobile shredder dust (mixed metal). It is possible to sort out aluminum mixed in non-ferrous metals and copper / brass. As the powder, for example, steel shot (separation specific gravity Dp is 4.0) can be used. In FIG. 8, 39 is a raw material supply, 61 is a sorting basket, 62 is a fluidized bed, 63 is a separation shutter, 64 is a switching damper, 65 is a sediment, 66 is a float, and 67 is a descent.

  In the example of the apparatus of FIG. 8, a series of flows will be described. First, a raw material which is a separation target is charged (raw material supply 39). Next, after the separation object is supplied, the sorting basket 61 is lowered. Fluidization is performed, and the separation object is separated in the fluidized bed 62. Thereafter, as a separating means, for example, the separation shutter 63 is closed to separate the sediment and the floated material, and then the sorting basket 61 is moved to the discharge position to discharge the sediment. The sediment 3 can be recovered by a recovery means for recovering the sediment. Further, the floating material is collected in the region other than the sediment by the switching damper 64. In this case, the floating shutter can be discharged by opening the separation shutter. The discharged float 1 can be recovered by a recovery means for recovering the float. The selection basket moves to the raw material supply position and one cycle is completed. In this case, the selection basket has a sieve shape, and the powder falls from the sieve, and only the separation object remains in the selection basket. It is also possible to selectively collect items and the like.

  FIG. 9 shows a schematic diagram in one embodiment of the present invention for recovering the components of the separation object. This is an example of a so-called continuous separation system. For example, it can be aimed at the separation of ores, in particular iron ores. As the powder, zircon sand, iron powder, a mixture thereof, and the like can be used. In this case, the separation specific gravity Dp is 2.6 to 4.0.

  In FIG. 9, 1 is an object that is lighter than the apparent density (or separation specific gravity Dp) of the fluidized bed, 2 is a solid-gas fluidized bed, 3 is an object that is heavier than the apparent density (or separation specific gravity Dp) of the fluidized bed, and 71 is the floating material transport , 72 is a float collection machine, 73 is a float discharge machine, 74 is a sediment transport machine, 75 is a sediment discharge machine, and 76 is an air chamber.

  About this aspect, although there are some differences such as the method described in FIG. 6 and the raw material supply method, the stirrer and the dust collector are not illustrated, the flow is generally the same as the aspect of FIG. Reference can be made to the explanation of FIG. The raw material supply 39 is supplied on the float carrier, and can stir the separation object using the conveyor of the carrier. Although the air chamber 37 is marked at one place in the drawing, it may be blown from a part or the whole of the lower part of the apparatus as described above.

  FIG. 10 shows a schematic diagram in one embodiment of the present invention for recovering the components of the separation object. This is an example of a so-called continuous separation system. For example, the separation of ore and mixed plastic can be aimed. As the powder, cinnabar sand, zircon sand, and a mixture thereof can be used. In this case, the separation specific gravity Dp can be set to 1.3 to 2.0.

  In FIG. 10, 1 is an object that is lighter than the apparent density (or separation specific gravity Dp) of the fluidized bed, 2 is a solid-gas fluidized bed, 3 is an object that is heavier than the apparent density (or separation specific gravity Dp) of the fluidized bed, 39 is a raw material supply, Reference numeral 81 is a raw material agitator, 82 is a floated material transporter, 83 is a floated material recovery machine, 84 is a floated material ejector, 85 is a sediment transporter, 86 is a sediment ejector, and 87 is an air chamber.

  This mode is slightly different from the mode described in FIG. 6, such as how to supply the raw material and the dust collector is not shown, but the flow is almost the same as the mode in FIG. You can refer to the description. The raw material supply 39 can be supplied while being stirred on the stirrer 81. Although the air chamber 87 is marked at one place in the drawing, it may be blown from a part or all of the lower part of the apparatus as described above, as well as an air chamber composed of a plurality of places (pieces).

  FIG. 11 shows a schematic diagram of one embodiment of the present invention for recovering the components of the separation object. For example, it can be used for separation of automobile shredder dust (mixed metal), particularly for sorting aluminum mixed in non-ferrous metal, copper, brass, and the like. This is a so-called batch separation system. For example, iron powder (separation specific gravity 4.0) can be used as the powder. In FIG. 11, 39 is a raw material supply, 1 is an object lighter than the apparent density (or separation specific gravity Dp) of the fluidized bed, 3 is an object heavier than the apparent density (or separation specific gravity Dp) of the fluidized bed, 91 is a sediment receiving box, 92 indicates a sorting basket, 93 indicates a fluidized bed, and 94 indicates an increase in the sorting basket.

  In the example of the apparatus in FIG. 11, a series of flows will be described. First, a raw material which is a separation target is charged (raw material supply 39). A sorting basket 92 is installed in the fluidized bed supplied with the separation object. Fluidization is performed to separate the objects to be separated. The floated material is collected by a collecting means (not shown). It may be collected manually. After collecting the float, the sorting basket rises. Thereafter, the sediment receiving box 91 moves below the sorting basket, the bottom of the sorting basket opens, the sediment falls, and the sediment is collected in the sediment receiving box. The selection basket moves to its original position and completes one cycle. In this case, the selection basket has a sieve shape, and the powder falls from the sieve, and only the separation object remains in the selection basket. It is also possible to selectively collect items and the like.

  FIG. 12 shows a schematic diagram in one embodiment of the present invention for recovering the components of the separation object. This is an example of a so-called continuous separation system. For example, it can be intended to separate automobile and home appliance shredder dust (mixed plastic). For example, vinyl chloride can be removed and low chlorine plastics can be recovered. As the powder, cinnabar sand or the like can be used. In this case, the separation specific gravity Dp can be set to 1.2 to 1.3.

  In FIG. 12, 1 is an object lighter than the apparent density (or separation specific gravity Dp) of the fluidized bed, 2 is a solid-gas fluidized bed, 3 is an object heavier than the apparent density (or separation specific gravity Dp) of the fluidized bed, 39 is a raw material supply, 101 is a raw material stirrer, 102 is a floated material transporter, 103 is a floated material recovery machine, 104 is a floated material ejector, 105 is a sediment transporter, 106 is a sediment ejector, and 107 is an air chamber.

  This mode is slightly different from the mode described in FIG. 6, such as how to supply the raw material and the dust collector is not shown, but the flow is almost the same as the mode in FIG. You can refer to the description. The raw material supply 39 can be supplied while being stirred on the stirrer 81. Although the air chamber 107 is marked at one place in the figure, it may be blown from a part or all of the lower part of the apparatus as described above, as well.

  Further, the dry separation apparatus of the present invention is a solid-gas fluidized bed formed by powder, a separation object charging means for charging a separation object, and the separation object is separated and floated by the solid-gas fluidized bed. A first recovery means for recovering levitated matter; a second recovery means for recovering the sediment that is separated by the solid-gas fluidized bed; and a specific gravity measuring means for measuring the specific gravity of the powder. And separating means for separating at least two kinds of powders in the solid-gas fluidized bed.

  This dry separation apparatus has the advantage that the separation specific gravity can be adjusted during operation. As a result, similar to the wet separation apparatus, the separation specific gravity can be prepared easily and reliably in the dry separation apparatus.

  The description of the dry separation apparatus of the present invention described above can be applied as it is to the solid-gas fluidized bed, the separation object input means, the first recovery means, and the second recovery means.

  Here, another dry separation apparatus of the present invention will be described with reference to the drawings. FIG. 14 illustrates an example using magnetism and non-magnetism as the difference in properties of the powder, but a difference in particle size or the like may be used. Specific gravity measuring means for measuring the specific gravity of the powder can be measured using, for example, a specific gravity meter 111 or the like. As long as the specific gravity can be measured, the specific gravity measuring means is not particularly limited.

  As a separating means for separating at least two kinds of powders in the solid-gas fluidized bed 2, a sieving, a magnetic separator or the like can be used. In FIG. 14, a magnetic separator 113 is used to separate magnetic powder and non-magnetic powder.

  Further, in a preferred embodiment of the dry separation apparatus of the present invention, the setting means for setting the separation specific gravity of the solid-gas fluidized bed, and the powder mixing ratio based on the separation specific gravity set by the setting means. It has a mixing ratio calculating means for calculating, and a powder supplying means for supplying the powder into the solid-gas fluidized bed based on the mixing ratio calculated by the mixing ratio calculating means.

  The setting means for setting the separation specific gravity of the solid-gas fluidized bed is to set a desired separation specific gravity when it is desired to adjust the separation specific gravity during operation. Usually, it can be automatically controlled by a personal computer or the like, but the setting means is not particularly limited as long as a desired separation specific gravity can be set. Once the separation specific gravity of the fluidized bed 2 is set, the mixing ratio of the powder is calculated based on the set separation specific gravity. The calculation of the mixing ratio can be performed by the mixing ratio calculation means.

  Based on the mixing ratio calculated by the mixing ratio calculating means, the powder is supplied into the solid-gas fluidized bed. The powder in the fluidized bed 2 can be supplied by a powder supply means. The powder supply means is not particularly limited as long as powder can be supplied. For example, in FIG. 14, a medium hopper 118 and a feeder 119 are used. The fine adjustment of the supply amount can be performed by a feeder, which can supply a desired amount based on the mixing ratio calculated by the mixing ratio calculation means.

  In the example of FIG. 14, the magnetic property is used. However, when the particle size is used, a magnetic separator or the like is not necessarily required. At least two kinds of powders in the layer 2 may be separated.

  EXAMPLES Hereinafter, the present invention will be described more specifically with reference to examples. However, the present invention is not intended to be interpreted as being limited to the following examples.

Example 1
Principle of sorting Coal selection technology is an assembly of many unit operations such as sieving, crushing, specific gravity sorting, dehydration, concentration and purification. Among these techniques, specific gravity sorting is a key technique. Except for flotation and oil granulation, coal sorting technology is basically a technology that relies on specific gravity separation.

  Usually, the mined raw coal has a continuous specific gravity distribution and particle size distribution. In order to evaluate the specific gravity selection and the expected value of the result, it is necessary to examine the specific gravity distribution and the particle size distribution.

  For this reason, we first conducted an ups and downs analysis. Then, preliminary investigations were made for the analysis of the rise and fall for process calculation.

In Table 1, the vertical axis indicates the specific gravity (SP.GR .: Specific Gravity) range. This specific gravity value is the specific gravity of the specific gravity liquid used for the flotation analysis. W% on the horizontal axis is the weight percent of coal in each specific gravity range, A% is the average ash value (Ash) of coal in that range, expressed in weight percent, and T / S% is the weight percent in that range. The average total sulfur content (inorganic sulfur content + organic sulfur content) and ΣW% of the coal in the range when accumulated from the lower specific gravity (or higher) to the higher (or lower) Weight%, FA is the average ash value when accumulating from the lower specific gravity to the higher one, SA is the average ash content when accumulating from the higher specific gravity to the lower one, and FS is higher from the lower specific gravity SS is the average total sulfur content when accumulated from the higher specific gravity to the lower one.

  Next, the degree of specific gravity sorting difficulty was evaluated. For example, the evaluation index was NGM: Near Gravity Material (wt%). NGM is indicated by the amount of solids: Wt% included in the specific gravity range of Do (Partition Density) ± 0.1.

  Author: According to Michell's “Coal preparation: COAL PREPARATION” A high degree of difficulty means that the amount contained in Do ± 0.1 is large, and therefore, in the specific gravity separation, there is a large amount contained in a range in which there is a high possibility of straying between floated material and sediment. Naturally, if there are many strays, there is a high possibility that the quality of the levitated or subsidence will not reach the target quality. Therefore, the increase in the difficulty level leads to severe restrictions on the separation conditions. Table 2 qualitatively expresses the severity of the separation conditions with increasing difficulty.

  Next, the influence of the difficulty level on the selection result was examined. There is a close relationship between the degree of difficulty and the yield efficiency. An example of the relationship in the jig is shown below. Table 2 qualitatively expresses the severity of separation conditions with increasing difficulty, while Table 3 quantitatively expresses the severity when the sorter is an air moving jig. . That is, when there is a large amount in a range where there is a high possibility of getting lost in the mutual product, the separation specific gravity must be changed in order to maintain the target quality. The change in separation specific gravity is directly linked to the change in yield. Table 3 shows the relationship between the actual yield and the theoretical yield, that is, the yield when the misdelivery is separated by the sorter with zero.

Remarks: Organic Efficiency = (Actual Yield) / (Theoretical Yield) x 100 (%)

  Next, the performance of the specific gravity sorter was examined.

(1) Partial recovery rate The partial recovery rate is an allocation rate that indicates how much solid matter (separation target) contained in each specific gravity category is discharged to the sediment (sediment) side. That is, it can be calculated by (sediment) / (sediment + floating matter) × 100 (%) in each specific gravity category. Details are shown in FIG. An enlarged view of the table in FIG.

(2) Display of sorting performance Next, a distribution rate curve was created. An allocation curve can be obtained by plotting partial recovery against specific gravity. The more the slope of the distribution ratio curve is a sphere, the smaller the amount of misdistributed items distributed to the subsidence. That is, it can be said that the slope of the distribution rate curve indicates the sorting performance. This slope is calculated and expressed as: Table 5 shows the distribution rate curve.

Here, in this case, Ep = (D75−D25) / 2. Ep is a probable error, and the Ep value increases as the separation specific gravity increases (accuracy decreases), and decreases as the particle size increases (accuracy increases). Ep
Ep = f (Dp) / f (d)
In this case, Dp: separation specific gravity and d: average particle diameter. For example, D50 can be defined as the actual separation density. In Table 4, D50 is 1.616, D75 = 1.675, and D25 = 1.530. Therefore, a value of Ep = (1.675−1.530) /2=0.073 can be obtained.

(3) Sorting results Each sorter has its own sorting accuracy. These sorting accuracy is expressed by Tera index Ep or incomplete separation degree I. Therefore, the sorting result can be calculated and predicted using these sorting accuracy.

  Based on such results, the prototype dry separation apparatus shown in FIGS. 1 to 12 was actually manufactured, and automobile shredder dust, home appliance shredder dust, and other industrial waste, general waste, ore coal, rare earth In addition to various mineral resources and industrial products, we tried to separate shredder dust, waste, minerals, crops, plastics, metals, etc., so that they can be understood based on the principle of specific gravity separation and the separation accuracy can be calculated. There was found. That is, it was proved that the dry separation method according to the present invention was separated on the same principle as the conventional wet separation method.

Example 2
Next, trial production of a dry separation apparatus capable of adjusting the separation specific gravity even during operation was attempted.

  Separation method is possible by paying attention to the difference in particle size, but since it becomes classification and sieving of 100 μm or less, in consideration of cost and equipment, in this example, as a powder, a powder having magnetism and Separation was attempted when it was desired to use non-magnetic powder.

  The separation method focusing on the difference in magnetism is easier to systemize by applying a magnetic separator because a high-performance magnetic separator is available as a general-purpose product and fine particles of about 10 μm can be collected. Therefore, in this embodiment, the magnetic separator 113 is used. The magnetic separator 13 is for selecting a magnetic material and a non-magnetic material. Further, since the circulation line of the magnetic medium can be maintained by combining with the demagnetizer 115, the demagnetizer 115 was also used.

  Regarding the required medium volume, it is considered that each medium (powder) needs to have a volume at least equal to the volume of the fluidized bed 2 + the holding volume of the circulation line. Each medium can be stored in its own dedicated hopper 118.

  When the separation specific gravity of the fluidized bed 2 is set by the setting means for setting the separation specific gravity of the solid-gas fluidized bed 2 (also simply referred to as a fluidized bed), the mixing ratio is calculated based on the separation specific gravity set by the setting means. The mixing ratio of the medium (powder) can be calculated by means. The fluidized bed 2 can be filled out in a fixed amount from each medium-dedicated hopper 118 based on the calculated mixing ratio.

  When the fluidized bed specific gravity has to be changed, this apparatus can calculate the medium mixing ratio after the change. Further, both media are cut according to the calculated ratio and supplied to the fluidized bed.

  On the other hand, an existing mixed medium in an amount substantially equal to the new mixed medium can be extracted from the fluidized bed 2 and supplied to the magnetic separator 113.

  The magnetic separator 113 separates the magnetic medium and the non-magnetic medium. The collected magnetic medium 114 is returned to the dedicated hopper 118b via the demagnetizer 115. The nonmagnetic medium 116 is also returned to the dedicated hopper 118a.

  The returned medium is cut out according to the changed mixing ratio and supplied to the fluidized bed 2.

  This circulation of the medium continues until the fluidized bed specific gravity reaches the changed specific gravity. The time can be designed in about 15-20 minutes, and during this time, the feed to the fluidized bed stops.

  The specific gravity of the fluidized bed 2 is measured at several places at any time with a hydrometer 111 (one place in FIG. 14, but a plurality of hydrometers may be provided) to confirm the change.

  The medium pulled out from the fluidized bed 2 is passed through a vibrating screen (separation means for separating powder and other materials) 112 having a sieve particle size of 0.5 mm before being sent to the magnetic separator 113. By collecting the contaminants 117 of +0.5 mm using the vibrating screen 112, the medium can be cleaned together.

  As described above, when silica sand and iron powder are used as the medium, the specific gravity of the fluidized bed can be automatically adjusted from 1.3 to 4.4, and it has been found that the separation specific gravity can be adjusted during operation.

  In this example, a dry separation apparatus capable of simply adjusting the separation specific gravity during operation is used, but the recovery rate of the separation target is changed according to the specific gravity difference described in FIGS. It is also applicable to the dry separation method.

  In addition, a solid-gas fluidized bed formed of powder, a separation object input means for inputting a separation object, and a first object for recovering a floated object that is separated and floated by the solid-gas fluidized bed. A recovery means; and a second recovery means for recovering the sediment that has been separated and settled by the solid-gas fluidized bed, wherein the first and / or second recovery means are arranged for the separation object. The present invention can also be applied to a dry separation apparatus having a mechanism for changing the collection speed of a separation object according to the specific gravity difference.

1 Body lighter than fluid bed apparent density 2 Solid-gas fluidized bed 3 Body heavier than fluid bed apparent density 4 Separation tank 5 Gas dispersion plate 6 Discharge machine A
7 Ejector C
8 Ejector E
9 Ejector B
10 Ejector D
11 Direction of flow of float (or sediment) 12 Direction of flow of sediment (or float) A 13 Direction of flow of sediment (or float) B 14 Direction of sediment (or float) C 15 Flow of sediment (Or levitated matter) direction 16 in which sediment E (or levitated matter) D flows in direction 17 direction in which levitated matter (or sediment) flows 18 direction in which sediment (or levitated matter) flows 19 levitated matter (or sediment) ) Flow direction 20 Sediment (or levitated material) flow direction 21 Power unit (motor)
22 Transmission 23 Fluidized bed 24 Flow direction of sediment (or levitated material) 31 Raw material stirrer 32 Float material conveyor 33 Float material collector 34 Float material ejector 35 Sediment material transporter 36 Sediment material ejector 37 Air chamber 38 Exhaust 39 Raw material supply 41 Medium hopper (1)
42 Raw material hopper 43 Medium hopper (2)
44 Cutting device 45 Fluid tank 46 Dust collector 47 Rotary distribution valve 48 Flow meter 49 Blower 50 Floating matter recovery 51 Sediment recovery 52 Lower layer medium input 53 Raw material input 54 Upper layer medium input 55 Fluidization separation 56 Float material suction 57 Sediment suction 61 Sorting basket 62 Fluidized bed 63 Separation shutter 64 Switching damper 65 Sediment 66 Sediment 67 Floating material 67 Descent 71 Floating material transporter 72 Floating material recovery machine 73 Floating material ejector 74 Sediment transporter 75 Sediment ejector 76 Air chamber 81 Raw material Agitator 82 Flotation material transport device 83 Float material recovery device 84 Float material discharge device 85 Sediment transport device 86 Sediment discharge device 87 Air chamber 91 Sediment receiving box 92 Sorting basket 93 Fluidized bed 94 Sorting basket rise 101 Raw material stirrer 102 Float Conveyor 103 Float collected machine 104 Float ejector 105 Sediment conveyor 106 Sediment ejector 107 Air chamber 110 Fluidized bed type specific gravity separator 111 Hydrometer 112 Vibrating screen 113 Magnetic separator 114 Magnetic material 115 Demagnetizer 116 Nonmagnetic material 117 Contaminant 118a Medium hopper (for nonmagnetic material)
118b Medium hopper (for magnetic materials)
119 Feeder (variable speed)

Claims (28)

The separation object is introduced into the solid-gas fluidized bed in which the powder is fluidized, the gas dispersed in the solid-gas fluidized bed is introduced, and the separation object is separated using the apparent density of the solid-gas fluidized bed. A dry separation method,
A dry separation method characterized by changing the recovery rate of the separation object according to the specific gravity difference of the separation object.   When the separation specific gravity of the solid-gas fluidized bed is Dp, the separation object having a specific gravity outside the range of Dp ± 0.2 is more than the separation object having a specific gravity within the range of Dp ± 0.2. The process of claim 1 wherein the recovery is at a fast rate.   When the separation specific gravity of the fluidized bed is Dp, the separation object having a specific gravity outside the range of Dp ± 0.1 is faster than the separation object having a specific gravity within the range of Dp ± 0.1. The method according to claim 1, wherein the process is recovered by   The dry separation method according to any one of claims 1 to 3, wherein the gas is introduced through a gas dispersion plate made of a porous material.   The method according to claim 4, wherein the porous material is a punching plate.   The method according to claim 1, wherein the powder is fluidized by blowing air from a lower part of the solid-gas fluidized bed. The method according to any one of claims 1 to 6, wherein the air is blown under a condition of air permeability of 5.0 (cm ³ / s) / cm ² or less. If the superficial velocity as u ₀ the minimum fluidization superficial velocity of the powder was u _mf, claims 1-7 wherein the u ₀ / u _mf is characterized by performing the air blowing in the range of 1-4 The method according to any one of the above.   9. The apparent density of the solid-gas fluidized bed is set between the maximum density and the minimum density of each component in the separation target to be separated. the method of.   The powder is at least one selected from the group consisting of unibeads, glass beads, zircon sand, polystyrene particles, steel, silica sand, alumina sand, and powders having a density comparable to these. The method according to any one of the paragraphs.   The method according to any one of claims 1 to 10, wherein the separation target is automobile shredder dust, home appliance shredder dust, and other industrial waste, general waste, ore, coal, or rare earth.   The method according to any one of claims 1 to 11, wherein the ores are iron ore, nickel ore, copper ore, limestone, or rare metal-containing ore.   The method according to claim 1, wherein the powder has an average particle size of 30 to 500 μm.   The components constituting the solid-gas fluidized bed are introduced, then the separation object is introduced, and then the components constituting the solid-gas fluidized bed are introduced, thereby entering between the components constituting the solid-gas fluidized bed. The method according to claim 1, wherein the separation object is introduced.   The method according to claim 1, wherein the powder is at least two kinds of mixed media.   The method according to claim 15, wherein the powders have different particle sizes.   The method according to claim 15, wherein the powder includes magnetic powder and non-magnetic powder.   A solid-gas fluidized bed formed of powder, a separation target input unit for inputting a separation target, and a first recovery unit for recovering a floating substance separated and floated by the solid-gas fluidized bed. And a second recovery means for recovering the sediment separated and settled by the solid-gas fluidized bed, wherein the first and / or second recovery means has a difference in specific gravity of the separation object. A dry separation apparatus having a mechanism for changing the recovery rate of the separation object according to the above.   When the first and / or second recovery means sets the separation specific gravity of the solid-gas fluidized bed to Dp, the separation object having a specific gravity outside the range of Dp ± 0.2 is set to Dp ± 0. The apparatus according to claim 18, wherein the recovery is performed at a faster rate than the separation object having a specific gravity within a range of two.   When the first and / or second recovery means has a separation specific gravity of the fluidized bed as Dp, the separation object having a specific gravity outside the range of Dp ± 0.1 is set to Dp ± 0.1. 19. The apparatus of claim 18, wherein the apparatus collects at a faster rate than the separation object having a specific gravity within a range.   21. The apparatus according to any one of claims 18 to 20, wherein the recovery directions for recovering the separation target of the first and / or second recovery means are different from each other.   Furthermore, the apparatus of any one of Claims 18-21 which has a dust collection collection | recovery means which collect | recovers the dust collection generate | occur | produced when isolate | separating and collect | recovering a separation target object.   23. The apparatus according to any one of claims 18 to 22, wherein the first and / or second recovery means recovers the powder together with the floated material and / or sediment.   Furthermore, the apparatus of any one of Claims 18-23 which has a isolation | separation means for isolate | separating the said floating material and the said sediment in the said solid-gas fluidized bed.   The said 1st and / or 2nd collection | recovery means collect | recovers the said levitation | floating matter and / or sediment by the collection | recovery container provided in the said solid-gas fluidized bed. Equipment.   The apparatus according to any one of claims 18 to 25, wherein the first and second recovery means are based on a suction mechanism.   27. The specific gravity measuring means according to any one of claims 18 to 26, further comprising a specific gravity measuring means for measuring the specific gravity of the powder and a separating means for separating at least two kinds of powders in the solid-gas fluidized bed. apparatus.   Further, a setting means for setting the separation specific gravity of the solid-gas fluidized bed, a mixing ratio calculation means for calculating the mixing ratio of the powder based on the separation specific gravity set by the setting means, and the mixing ratio calculation means 28. The apparatus according to any one of claims 18 to 27, further comprising powder supply means for supplying the powder into the solid-gas fluidized bed based on the calculated mixing ratio.