KR102075589B1 - System for aluminium black dross recycling - Google Patents

Abstract

The present invention relates to an aluminum black dross recycling system, wherein an aluminum black dross recycling system for recycling black dross generated when dissolving aluminum scrap in a fluxed aluminum molten metal is used. A dividing unit for dividing into dross particulate powder; And a reactor for reacting the dross fine particle powder with water to divide into a soluble solid solution, an insoluble solid component and a hydrolysis gas, and the water contained in the hydrolysis gas by passing the hydrolysis gas discharged from the reactor through water. And a water decomposition unit including a trap for collecting impurities and a condenser for cooling the hydrolysis gas discharged from the trap and condensing water vapor contained in the hydrolysis gas.

Description

Aluminum black dross recycling system {System for aluminum black dross recycling}

The present invention relates to an aluminum black dross recycling system for carrying out a recycling process of aluminum black dross.

Many aluminum parts used in automobiles, home appliances, and building materials are manufactured using aluminum casting equipment. It is aluminum melting furnace to supply molten aluminum to such an aluminum casting apparatus. Aluminum melting furnace is a device that melts aluminum scrap formed into a certain size at high temperature.

Since aluminum is a highly oxidizing metal, aluminum oxide is generated in the process of dissolving aluminum in the molten aluminum. If the generation amount of such aluminum oxide increases, the recovery rate of aluminum falls. In addition, in general, the aluminum lump to be added to the molten aluminum is interposed with paint and other inclusions. As these inclusions increase, the purity of aluminum decreases.

In order to solve the problems caused by the aluminum oxide and inclusions, a flux capable of preventing oxidation of aluminum and capturing the inclusions is introduced into the molten aluminum. In this way, the dross generated when dissolving the aluminum scrap in the fluxed aluminum molten metal is called black dross.

However, in the related art, a method for effectively recycling the black dross has not been proposed in order to recycle materials included in the black dross such as aluminum, aluminum oxide, and flux according to a purpose. Therefore, the black dross is disposed of and disposed of in the soil, which causes a problem of environmental pollution and resource waste.

SUMMARY OF THE INVENTION The present invention has been made in view of the above problems, and an object thereof is to provide an aluminum black dross recycling system having an improved structure to facilitate recycling of the compositions included in the black dross.

Aluminum black dross recycling system according to a preferred embodiment of the present invention for solving the above problems, in the aluminum black dross recycling system for recycling the black dross generated when dissolving aluminum scrap in the flux-treated aluminum molten metal A dividing unit for dividing the black dross into aluminum grains and dross particulate powder; And a reactor for reacting the dross fine particle powder with water to divide into a soluble solid solution, an insoluble solid component and a hydrolysis gas, and the water contained in the hydrolysis gas by passing the hydrolysis gas discharged from the reactor through water. And a water decomposition unit including a trap for collecting impurities and a condenser for cooling the hydrolysis gas discharged from the trap and condensing water vapor contained in the hydrolysis gas.

Preferably, the aluminum scrap comprises at least aluminum scrap can scrap, and the flux is 93-97 parts by weight of a mixture of sodium chloride (NaCl) and potassium chloride (KCl) in the same parts by weight and cryolite, Potassium Cryolite) 3-7 parts by weight.

Preferably, the dividing unit is divided into the aluminum grains and the dross fine particle powder by crushing and pulverizing the black dross.

Preferably, the water decomposition unit further includes a first connection line connecting the reactor and the trap so that the hydrolysis gas released from the water contained in the reactor passes through the water contained in the trap.

Preferably, the first connection line has an extension part provided to be immersed in the water contained in the trapper by a predetermined depth and a discharge part for discharging the hydrolysis gas passing through the extension part to the water stored in the trap device. .

Preferably, the discharge portion has at least one injection hole perforated to inject the hydrolysis gas passing through the extension portion into the water contained in the trap.

Preferably, the trap includes a plurality of separator plates each having at least one guide hole perforated to guide the hydrolysis gas released from the water contained in the trap to the condenser.

Preferably, the separating plates are arranged such that the guide holes provided in the respective separating plates are staggered from each other.

Preferably, the water decomposition unit further includes a second connecting line connecting the trap and the condenser such that the hydrolysis gas released from the water contained in the trap is delivered to the condenser.

Preferably, the water decomposition unit, the condensed water formed by condensation of the water and the water vapor contained in the trap is introduced, and the negative pressure generated by the cooling of the hydrolysis gas is delivered, so that the trap and the condenser It is further provided with a gas pressure compensation line connected to each.

Preferably, the gas pressure compensation line has a mixed water chamber configured to receive at least a portion of the mixed water mixed with the water and the condensed water.

Preferably, the mixed water chamber has an observation window formed to be able to observe the level change of the mixed water.

Preferably, the gas pressure compensation line, the first on-off valve provided between the trap and the mixed water chamber to selectively communicate the trap and the mixed water chamber, and selectively communicates the condenser and the mixed water chamber And a second open / close valve installed between the condenser and the mixed water chamber to enable it.

Preferably, the gas pressure compensation line has a drain valve provided to selectively discharge the mixed water mixed with the water and the condensed water to the outside.

Preferably, the gas pressure compensation line has a first inlet connected to the trap so that the water is introduced by water pressure, and a second inlet connected to the condenser so that the condensate is introduced by gravity.

Preferably, further comprises a combustion unit for burning the hydrolysis gas discharged from the condenser.

Preferably, further comprising a gas storage unit for storing the hydrolysis gas discharged from the condenser, wherein the combustion unit burns the hydrolysis gas discharged from the gas storage unit.

Preferably, the combustion unit is provided to preheat the aluminum scrap using the heat of combustion of the hydrolysis gas.

The present invention relates to an aluminum black dross recycling system, and has the following effects.

First, the present invention is to recycle the composition contained in the aluminum black dross to aluminum granules, soluble solids, insoluble solids and hydrolysis gas according to the nature, so that the composition contained in the black dross is discarded without recycling. The composition can be minimized to improve economics.

Second, the present invention can increase the purity of the hydrolysis gas through filtering the impurities contained in the hydrolysis gas, it is possible to further improve the economics.

1 is a block diagram schematically showing an aluminum black dross recycling system according to a preferred embodiment of the present invention.
FIG. 2 is a schematic diagram schematically showing the aluminum melting furnace of FIG. 1. FIG.
3 is a cross-sectional view of the melting chamber and the flow force applying chamber of FIG. 2.
FIG. 4 is a schematic diagram showing a state in which a spherical black dross is formed in the dissolution chamber of FIG. 2. FIG.
5 is a photograph of a spherical black dross formed in the dissolution chamber of FIG. 2.
6 is a plan view of a melting chamber showing a state in which a spherical black dross is suspended on the surface of the molten aluminum contained in the melting chamber of FIG. 2.
7 is a schematic diagram schematically showing the black dross recycling apparatus of FIG.
8 is a photograph of atomized dross powder.
FIG. 9 is a schematic view schematically showing the water decomposition unit shown in FIG. 7; FIG.
10 is a view showing a schematic structure of the trap shown in FIG.
FIG. 11 is a plan view of the separators shown in FIG. 10. FIG.
12 is a photograph of soluble solids precipitated and dried.
FIG. 13 is a SEM-EDS chart qualitatively analyzing the soluble solids shown in FIG. 12.
FIG. 14 is a table showing a composition ratio of soluble solids shown in FIG. 12. FIG.
15 is a photograph of insoluble solids dried.
Fig. 16 is a photograph of insoluble solids subjected to calcination
FIG. 17 is a SEM-EDS chart for qualitatively analyzing the insoluble solids subjected to the calcination shown in FIG. 16. FIG.
FIG. 18 is a chart showing the composition ratio of insoluble solids subjected to baking shown in FIG. 16. FIG.
19 is a flow chart schematically showing the aluminum black dross recycling method according to another preferred embodiment of the present invention.
20 is a flowchart for explaining details of the aluminum dissolving step and the step of crushing and crushing the spherical black dross described in FIG. 19.
21 is a flow chart for explaining the details of the dross powder water decomposition step and the water decomposition product recycling step described in FIG.

The terms or words used in this specification and claims are not to be construed as being limited to the common or dictionary meanings, and the inventors may appropriately define the concept of terms in order to best describe their invention. It should be interpreted as meanings and concepts corresponding to the technical idea of the present invention based on the principle that the present invention. Therefore, the embodiments described in the specification and the drawings shown in the drawings are only the most preferred embodiment of the present invention and do not represent all of the technical idea of the present invention, various modifications that can be replaced at the time of the present application It should be understood that there may be equivalents and variations.

In the drawings, the size of each component or a specific portion constituting the components is exaggerated, omitted, or schematically illustrated for convenience and clarity of description. Thus, the size of each component does not entirely reflect its actual size. If it is determined that the detailed description of the related known function or configuration may unnecessarily obscure the subject matter of the present invention, such description will be omitted.

1 is a block diagram schematically showing an aluminum black dross recycling system according to a preferred embodiment of the present invention.

1, an aluminum black dross recycling system 1 according to a preferred embodiment of the present invention comprises: an aluminum melting furnace 2 for dissolving aluminum scrap in a fluxed aluminum molten metal; And a black dross recycling apparatus 3 for recycling the black dross formed by trapping inclusions contained in the aluminum molten metal in the flux when the aluminum scrap is dissolved in the aluminum molten metal. The aluminum black dross recycling system 1 dissolves aluminum scrap in the fluxed aluminum molten metal to secure the aluminum molten metal for producing the aluminum casting, and recycles the components contained in the black dross. To handle the black dross.

Hereinafter, for convenience of description, the aluminum melting furnace 2 will be described first, and then the black dross recycling apparatus 3 will be described.

FIG. 2 is a schematic view schematically showing the aluminum melting furnace of FIG. 1.

Referring to FIG. 2, the aluminum melting furnace 2 includes a heating chamber 10 in which aluminum molten metal M is heated, and a melting chamber in which aluminum scraps A and flux F are introduced into aluminum molten metal M, respectively. 20 and a flow force imparting chamber 30 for imparting a flow force to the molten aluminum M.

The aluminum melting furnace 2 has a plurality of spaces partitioned by walls having a refractory material, as shown in FIG. 2. The heating chamber 10, the melting chamber 20, and the flow force imparting chamber 30 are each provided in a state independent of other spaces in any one of a plurality of spaces of the aluminum melting furnace 2.

The heating chamber 10 is a space for heating the molten aluminum M to a predetermined temperature.

The heating chamber 10 communicates with the 2nd flow path 29 of the melting chamber 20 mentioned later, and receives the aluminum molten metal M from the melting chamber 20. The heating chamber 10 is formed in a hermetically sealed structure that is separated from the outside except for a portion connected to the first flow passage 16 and the second flow passage 29 which will be described later to minimize heat loss.

As shown in FIG. 2, the heating chamber 10 includes a heating unit 12 for heating the aluminum molten metal M and a hot water outlet for discharging the aluminum molten metal M to the outside of the aluminum melting furnace 2. 14 and a first flow passage 16 for transferring the molten aluminum M accommodated in the heating chamber 10 to the flow force applying chamber 30.

The heating unit 12 is a device for heating the molten aluminum M to a predetermined temperature.

The heating unit 12 is. As shown in FIG. 2, the burner may be a burner installed at the walls partitioning the heating chamber 10. The heating temperature of the aluminum molten metal M is not specifically limited. The temperature of the aluminum molten metal M may be measured by a temperature sensor (not shown) installed in the heating chamber 10, and the heating unit 12 receives the temperature of the aluminum molten metal M from the temperature sensor, thereby causing aluminum. The molten metal M can be heated to a predetermined heating temperature.

The hot water outlet 14 is an outlet for discharging the molten aluminum M heated in the heating chamber 10 to the outside of the aluminum melting furnace 2.

 The tap opening 14 may be connected with an aluminum casting apparatus for producing an aluminum casting or with a molten metal transfer container for transferring an aluminum molten metal M. FIG. In the tap opening 14, an opening and closing valve 18 for selectively opening and closing the tap opening 14 may be provided.

The first flow passage 16 is a passage for transferring the molten aluminum M accommodated in the heating chamber 10 to the flow force applying chamber 30.

As shown in FIG. 2, the first flow passage 16 is formed by penetrating a wall partitioning the heating chamber 10 and the flow force applying chamber 30, and the aluminum molten metal M is formed in the first flow passage ( 16) flows into the flow force providing chamber (30).

3 is a cross-sectional view of the dissolution chamber and the flow force imparting chamber illustrated in FIG. 2, illustrating a spherical black dross formed in the dissolution chamber of FIG. 2 illustrated in FIG. 4, and the dissolution of FIG. 2 illustrated in FIG. 5. Picture of spherical black dross formed from yarn.

The melting chamber 20 is a space for injecting the flux F and the aluminum scrap A into the molten aluminum M. As shown in FIG.

The melting chamber 20 communicates with the 3rd flow path 34 of the flow force provision chamber 30 mentioned later, and receives the molten aluminum M from the flow force provision chamber 30. The melting chamber 20 is formed in an open structure in which at least a portion of the upper surface is opened to inject the flux F and the aluminum scrap A into the molten aluminum M, and is smaller than the heating chamber 10. Has a volume. That is, the melting chamber 20 is formed in an open structure so that the aluminum scrap A may be injected into the melting chamber 20 to perform the dissolving operation, and the heating chamber 10 may be relatively smaller than the heating chamber 10 to reduce the heat loss. It has a small volume.

As shown in FIGS. 2 and 3, the melting chamber 20 includes a vortex unit 21 for generating a swirl V descending in the molten aluminum M, and the flux F through the vortex V. The heating chamber 10 includes a flux supply unit 23 to be introduced into the raw material, a raw material supply unit 25 to inject aluminum scrap A into the vortex V, and an aluminum molten metal M contained in the melting chamber 20. And a second flow passage 29 for delivery therethrough.

The vortex unit 21 is a member for forming the vortex V which swings and descends on the molten aluminum M accommodated in the melting chamber 20.

The vortex unit 21 is installed in the melting chamber 20 so that at least a part thereof is immersed in the molten aluminum M. In the case where the flow of the vortex V generated by the vortex unit 21 and the flow of the aluminum molten metal M flowing into the melting chamber 20 through the third flow passage 34 directly face each other, the aluminum melt M ) Flow may be disturbed. In order to prevent this, as shown in FIG. 2, the vortex unit 21 is preferably installed on one side of the melting chamber 20 so as not to be in line with the third flow passage 34, but is limited thereto. It is not.

As shown in FIG. 3, the vortex unit 21 has a rotary shaft having a lower end immersed in the aluminum molten metal M and an upper end extending outward of the aluminum molten metal M and axially coupled to a driving motor (not shown). 21a) and a stirring impeller 21b axially coupled to the lower end of the rotation shaft 21a. When the driving motor is driven, as shown in FIG. 3, the stirring impeller 21b is rotated about the rotation shaft 21a to pivot around the rotation shaft 21a in the aluminum molten metal M accommodated in the melting chamber 20. A descending vortex V is produced.

The flux supply unit 23 is a device for injecting the flux F supplied from an external flux supply source (not shown) into the molten aluminum M accommodated in the melting chamber 20.

Flux F is a mixed salt having a specific gravity smaller than that of aluminum, and is formed of a material having a high affinity for inclusions. The flux supply unit 23 injects the flux F into the vortex V generated by the vortex unit 21 as shown in FIG. 3. Then, the flux (F) is rapidly immersed in the molten aluminum (M) by the vortex (V) to dissolve and can be evenly spread in the dissolution chamber (20). However, the present invention is not limited thereto, and the flux supply unit 23 may inject the flux F into a portion other than the vortex V.

The flux (F) injection timing is not particularly limited. For example, the flux supply unit 23 can inject the flux F into the vortex V before the raw material supply unit 25 injects the aluminum scrap A into the vortex V. As shown in FIG. Then, the flux F is immersed and melt | dissolved in the molten aluminum M while turning down by vortex V. However, since the flux F has a specific gravity smaller than that of aluminum, the flux F dissolved in the aluminum molten metal M rises to the surface of the aluminum molten metal M, and the molten flux layer is formed on the surface of the aluminum molten metal M. That is, a salt bath layer is formed. Such a molten flux layer can block the aluminum molten metal M and the aluminum script A injected into the molten aluminum M from contacting oxygen in the air, thereby reducing the amount of aluminum oxide generated.

Such flux F has a composition capable of selectively trapping inclusions and forming a molten flux layer. Preferably, the flux (F) may include 93-97 parts by weight of a mixture of sodium chloride (NaCl) and potassium chloride (KCl) in the same parts by weight and 3-7 parts by weight of cryolite (Cryolite, Potassium Cryolite). More preferably, the flux (F) may include 47.5 parts by weight of sodium chloride (NaCl), 47.5 parts by weight of potassium chloride (KCl) and 5 parts by weight of potassium aluminum fluoride (KAlF ₄ ).

On the other hand, when the input of aluminum scrap A is started by the raw material supply unit 25 which will be described later, the flux supply unit 23 vortex flux F simultaneously or at the same time as the raw material supply unit 25. You can put it in That is, the flux F is continuously or intermittently supplied in accordance with the supply trend of the aluminum scrap A even after the introduction of the aluminum scrap A is started.

The flux (F) is preferably supplied with the same amount as the amount of inclusions to be captured using this, but is not limited thereto. Therefore, the supply amount of flux F can be adjusted according to the supply amount of aluminum scrap A and the kind of aluminum scrap A. FIG. That is, when aluminum scrap A containing a large amount of paint or other inclusions is supplied, the supply amount of flux F is increased, and when aluminum scrap A with high purity is supplied, the supply amount of flux F is supplied. Can be reduced.

The raw material supply unit 25 is an apparatus for injecting the aluminum scraps A supplied from an external raw material supply source (not shown) into the molten aluminum M accommodated in the melting chamber 20.

As shown in FIG. 3, the raw material supply unit 25 injects aluminum scrap A into the vortex V generated by the vortex unit 21. Then, the aluminum scrap (A) can be rapidly immersed in the molten aluminum (M) and dissolved while turning down by the vortex (V), the contact between the aluminum scrap (A) immersed in the aluminum molten metal (M) is further contacted. By effectively blocking, the amount of aluminum oxide generated can be further reduced.

The injection timing of aluminum scrap (A) is not specifically limited. For example, the raw material supply unit 25 may start to input aluminum scrap A after the molten flux layer is formed on the surface of the aluminum molten metal M. For example, as shown in FIG. Then, the aluminum scrap (A) may be immersed in the aluminum molten metal (M) in a state where a molten flux layer is formed on the surface of the aluminum molten metal (M). For this reason, since the contact between the aluminum scrap A immersed in the molten aluminum M and the atmosphere is more effectively blocked, the amount of aluminum oxide can be further reduced.

If the diameter of the aluminum scrap (A) is large, there is a problem that the heat transfer rate is lowered. Therefore, it is preferable that aluminum scrap (A) has a diameter of 5 cm or less. The kind of such aluminum scrap (A) is not specifically limited. For example, the aluminum scraps A may be aluminum waste can scraps (UBCs, A 3XXX series, A 5XXXX series) mainly comprising aluminum, magnesium and aluminum alloys. The chemical composition of this aluminum waste can scrap is shown in Table 1.

part
Al alloy
line Chemical composition (%) Si Fe Cu Mn Zn Mg Body A 3004 <0.3 <0.70 <0.25 1.0-1.5 <0.25 0.8-1.3 Lid A 5052 <0.25 <0.40 <0.10 <0.10 <0.10 2.2-2.8 Tab A 5182 <0.2 <0.35 <0.15 0.2-0.5 <0.25 4.0-5.0

On the other hand, inclusions (inclusions) of the aluminum scrap (A), when the aluminum scrap (A) is charged and dissolved in the aluminum molten metal (M), has a property to aggregate with the molten aluminum. By the way, the molten flux layer, ie, flux F, weakens the cohesion between inclusions and molten aluminum to dissociate inclusions and molten aluminum, and selectively captures molten aluminum and dissociated inclusions to form black dross B ₁ . do. The black dross B ₁ has a specific gravity lower than that of molten aluminum due to its increased volume in the above-described forming process, and thus rises to the surface of the molten aluminum M. In addition, the black dross B ₁ As shown in FIGS. 3 and 4, when the vehicle descends by the vortex V and reaches the lower end of the vortex V, it is released from the vortex V, and then floated to the surface of the aluminum molten metal M. After that, it joins the vortex V again by the suction force of the vortex V. Thus, the black dross (B ₁₎ is coupled with the surface of the other black dross (B ₁₎ generated in the aluminum molten metal (M) through this process. When this process is repeated, as shown in FIG. 5, a spherical black dross B ₂ in which a plurality of black dross B ₁ is collected in a spherical form is formed. That is, the vortex unit 21 repeatedly lowers and floats the black dross B ₁ through the vortex V to form a spherical black dross B in which a plurality of black dross B ₁ is spherically collected. ₂ ) to form. The chemical composition of such spherical black dross (B ₂ ) is not specifically limited. For example, as described above, aluminum scrap (A) is aluminum waste can scrap (UBCs scrap) and flux (F) is 47.5 parts by weight sodium chloride (NaCl), 47.5 parts by weight potassium chloride (KCl) and potassium aluminum fluorine. If it comprises 5 parts by weight of the ride (KAlF ₄ ). The chemical composition of the spherical dross (B2) is shown in Table 2.

Chemical composition Chemical composition (%) Al 5-10 Al ₂ O ₃ 25-35 Mg 5-10 MgO 5-10 NaCl 20-30 KCl 20-30

Spherical black dross (B ₂ ) is a common black dross formed once without black dross (B ₁ ) gradually descending and floating the aluminum molten metal (M), without such a drop and injury process. Compared to the removal of inclusions is superior. Because of this, the case of forming the spherical black dross (B ₂₎ may be reduced with aluminum content in the dross in comparison with the case of forming the common black dross. That is, a general black dross, for example, a general black dross formed by fluxing white dross in a conventional aluminum waste can melting process has an aluminum content of about 50% or more, but a spherical black dross (B ₂ ) is about It has a content rate of aluminum of 10% or less. Therefore, by forming spherical black dross (B ₂ ), the dissolution recovery rate of pure aluminum can be improved. In addition, by forming the spherical black block dross (B2), it is possible to omit the dross reprocessing process for recovering the aluminum trapped in the dross by reprocessing the dross using a heating agent flux and a reprocessing indenter. The cost required for reprocessing can be reduced. The second flow passage 29 is a passage for transferring the molten aluminum M in which the aluminum scrap A is dissolved, to the heating chamber 10.

As shown in FIG. 2, the second flow passage 29 is formed through a wall partitioning the melting chamber 20 and the heating chamber 10, and the aluminum molten metal M is formed in the second flow passage 29. It is introduced into the heating chamber 10 through.

Next, the flow force provision chamber 30 is a space for applying flow force to the molten aluminum M so that the aluminum molten metal M can circulate between the heating chamber 10 and the melting chamber 20.

The flow force imparting chamber 30 communicates with the first flow passage 16 of the heating chamber 10 to receive the aluminum molten metal M from the heating chamber 10.

As shown in FIG. 2, the flow force imparting chamber 30 is preferably provided between the first flow passage 16 and the dissolution chamber 20 of the heating chamber 10. However, the present invention is not limited thereto, and the flow force applying chamber 30 may be installed between the second flow passage 29 and the heating chamber 10 of the dissolution chamber 20.

As shown in FIGS. 2 and 3, the flow force applying chamber 30 accelerates the aluminum molten metal M to impart a flow force to the aluminum molten metal M, and the flow force is imparted. And a third flow passage 34 for transferring the melted aluminum M to the dissolution chamber 20.

The acceleration unit 32 is provided in the flow force provision chamber 30 so that at least one part may be immersed in the molten aluminum M. FIG. For example, as shown in FIG. 3, the acceleration unit 32 receives a driving force from a driving motor (not dosing) provided outside the flow force applying chamber 30, and thus, the acceleration unit 32 receives the flow force to the flow force applying chamber 30. It may be a melt pump capable of circulating the received molten aluminum (M).

The third flow passage 34 is a passage for transmitting the molten aluminum M applied with the flow force by the acceleration unit 32 to the flow force applying chamber 30.

As shown in FIGS. 2 and 3, the third flow passage 34 penetrates so that the lower part of the wall partitioning the flow force imparting chamber 30 and the dissolution chamber 20 faces the impeller of the acceleration unit 32. The molten aluminum M is introduced into the dissolution chamber 20 through the third flow passage 34.

In the present specification, the flow force applying chamber 30 having the acceleration unit 32 is provided between the heating chamber 10 and the melting chamber 20, but the present invention is not limited thereto. That is, the vortex unit 20 of the melting chamber 20 forms the vortex V to raise and lower the aluminum molten metal M, and at the same time, transmit the flow force for circulating the aluminum melting furnace 2 to the aluminum molten metal M. FIG. Since it can be provided, the flow force provision chamber 30 and the acceleration unit 32 provided in this can be abbreviate | omitted.

6 is a plan view of a melting chamber showing a state in which a spherical black dross is suspended on the surface of the molten aluminum contained in the melting chamber of FIG. 2.

When a large number of spherical black dross (B ₂ ) is concentrated in the vortex (V), the lowering and floating action of the spherical black dross (B ₂ ) by the vortex (V) is weakened and the spherical black dross (B ₂ ) There is a fear that the formation efficiency of the amine may decrease. Therefore, it is preferable to adjust the density of the spherical black dross B ₂ located in the vortex V to an appropriate level by releasing the spherical black dross B ₂ grown by a predetermined reference diameter from the vortex V.

Based on the diameter of the spherical black dross (B ₂₎ it is not particularly limited. For example, aluminum scrap (A) is aluminum waste can scrap (UBCs scrap) and flux (F) is 47.5 parts by weight sodium chloride (NaCl), 47.5 parts by weight potassium chloride (KCl) and potassium aluminum fluoride (KAlF ₄ ) In the case of 5 parts by weight, the spherical black dross (B ₂ ) has a reference diameter of 2 cm to 5 cm.

In order to separate the spherical black dross B ₂ grown by the reference diameter from the vortex V, the dissolution chamber 20 separates the spherical black dross B ₂ from the vortex V ( 27) may further include.

As shown in FIG. 3, the separation unit 27 has a shape in which the spherical black dross B ₂ suspended on the surface of the aluminum molten metal M can be pulled away from the vortex V. 27a, and a connecting rod 27b connecting the driving device (not shown) and the separator 27a. Here, the drive device is preferably a work vehicle provided outside the melting chamber 20, but is not limited thereto.

As the separation unit 27 is provided in this way, the spherical black dross B ₂ having a predetermined reference diameter may be pulled away from the vortex V using the separation plate 27a to separate from the vortex V. Can be. Therefore, since the spherical black dross B ₂ is concentrated, the formation efficiency of the spherical black dross B ₂ can be prevented from falling. Here, the separation unit 27 may also perform a function of discharging the spherical black dross (B ₂ ) from the molten aluminum (M) to the outside.

On the other hand, when the spherical black dross B ₂ is pulled away from the vortex V using the separation unit 27, as shown in FIG. 6, the molten aluminum M accommodated in the dissolution chamber 20 is shown. The surface of) is covered with a spherical black dross (B ₂ ) deviating from the vortex (V). Therefore, the aluminum molten metal M contained in the melting chamber 20 is blocked from the atmosphere by the spherical black dross B ₂ covering the molten aluminum 20, and the spherical black dross B ₂ is the aluminum molten metal contained in the melting chamber 20. It has a thermal effect on (M). Therefore, being a heat loss of the aluminum molten metal (M) minimized by the rectangular black dross (B _2), the molten aluminum compared with the case the aluminum molten metal (M) is not covered by the spherical black dross (B ₂₎ (M Temperature rises.

In the conventional aluminum melting furnace, the temperature of the aluminum molten metal M contained in the melting chamber is generally 700 ° C. or lower, but the aluminum melting furnace 2 has the temperature of the aluminum molten metal M contained in the melting chamber 20 of 730 ° C. or higher. Can be raised. For this reason, in the aluminum melting furnace 2, the melting efficiency of aluminum scrap (A) can be further improved compared with the conventional aluminum melting furnace.

7 is a schematic view schematically showing the black dross recycling apparatus of FIG. 1.

When the aluminum scrap (A) is dissolved using the aluminum melting furnace (2) described above, a spherical black dross (B ₂ ) in which the black dross (B ₁ ) is spherically aggregated is formed. Spherical black dross (B ₂ ) not only contains a certain proportion of aluminum but is relatively low in comparison to a general black dross, but also contains a predetermined proportion of economically valuable compositions such as aluminum oxide, flux (F), and the like. . Accordingly, when the spherical black dross (B ₂ ) is disposed of as it is without reprocessing through landfilling or the like, the composition contained in the spherical black dross (B ₂ ) may not be recycled, thereby reducing economic efficiency. Spherical black dross (B ₂ ) may cause environmental pollution.

To solve this problem, aluminum black dross recycling system (1), spherical black dross (B ₂₎ Black dross recycling apparatus for processing recyclable spherical black dross (B ₂₎ for the recycling of the composition contained in the It includes (3).

As shown in FIG. 7, the black dross recycling apparatus 3 divides and spuns the spherical black dross B ₂ and divides it into aluminum grains N and dross fine powder P ₂ . (40) and a water decomposition unit (50) which decomposes the dross fine particle powder (P ₂ ) with water (W1) to decompose into soluble solids (S), insoluble solids (I), and hydrolysis gas (G). And a precipitation unit 60 for distilling the aqueous solution Q in which the soluble solids S are dissolved so that the soluble solids S is precipitated, and a soluble solids storage unit 70 for drying and storing the soluble solids S. , An aluminum grain storage unit 80 for storing aluminum grains N, an insoluble solids storage unit 90 for drying and baking insoluble solids I, and a gas storage for storing hydrolyzed gas G Unit 100 may be included.

First, the dividing unit 40 is an apparatus for crushing and crushing spherical black dross B ₂ .

Dividing unit 40, to remove the aluminum grains (N) and dross powder (P ₁₎ of the lysate of the crusher 41, and a rectangular black dross (B ₂₎ for crushing the spherical black dross (B ₂₎ first separating member 42 and the dross powder (P ₁₎ for grinding by the aluminum grains (N) and a grinder (43) of the pulverized product of the pulverizing mill (43) and a dross powder (P ₁₎ to which And a second separation member 44 which separates the atomized dross fine particle powder P ₂ .

The crusher 41 is an apparatus for crushing the spherical black dross B ₂ and dividing it into aluminum grains N and dross powder P ₁ .

Among the aluminum particles and aluminum alloy particles included in the spherical black dross (B ₂ ), the relatively large particle sizes and the aluminum alloy particles are agglomerated due to the heat generated when the spherical black dross (B ₂ ) is broken. Aluminum Granules and Aluminum Alloy Granules. In addition, among the aluminum particles and the aluminum alloy particles included in the spherical black dross (B ₂ ), the aluminum particles and the aluminum alloy particles having relatively small particle sizes are not aggregated to become aluminum powder and aluminum alloy powder. For convenience of explanation, hereinafter, aluminum grains N and aluminum alloy grains will be collectively referred to as aluminum grains N. FIG.

The crusher 41 breaks the spherical black dross B ₂ supplied from the aluminum melting furnace 2 by using the characteristics of the aluminum particles, and breaks it into aluminum grains N and dross powder P ₁ . will be. The dross powder (P ₁ ) includes the remaining compositions in the form of powder except for the relatively large particle size aluminum particles of the spherical black dross (B ₂ ).

The first separating member 42 is a member for separating the aluminum grains N and the dross powder P _{1 from} the crushed products of the spherical black dross B ₂ .

The structure of the first separating member 42 is not particularly limited. For example, the first separating member 42 may be composed of a vibrating screen having a predetermined first reference particle size. The first reference particle size is preferably about 10 mm, but is not limited thereto.

After the first separating member 42 separates the aluminum grains N and the dross powder P ₁ , the aluminum grains N are transferred to the aluminum storage unit 80 and the dross powder P _{1 is separated.} ) Is delivered to the grinder 43.

The crusher 43 is an apparatus for crushing dross powder P ₁ and dividing it into aluminum grains N and dross fine particle powder P ₂ .

Among the compositions contained in the dross powder (P ₁ ), insoluble solids (I) such as aluminum oxide and magnesium oxide are preferably atomized in order to easily recycle them. Therefore, the grinder 43 for grinding and atomizing the dross powder P ₁ is provided.

However, some of the aluminum particles included in the dross powder P ₁ may be agglomerated while the dross powder P ₁ is pulverized using the grinder 43 to produce aluminum grains N. Therefore, the crusher 43 grinds the dross powder P ₁ received from the first separating member 42, and divides the dross powder P ₁ into aluminum grains N and the finely divided dross fine powder P ₂ .

The second separating member 44 is a member for separating the aluminum grains N and the dross fine particle powder P _{2 from} the pulverized product of the dross powder P ₁ .

The structure of the second separating member 44 is not particularly limited. For example, the second separating member 44 may be configured as a trommel screen having a second predetermined particle size. The second reference particle size is preferably 0.5 mm, but is not limited thereto.

The second separating member 44 separates the aluminum grains N received from the grinder 43 and the dross fine particle powder P ₂ , and then the aluminum grains N are transferred to the aluminum grain storage unit 80. In addition, the dross fine particle powder (P ₂ ) is delivered to the reactor 51 of the water decomposition unit 50 to be described later.

8 is a photograph of dross particulate powder.

Next, the water decomposition unit 50 is an apparatus for water-decomposing the dross fine particle powder P ₂ received from the 2nd separating member 44.

As shown in FIG. 8, the dross fine particle powder P _{2 is} formed in a dark gray powder form, including compositions having various physicochemical properties such as salt flux, aluminum, aluminum-magnesium alloy, magnesium, and oxide. Have

So in order to recycle the compositions contained in such a de los particulate powder (P ₂₎ de los preferred that the conversion and decomposition so as to facilitate the recycling of the composition contained in the fine particle powder (P _2), to this dross fine powder (P ₂ ) Is provided with a water decomposition unit 50 capable of water decomposition.

FIG. 9 is a schematic view schematically showing the water decomposition unit shown in FIG. 7, FIG. 10 is a view showing a schematic structure of a trap shown in FIG. 9, and FIG. 11 is a plan view of the separators shown in FIG. 10. .

The water decomposition unit 50 has dross fine particles such that the dross fine particle powder P ₂ is decomposed into water (W1) to decompose into soluble solids (S), insoluble solids (I) and hydrolyzed gases (G). Water contained in the hydrolysis gas (G) by passing the hydrolysis gas (G) discharged from the reactor 51 and the reactor 51 for stirring the powder (P ₂ ) with water (W1) through the water (W2) And a condenser 53 for collecting impurities, a condenser 53 for cooling the hydrolysis gas G such that water vapor contained in the hydrolysis gas G discharged from the trap 52 is condensed, and a condenser from the condenser. Centrifuging the gas separation purifier 54 for separating and purifying the discharged hydrolysis gas (G), and the aqueous solution (Q) and insoluble solid (I) formed by dissolving soluble solids in water (W1) contained in the reactor 51. It may include a first centrifuge (55).

The reactor 51 is an apparatus for water-decomposing dross fine particle powder P2 by stirring dross fine particle powder P2 and water W1.

As shown in FIG. 9, the reactor 51 has a tank shape in which water W1 is accommodated therein by a predetermined level. In particular, the reactor 51 preferably has a predetermined volume such that a predetermined space is formed between the water surface of the water W1 accommodated therein and the ceiling surface of the reactor 51, but is not limited thereto.

The reactor 51, the dross fine particle powder (P ₂ ) and water (W1) mixed at a predetermined mixing ratio by stirring using at least one blade (51a), thereby causing the dross fine particle powder (P ₂ ) Water decomposes. The mixing ratio of the dross fine particle powder P ₂ and the water W1 is preferably 1: 2, but is not limited thereto.

Hereinafter, the physicochemical phenomenon that occurs when the dross fine particle powder (P ₂ ) is stirred with water (W1) will be described by dividing the properties of the compositions contained in the dross fine particle powder (P ₂ ).

First, the soluble solids (S) having solubility in water (W1) among the compositions contained in the dross fine particle powder (P ₂ ) are dissolved in water (W1), whereby the soluble solids (S) as a solute An aqueous solution (Q) containing and also containing water (W1) as a solvent is produced. Such soluble solids (S) mainly include chloride salts contained in flux (F) such as sodium chloride (NaCl) and potassium chloride (KCl). When the mixing ratio of the dross fine particle powder P ₂ and the water W1 is 1: 2, the concentration of the chloride salt in the aqueous solution Q is about 20%.

Next, insoluble solids (I) having insolubility insoluble in water (W1) among the compositions contained in the dross fine particle powder (P ₂ ) are dispersed or precipitated in the aqueous solution (Q). Insoluble solids (I) mainly include aluminum, aluminum-magnesium alloy, magnesium, aluminum oxide (Al ₂ O ₃ ), magnesium oxide (MgO), and spinel oxide (MgAl ₂ O ₄ ).

Next, among the compositions included in the dross fine particle powder P ₂ , a reactant having a property of being hydrolyzed by water W1 is hydrolyzed by water W1. By this hydrolysis reaction, water decomposition solids and hydrolysis gas (G) are generated, and reaction heat is generated with this. The reactants mainly include metals and metal compounds contained in spherical black dross (B ₂ ) such as aluminum (Al), magnesium (Mg), and aluminum carbide (Al ₄ C ₃ ). Here, aluminum carbide (Al ₄ C ₃ ) is not the first composition of the aluminum waste can, but is a by-product generated in the process of manufacturing aluminum waste can scrap by processing the aluminum waste can.

 Looking at the hydrolysis reaction of the reactant and water (W1), as shown in the reaction formulas 1 to 3, when aluminum and water (W1) is hydrolyzed, aluminum oxide and hydrogen are produced, magnesium and water (W1) is hydrolyzed Magnesium oxide and hydrogen are produced. When aluminum carbide and water (W1) are hydrolyzed, aluminum oxide and methane are produced. In particular, when aluminum or aluminum alloy is in contact with water (W1), the hydrolysis reaction occurs violently, and the temperature of water (W1) rises above 90 ° C, so that the above-mentioned hydrolysis reaction can be further promoted by such a temperature rise. Can be.

<Scheme 1>

2Al + 3H ₂ O →→ Al ₂ O ₃ + 3H ₂ + Heat

<Scheme 2>

Mg + H ₂ O →→ MgO + H ₂ + Heat

<Scheme 3>

Al ₄ C ₃ + 6H ₂ O →→ 2Al ₂ O ₃ + 3CH ₄ + Heat

The water-decomposed solids produced by such a hydrolysis reaction mainly contain insoluble solids such as aluminum oxide, magnesium oxide, aluminum oxide alloy, carbon component, and are dispersed or precipitated in the aqueous solution Q. Therefore, insoluble solution (I) already contained in spherical black dross (B ₂ ) and insoluble solids produced by the water decomposition reaction are dispersed or precipitated in aqueous solution Q, respectively. For convenience of explanation, hereinafter, the insoluble solids (I) already included in the spherical black dross (B ₂ ) and the insoluble solids produced by the water decomposition reaction will be collectively referred to as insoluble solids (I). .

On the other hand, in addition to the above-described aluminum, magnesium, aluminum carbide, a small amount of reactants contained in the dross fine particle powder (P ₂ ) is hydrolyzed, thereby generating various hydrolysis gases (G). The composition ratio of this hydrolysis gas (G) is shown in Table 3 below.

division Gas component (%) Hydrogen methane ethane Eten Propane Propene Hydrogen sulfide Early capture
(much) 48.14 51.55 0.020 0.009 0.009 0.012 0.0047 Terminal collection (small amount) 92.13 7.58 0.003 0.001 0.001 0.001 0.0020

As shown in Table 3, the hydrolysis gas G mainly contains methane gas (CH ₄ ) and hydrogen gas (H ₂ ). Such methane gas and hydrogen gas account for about 99% of the amount of hydrolysis gas G generated. In the initial stage of the water decomposition process, the hydrolysis reaction of aluminum, aluminum alloy, and aluminum carbide proceeds mainly to generate hydrogen gas and methane gas. At the end of the water decomposition process after a predetermined time has elapsed since the start of the water decomposition process, the hydrolysis reaction of aluminum and aluminum alloy proceeds mainly to generate hydrogen gas. The component analysis of the hydrolysis gas (G) is preferably performed using the gas chromatography (GC) analysis method of ASTM D1945-03, but is not limited thereto. Meanwhile, the method of measuring the amount of generation of the hydrolysis gas (G) Is not specifically limited. For example, the amount of hydrolyzed gas G can be measured by the following method. First, spherical black dross (B ₂ ) having a diameter of 2 cm to 5 cm is crushed and pulverized. Next, 0.5 cm (500 µm) passage of the crushed product of spherical black dross (B ₂ ) is obtained as a reaction sample. Thereafter, 100 g of the reaction sample and 1 L of distilled water were added to a closed glass flask having a 2 L capacity. Next, the reaction sample and the distilled water are stirred at 100 rpm to 200 rpm using the reactor 51 installed in the glass flask to decompose the reaction sample. Thereafter, the hydrolyzed gas G generated by the water decomposition of the reaction sample is collected by substituting aqueous phase from distilled water using a graduated cylinder. When 100 g of the reaction sample is water-decomposed through this test process, 8 L to 12 L of hydrolysis gas (G) can be collected.

The trap 52 is an apparatus for collecting water vapor and impurities contained in the high temperature hydrolysis gas G discharged from the reactor 51 by using water W2.

As shown in FIG. 9, the hydrolysis gas G generated by the hydrolysis reaction in the reactor 51 is floated in the water W1 contained in the reactor 51 and then the water contained in the reactor 51 ( By being separated from the water W1 contained in the reactor 51 through the water surface of W1, it is introduced into the space between the water surface of the water W1 contained in the reactor 51 and the ceiling surface of the reactor 51.

However, in the reactor 51, since the reactant having the property of being hydrolyzed by the water W1 is violently hydrolyzed by the water W1, the heat of reaction is generated, so that the water W1 contained in the reactor 51 is the reaction heat. Heated violently. Thus, the hydrolysis gas G released from the water W1 accommodated in the reactor 51 is finely crushed by the water W1 contained in the reactor 51, and the water contained in the reactor 51 ( W1) may include moisture containing water vapor generated by evaporation, impurities including spherical black dross (B ₂ ), by-products generated in the process of manufacturing aluminum scrap (A), and the like. Therefore, since the hydrolysis gas G is discharged from the reactor 51 in a state in which the purity is lowered due to such moisture and impurities, the combustion rate is remarkable when the hydrolysis gas G is used as it is discharged from the reactor 51. Problems such as lowering will occur.

In order to solve this problem, the trap 52 is provided to increase the purity of the hydrolysis gas (G) by filtering the hydrolysis gas (G) using water (W1). As shown in FIG. 9, the trap 52 has a tank shape in which water W2 is accommodated therein by a predetermined level. In particular, the trap 52 preferably has a predetermined volume so that a predetermined space is formed between the water surface of the water W2 accommodated therein and the ceiling surface of the trap 52, but is not limited thereto.

The trap 52 is connected to the reactor 51 by the first connection line 56 to receive the hydrolysis gas G from the reactor 51. The first connection line 56 is provided such that the hydrolysis gas G released from the water W1 contained in the reactor 51 passes through the water W2 contained in the trap 52. For example, as shown in FIG. 9, one end of the first connection line 56 is in communication with the space between the water surface of the water W1 accommodated in the reactor 51 and the ceiling surface of the reactor 51, It may be fixed to one side wall of the reactor (51). Correspondingly, the other end of the first connection line 56 may be inserted into the trap 52 through one side wall of the trap 52. In particular, as shown in FIG. 10, the other end of the first connection line 56 includes an extension 56a and an extension 56a provided to be immersed in the water W2 accommodated in the trap 52. It may have a discharge portion (56b) for discharging the hydrolyzed gas (G) passed to the water (W2) accommodated in the trap 52.

As shown in FIG. 10, the upper end of the extension portion 56a may be formed by the trap 52 from the water surface of the water W 2 contained in the trap 52 so as not to be submerged in the water W 2 contained in the trap 52. It is extended to be spaced toward the ceiling surface. Through this, the extension 56a may prevent the water W2 contained in the trap 52 from flowing back toward the reactor 51 beyond the upper end of the extension 56a.

As shown in FIG. 10, the lower end of the extension 56a is formed to be spaced apart from the water surface of the water W2 accommodated in the trap 52 toward the bottom surface of the trap 52. Then, the extension portion 56a is connected to the water W2 accommodated in the trap 52 by a depth corresponding to the distance between the water surface of the water W2 contained in the trap 52 and the lower end of the extension portion 56a. It is locked.

As shown in FIG. 10, the discharge portion 56b is formed extending from the lower end of the extension portion 56a so as to be immersed in the water W2 contained in the trap 52. In particular, the discharge portion 56b is preferably formed at the same height as the lower end of the extension portion 56a, but is not limited thereto. The discharge part 56b includes at least one injection hole 56c which is punctured to inject the hydrolysis gas G passing through the extension part 56a into the water W2 contained in the trap 52. Can have. According to the injection holes 56c, the inside of the trap 52 and the inside of the first connection line 56 communicate with each other. Therefore, the water W2 contained in the trap 52 is filled through the injection holes 56c inside the discharge part 56b and the extension part 56a.

According to this first connecting line 56, the hydrolysis gas G released from the water surface of the water W1 received in the reactor 51 passes through the first connecting line (1) through one end of the first connecting line 56. 56). Next, the hydrolysis gas G introduced into the first connection line 56 flows along the first connection line 56 and then flows into the water W2 contained in the extension 56a. Thereafter, the hydrolysis gas G introduced into the water W2 contained in the extension 56a flows along the extension 56a and the discharge portion 56b and is trapped through the injection holes 56c. It is sprayed into the water W2 accommodated in 52. Then, moisture and impurities contained in the hydrolysis gas G are collected by the water W2 in the course of passing through the water W2 accommodated in the first connection line 56 and the trap 52. Thus, the trap 52 can filter the hydrolysis gas G primarily using water W2, and can raise the purity of the hydrolysis gas G. FIG.

In addition, the inside of the first connection line 56 is trapped through the injection holes 56c of the discharge portion 56b disposed to be immersed in the water W2 received in the trap 52 by a predetermined depth. 52) is connected to the inside. Therefore, a high pressure is applied to the water W2 contained in the first connection line 56 in proportion to the capacity of the water W2 contained in the trap 52. This high pressure can act as a pressure load when the hydrolysis gas G enters the water W2 contained inside the first connection line 56. As a result, the internal pressure of the reactor 51 connected with the first connection line 56 and the first connection line 56 may be increased by the water W2 contained in the first connection line 56. . Then, the internal pressure of the reactor 51 is increased higher than the atmospheric pressure, so that the boiling point of the water (W1) accommodated in the reactor 51 can be increased higher than the boiling point of 100 ° C of water at atmospheric pressure. For example, when the internal pressure of the reactor 51 is increased to 1.5 kg / cm 2, the boiling point of the water W1 contained in the reactor 51 may be increased to about 140 ° C. to 150 ° C. As such, when the boiling point of the water W1 contained in the reactor 51 is increased, the water decomposition reaction in the reactor 51 may be promoted, so that the trap 52 and the first connection line 56 are connected to the reactor 51. ) Can improve the water decomposition performance.

Meanwhile, the hydrolyzed gas G, which is primarily filtered while passing through the water W2 accommodated in the first connection line 56 and the trap 52, has a water surface of the water W2 housed in the trap 52. To escape from the water W2 contained in the trap 52. However, if the hydrolysis gas (G) is primarily filtered using water (W2), most of the impurities containing solid by-products, dust, and the like are removed, but a part of the water containing liquid droplets and vapor vapor, etc. Can still be included in the hydrolysis gas (G). Accordingly, the trap 52 may include a plurality of separation plates 52a and 52b provided to separate residual water such as water droplets and water vapor contained in the hydrolysis gas G from the hydrolysis gas G. Can be.

The separating plates 52a and 52b are arranged at a predetermined interval in the space between the water surface of the water W2 accommodated in the trap 52 and the ceiling surface of the trap 52. The number of installation of the separation plates 52a and 52b is not particularly limited. For example, as shown in FIG. 10, in the space between the water surface of the water W2 accommodated in the trap 52 and the ceiling surface of the trap 52, a pair of separator plates 52a and 52b are provided. Can be installed.

As shown in Figs. 11 (a) and 11 (b), each of the separation plates 52a and 52b receives the hydrolysis gas G released from the water W2 contained in the trap 52 and the condenser ( 53 may have at least one guide holes 52c, 52d perforated to be guided toward 53). In particular, as shown in FIG. 11 (c), the separating plates 52a and 52b are formed so that the guide holes 52c and 52d provided in the respective separating plates 52a and 52b are alternately positioned. Can be. Then, the hydrolysis gas G which enters into the space between the lower separating plate 52a and the upper separating plate 52b through the guide holes 52c of the lower separating plate 52a is the lower separating plate 52a. Guide holes 52c of the upper separation plate 52b and the guide holes 52d of the upper separation plate at least by bypassing the space between the lower separation plate 52a and the upper separation plate 52b at a distance from each other, the upper separation It can be guided toward the condenser 53 through the guide holes 52d of the plate 52b. As a result, the residual moisture contained in the hydrolysis gas G is formed by colliding with the wall surfaces of the separators 52a and 52b around the droplets having a relatively large particle size. Accordingly, the trap 52 may further filter the hydrolysis gas G using the separators 52a and 52b to further increase the purity of the hydrolysis gas G.

The condenser 53 is a device for cooling the hydrolysis gas G discharged from the trap 52 to condense the water vapor contained in the hydrolysis gas G.

In the trap 52, the hydrolysis gas G is secondarily filtered by water W2 and the separators 52a, 52b, but the hydrolysis gas G may still contain traces of water vapor. . In order to solve this problem, the condenser 53 is provided to increase the purity of the hydrolysis gas G by filtering the hydrolysis gas G using condensation of water vapor. As shown in FIG. 9, the condenser 53 includes an inlet 53a through which the hydrolyzed gas G discharged from the trap 52 flows in and a hydrolyzed gas passed through the inlet 53a ( Heat exchanger (53b) for condensing water vapor contained in hydrolysis gas (G) by exchanging G) with the refrigerant, and discharge portion (53c) through which hydrolyzed gas (G) passed through heat exchanger (53b) is discharged. And the like.

The kind of refrigerant which can be used for condensation of the water vapor contained in the hydrolysis gas G is not specifically limited. For example, the refrigerant may be air, water, or the like.

As shown in FIG. 9, the condenser 53 is installed to be inclined such that the discharge part 53c is lower than the inlet part 53a. Then, the condensed water formed by condensation of water vapor in the heat exchange part 53b may flow toward the discharge part 53c by gravity.

The condenser 53 is connected to the trap 52 by the second connection line 57 so that the hydrolysis gas G can be delivered from the trap 52. The second connection line 57 is provided such that the hydrolysis gas G passing through the separator plates 52a and 52b is delivered to the inlet portion 53a of the condenser 53. For example, as shown in FIG. 9, one end of the second connection line 57 communicates with the space between the separator plates 52a and 52b and the ceiling surface of the trap 52. It can be fixed to one side wall. Correspondingly, the other end of the second connection line 57 may be fixed to one side wall of the condenser 53 so as to communicate with the inside of the inflow portion 53a.

According to the second connecting line 57, the hydrolysis gas G passing through the separator plates 52a and 52b with water vapor included is an inlet of the condenser 53 through the second connecting line 57. Flows into 53a. Next, the hydrolysis gas G introduced into the inlet 53a of the condenser 53 is exchanged with the refrigerant while passing through the heat exchanger 53b. In this process, the hydrolysis gas G and the water vapor contained therein are cooled by the refrigerant, so that the water vapor contained in the hydrolysis gas G is condensed to form condensed water. Thereafter, the hydrolysis gas G and the condensate are separately delivered to the discharge portion 53c of the condenser 53 in a state separated from each other. In addition, as shown in FIG. 9, the hydrolysis gas G delivered to the outlet 53c of the condenser 53 is delivered to the gas separation purifier 54 through the third connection line 58, and the condenser The condensed water delivered to the discharge portion 53c of the 53 is accommodated in the gas pressure compensation line 59 to be described later.

Such a condenser 53 can thirdly filter the hydrolysis gas G by condensation of water vapor, thereby further increasing the purity of the hydrolysis gas G.

On the other hand, as the hydrolysis gas G is cooled by the refrigerant in the heat exchange part 53b of the condenser 53 and the volume shrinks, the hydrolysis gas G of the discharge part 53c of the condenser 53 is reduced. The pressure is lower than the pressure of the hydrolysis gas G at the inlet 53a of the condenser 53. In order to eliminate the pressure unevenness of the hydrolysis gas G, as shown in FIG. 9, the water decomposition unit 50 includes the water W2 accommodated in the trap 52 and the condensed water accommodated in the condenser 53. Are respectively introduced, and further comprising a gas pressure compensation line 59 connected to the trap 52 and the condenser 53 so that the negative pressure generated by cooling the hydrolysis gas G in the condenser 53 is transmitted. can do.

As illustrated in FIG. 9, the gas pressure compensating line 59 may include a first inlet 59a connected to the trap 52 so that water W 2 contained in the trap 52 is introduced by water pressure, and a condenser The second inlet 59b connected to the outlet 53c of the condenser 53 and the water W2 introduced through the first inlet 59a so that the condensed water accommodated in the outlet 53c of the 53 is introduced by gravity. And the mixed water chamber 59c formed to accommodate at least a portion of the mixed water mixed with each other and the condensed water introduced through the second inlet 59b and the trap 52 and the mixed water chamber 59c selectively. The first on-off valve 59d provided between the trap 52 and the mixed water chamber 59c, the discharge part 53c of the condenser 53, and the mixed water chamber 59c can be selectively communicated with each other. The second open / close valve 59e provided between the discharge part 53c of the condenser 53 and the mixed water chamber 59c, and the mixed water accommodated in the gas pressure compensation line 59 to the outside. It may have a drain valve (59f) and the like is installed to be selectively discharged. In addition, the gas pressure compensation line 59 may have a 'U'-shaped structure in which first inlets 59a and second inlets 59b are formed at both ends, respectively, so that a predetermined amount of mixed water may be accumulated therein. It is not limited to this.

The first inlet 59a may be configured such that the water W2 located at a point separated from the water surface of the water W2 accommodated in the trap 52 by a predetermined depth may be introduced by the hydraulic pressure. It is connected to one side wall. The second inlet 59b is connected to one side wall of the condenser 53 so that the condensed water collected at the bottom surface of the outlet 53c of the condenser 53 may be introduced by gravity. According to the first inlet 59a and the second inlet 59b, the water W2 accommodated in the trap 52 and the condensed water accommodated in the discharge part 53c of the condenser 53 are provided in the first inlet 59a and the second inlet 59b. As each of the gas pressure compensation line 59 is introduced into the gas pressure compensation line 59 through the second inlet 59b, the water W2 introduced from the trap 52 and the condensed water introduced from the condenser 53 are introduced into the gas pressure compensation line 59. Mixed water mixed with each other is accommodated. The quantity of the mixed water accommodated in the gas pressure compensation line 59 can be adjusted by selectively driving the first open / close valve 59d, the second open / close valve 59e and the drain valve 59f.

The mixed water chamber 59c is provided so that at least a portion of the mixed water can be accommodated. For example, the mixed water chamber 59c may be installed to be at the same height as the first inlet 59a so that the surface of the mixed water may be formed in the mixed water chamber 59c. However, when the second inlet 59b is located at a lower level than the first inlet 59a, the surface of the mixed water cannot be located in the mixed water chamber 59c. Therefore, the gas pressure compensation line 59 is installed so that the second inlet port 59b is located at a higher height than the first inlet port 59a.

In addition, the mixed water chamber 59c may have an observation window 59g formed so that the change in the level of the mixed water can be observed. For example, the observation window 59g may be composed of glass formed to be able to project the inside of the mixed water chamber 59c. Through the observation window (59g) it is possible to observe the position and the water level change of the surface of the mixed water from the outside.

According to such a gas pressure compensation line 59, the pressure of the hydrolysis gas G at the outlet 53c of the condenser 53 is reduced to that of the hydrolysis gas G at the inlet 53a of the condenser 53. In the case where the pressure is lower than the pressure, negative pressure acts toward the discharge portion 53c of the condenser 53 to the mixed water accommodated in the gas pressure compensation line 59. The magnitude of this negative pressure is the pressure difference between the pressure of the hydrolysis gas G at the inlet portion 53a of the condenser 53 and the pressure of the hydrolysis gas G at the discharge portion 53c of the condenser 53. Proportional to According to such a negative pressure, the mixed water accommodated in the gas pressure compensation line 59 is sucked by the negative pressure toward the discharge part 53c of the condenser 53, and the surface of the mixed water rises. Then, the pressure of the hydrolysis gas G in the discharge part 53c of the condenser 53 is compensated for by the rise of the water level of the mixed water, so that the hydrolysis gas G in the discharge part 53c of the condenser 53 is compensated. ) Pressure is increased. Accordingly, the gas pressure compensation line 59 receives the pressure of the hydrolysis gas G at the outlet 53c of the condenser 53 through the pressure compensation and hydrolyzes the gas at the inlet 53a of the condenser 53. It can be adjusted equally to the pressure of the gas (G).

The gas separation purifier 54 collects the gases contained in the hydrolyzed hydrolyzate G in order to increase the purity of the recyclable gas in the hydrolyzed hydrolyzate G or to separate a specific gas suitable for recycling purposes from other gases. It is provided to be separated and purified. The configuration of such a gas separation purifier 54 is not particularly limited. For example, the gas separation purifier 54 may be provided to separate and purify gases contained in the hydrolysis gas G through a pressure swing adsorption method. For example, the gas separation purifier 54 may be provided to convert the methane gas separated and purified from the hydrolysis gas G through hydrogen steam methane reforming to be converted into hydrogen gas. The hydrolyzed hydrolyzate G separated and purified in the gas separation purifier 54 may be delivered to the gas storage unit 100 through the gas storage line 110.

The first centrifugal separator 55 is an apparatus for centrifuging the aqueous solution Q and the insoluble solid component I.

As described above, the hydrolysis gas G generated in the reactor 51 is filtered by the trap 52 and the condenser 53 after being separated from the water W 1 contained in the reactor 51, but the reactor 51 Soluble solids (S) produced in) is dissolved in water (W1) contained in the reactor 51 to form an aqueous solution (Q) with water (W1), the insoluble solids (I) produced in the reactor 51 Precipitates in this aqueous solution (Q). As shown in FIG. 7, the first centrifugal separator 55 is provided to receive such an aqueous solution Q and an insoluble solid I from the reactor 51.

The first centrifuge 55 is preferably configured as a B.S.P centrifuge, but is not limited thereto. The first centrifugal separator 55 may include a first filter having a third reference particle size predetermined so that the aqueous solution Q and the insoluble solid content I can be separated. The first filter is a nonwoven filter, and the third reference particle size is preferably 7 μm to 15 μm, but is not limited thereto.

The first centrifuge 55, after centrifuging the aqueous solution (Q) and insoluble solids (I) using a first filter, the aqueous solution (Q) is transferred to the precipitation unit (60) and the insoluble solids (I) is Deliver to insoluble solids storage unit 90.

On the other hand, the insoluble solid (I) and the aqueous solution (Q) is separated by the first centrifugal separator 55, but some of the aqueous solution (Q) can not be separated and can be adsorbed to the insoluble solid (I). By the way, since the aqueous solution (Q) contains the soluble solids (S), there is a fear that the product prepared by recycling the insoluble solids (I) may be corroded by the chlorides contained in the soluble solids (S). In addition, when the insoluble solid (I) is dried or calcined, sodium oxide (Na ₂ O) and potassium oxide (K ₂ 0) are generated from chlorides contained in the soluble solid (S). There exists a possibility that the durability of the manufacture manufactured by recycling insoluble solid content (I) by potassium may fall.

In order to prevent this, the first centrifuge 55 washes the insoluble solids (I) adsorbed with the aqueous solution (Q) using distilled water so that the chlorine concentration of the insoluble solids (I) is less than or equal to a predetermined reference chlorine concentration. Distilled water used for washing solid (I) and insoluble solid (I) can be centrifuged. The washing process of insoluble solids (I) using such distilled water may be repeatedly performed until the chlorine concentration of the insoluble solids (I) is below the reference chlorine concentration. The reference chlorine concentration is preferably 300 ppm, but is not limited thereto. Here, the first centrifugal separator 55 is an insoluble solid (I) as distilled water (D) generated by condensation (64) of the precipitation unit (60), which will be described later, by condensing the water vapor (T) evaporated in the vacuum distillation unit (62). ), But is not limited thereto.

Next, the precipitation unit 60 is an apparatus for distilling the aqueous solution Q such that the soluble solid content S is precipitated from the aqueous solution Q.

The precipitation unit 60 includes a vacuum distillation unit 62 for distilling the aqueous solution Q under reduced pressure at a predetermined temperature and pressure to precipitate soluble solids S, and water W1 contained in the aqueous solution Q is a vacuum distillation unit. The condenser 64 which condenses the water vapor T generated by evaporation by 62 to produce distilled water D, and the soluble solids S and the aqueous solution Q precipitated by the vacuum distillation 62 are centrifuged. It may include a second centrifuge 66 for separating.

The vacuum distillation unit 62 is an apparatus for depositing the aqueous solution Q discharged from the first centrifugal separator 55 under reduced pressure at a predetermined reduced pressure distillation temperature and a reduced pressure distillation pressure to precipitate soluble solids S.

The vacuum distillation unit 62 may be constituted by a general vacuum distillation unit used to precipitate the solute from the water solvent. The vacuum distillation temperature and the vacuum distillation pressure of the vacuum distillation unit 62 are set in consideration of the sensitivity of crystal growth of the soluble solids S. However, since the soluble solids (S) mainly include chloride salts contained in the flux (F), such as sodium chloride (NaCl), potassium chloride (KCl), the reduced-pressure distillation temperature is set to 40 ℃ ℃ to 70 ℃ ℃ And, the reduced-pressure distillation pressure is preferably set to 12 kPa to 40 kPa, but is not limited thereto.

When the aqueous solution (Q) is distilled under reduced pressure under such a temperature and pressure, the water (W1) contained in the aqueous solution (Q) evaporates and the concentration of the soluble solids (S) increases, and when the concentration of the soluble solids (S) reaches a saturated concentration, Soluble solid (S) precipitates from aqueous solution (Q) and starts to crystallize. The saturation concentration is not particularly limited. For example, when the vacuum distillation temperature is about 65 ° C. and the vacuum distillation pressure is about 27 kPa, the saturation concentration of the aqueous solution Q ₁ by vacuum distillation is 27% to 30%.

When the aqueous solution Q is distilled under reduced pressure in this manner, the aqueous solution Q is vaporized by evaporation under reduced pressure, the soluble solids S precipitated and crystallized from the aqueous solution Q, and the remaining solubility not precipitated. solid (S) is separated into an aqueous solution (Q ₁₎ is dissolved. The vacuum distillation unit 62 transmits water vapor T to the condenser 64, and delivers the aqueous solution Q ₁ in which the precipitated crystallized soluble solids S are dispersed and precipitated to the second centrifuge 66. .

The condenser 64 is a device for condensing moisture to generate distilled water (D).

The condenser 64 condenses the water received from the vacuum distillation 62 to produce distilled water D. The condenser 64 transfers the distilled water D to the first centrifuge 55 so that the first centrifuge 55 can wash the insoluble solids I separated from the aqueous solution Q with distilled water D. Preferably, but not limited to.

The second centrifuge 66 is a device for centrifuging the soluble solids S and the aqueous solution Q ₁ received from the vacuum distillation 62.

The second centrifugal separator 66 is preferably configured as a Contavex centrifuge, but is not limited thereto. The second centrifuge 66 may include a second filter having a fourth reference particle size predetermined to separate the soluble solids S and the aqueous solution Q ₁ . The second filter is a wire mesh filter, and the fourth reference particle size is preferably 0.05 mm to 0.3 mm, but is not limited thereto.

The second centrifuge 66, after centrifuging the soluble solids (S) and the aqueous solution (Q ₁ ) using a second filter, the soluble solids (S) is transferred to the soluble solids storage unit 70 and the aqueous solution (Q) ₁ ) is passed back to the vacuum distillation unit 62.

The vacuum distillation unit 62 repressurizes the aqueous solution Q ₁ re-delivered from the second centrifuge 66 at a predetermined temperature and pressure. This reduced pressure distillation and centrifugation process may be repeatedly performed several times. To this end, a plurality of vacuum distillation units 62 having different vacuum distillation temperatures and vacuum distillation pressures may be provided to selectively re-precipitate the soluble solids S using any one of the vacuum distillation units 62 according to the process sequence. Can be.

On the other hand, it was demonstrated that the soluble solid content S is reprecipitated from the aqueous solution Q ₁ using the vacuum distillation machine 62, but it is not limited to this. For example, the precipitation unit 60 may further include at least one of solar exposure salt salt and forced evaporative indoor salt salt in order to reprecipitate the soluble solids S from the aqueous solution Q ₁ . The photovoltaic exposure to the solar exposure and forced evaporation indoor salt, respectively, may precipitate the soluble solids (S) from the aqueous solution (Q ₁ ) delivered from the second centrifuge (66) and deliver it to the soluble solids storage unit (70).

12 is a photograph of soluble solids precipitated and dried, FIG. 13 is a SEM-EDS chart qualitatively analyzing the soluble solids shown in FIG. 12, and FIG. 14 is a chart showing the composition ratio of the soluble solids shown in FIG. 12. .

Next, the soluble solids storage unit 70 is a device for drying and storing the soluble solids (S) received from the second centrifuge (66).

The structure of the soluble solids storage unit 70 is not particularly limited. For example, the soluble solids storage unit 70 includes a soluble solids dryer 72 for drying the soluble solids S, and a soluble solids for storing the soluble solids S ₁ dried by the soluble solids dryer 72. Storage chamber 74.

The soluble solids dryer 72 is an apparatus for drying the soluble solids S separated from the aqueous solution Q ₁ by the second centrifuge 66.

The soluble solids (S) and the aqueous solution (Q ₁ ) are separated by the second centrifuge 66, but some of the aqueous solutions (Q ₁ ) are not separated from the soluble solids (S) on the surface of the soluble solids (S). Can be adsorbed. For this reason, the soluble solid S separated from the aqueous solution Q ₁ by the second centrifuge 66 is present in the slurry state by the aqueous solution Q ₁ adsorbed on the surface. By the way, if the soluble solids (S) is present in the slurry state is not easy to recycle, so that the soluble solids dryer 72 is provided to solve this.

This soluble solids dryer 72 dries the soluble solids S discharged from the second centrifuge 66 so that the soluble solids S contain water of less than a predetermined reference moisture. The reference moisture is preferably about 0.3%, but is not limited thereto.

The dried soluble solids (S ₁ ), as shown in FIGS. 12 and 13, have a white powder form and mainly include chloride salts such as NaCl and KCl. The soluble solids dryer 72 delivers the soluble solids S ₁ thus dried to the soluble solids storage chamber 74.

The soluble solids storage chamber 74 is a device for storing soluble solids S ₁ from which moisture has been removed by the soluble solids dryer 72.

The soluble solids storage chamber 74 may be configured as a general storage chamber capable of storing a storage object. The soluble solids storage chamber 74 receives the soluble solids S ₁ from which moisture is removed from the soluble solids dryer 72 and stores the soluble solids S ₁ in an isolated state from the outside. The soluble solids S ₁ stored in the soluble solids storage chamber 74 mainly contain chloride salts contained in the fluxes F, as shown in FIGS. 13 and 14, so that they are recycled as fluxes F. desirable. However, the present invention is not limited thereto, and the soluble solid (S ₁ ) may be recycled in various fields requiring mixed salts.

Next, the aluminum grain storage unit 80 is a device for storing aluminum grains N discharged from the dividing unit 40.

The structure of the aluminum grain storage unit 80 is not specifically limited. For example, the aluminum grain storage unit 80 may store aluminum grains N, which are separated and discharged from the first separating member 42 and the second separating member 44, as shown in FIG. 7. It may include a grain storage chamber 82.

Next, the insoluble solids storage unit 90 is an apparatus for drying, baking, and storing the insoluble solids I received from the first centrifuge 55.

The structure of the insoluble solids storage unit 90 is not particularly limited. For example, the insoluble solids storage unit 90 includes the insoluble solids dryer 92 for drying the insoluble solids I and the insoluble solids I ₁ dried by the insoluble solids dryer 92. The kiln 94 and an insoluble solids storage chamber 96 for storing the insoluble solids I ₂ fired by the insoluble solids kiln 94 may be included.

It is a photograph of the insoluble solid content dried.

The insoluble solids dryer 92 is an apparatus for drying the insoluble solids I separated from the aqueous solution Q by the first centrifuge 55.

Insoluble solids (I) are separated by distilled water (D) and the first centrifugal separator (55), but some distilled water (D) is adsorbed on the surface of insoluble solids (I) without being separated from insoluble solids (I). Can be. For this reason, the insoluble solid content I discharged | emitted from the 1st centrifugal separator 55 exists in the slurry state containing about 30 to 40% of water. By the way, when the insoluble solid (I) is present in the slurry state is not easy to transport and recycle the insoluble solid (I), insoluble solids dryer 92 is provided to solve this.

The insoluble solids dryer 92 dries the insoluble solids I discharged from the first centrifugal separator 55 such that the insoluble solids I contain moisture of less than or equal to a predetermined reference moisture.

The reference moisture is not particularly limited and is preferably set differently according to the purpose of recycling the insoluble solid content (I). For example, when the insoluble solid (I) is recycled to the cement raw material, the reference moisture is about 40%. For example, when the insoluble solid (I) is recycled into a brick refractory or ceramic material, the reference moisture is about 0.5%. For reference, when the insoluble solid (I) is recycled to brick refractory or ceramic material, a material calcined at about 1,200 ° C. is required, so that the insoluble solid (I) is relatively lower than that of the cement raw material. Reference moisture is required.

The insoluble solids I ₁ dried by the insoluble solids dryer 92 have a dark gray powder form due to the carbon component adsorbed on the surface, as shown in FIG. 15. This insoluble solid (I ₁ ) is delivered to the insoluble solid kiln 94.

FIG. 16 is a photograph of calcined insoluble solids, FIG. 17 is a SEM-EDS chart qualitatively analyzing calcined insoluble solids shown in FIG. 16, and FIG. 18 is a composition ratio of calcined insoluble solids shown in FIG. 16. This is a chart showing.

The insoluble solids baking furnace 94 is an apparatus for baking the insoluble solids I ₁ dried by the insoluble solids dryer 92.

When the finely divided aluminum, magnesium and aluminum alloy contained in the dross fine particle powder P ₂ are water-decomposed, aluminum hydroxide, magnesium hydroxide and aluminum alloy hydrate (hereinafter, referred to as 'hydrates') may be formed. Since these hydrates are insoluble solids (I), they are separated from the aqueous solution (Q) by the first centrifuge (55) and transferred to the insoluble solids dryer (92). However, since hydrates are unstable compared to aluminum oxide, magnesium oxide and aluminum alloy oxide (hereinafter referred to as 'oxides'), insoluble solids (I) containing such hydrates are not suitable for recycling.

To solve this problem, the water-insoluble solid content storage unit 90, as illustrated in Figure 7, the water-insoluble solids to a water insoluble solid content (I ₁₎ treated dried by the insoluble solids dryer (92) the firing process (I ₁₎ And an insoluble solids kiln 94 for transferring the contained hydrates to the oxides.

The insoluble solids firing furnace 94 heats the insoluble solids (I ₁ ) to about 800 ° C. or higher to calcinate the hydrates. The hydrates are then calcined and transferred to oxides, while at the same time the carbon component adsorbed on the surface of the insoluble solid (I ₁ ) is combusted. Therefore, the insoluble solid (I ₂ ) fired by the insoluble solid baking (94) is in the form of a pale yellow powder, as shown in FIG. The insoluble solids kiln 94 transfers such insoluble solids I ₂ to the insoluble solids storage chamber 96.

On the other hand, when the insoluble solids firing furnace 94 has a structure capable of continuously performing the drying process and the firing process like the microwave firing furnace, the insoluble solids dryer 92 described above may be omitted.

The insoluble solids storage chamber 96 is a device for storing insoluble solids I ₂ fired by the insoluble solids kiln 94.

Insoluble solids storage chamber 96 may be configured as a general storage chamber capable of storing a storage object. The insoluble solids storage chamber 96 receives the insoluble solids I ₂ from the insoluble solids kiln 94 and stores the insoluble solids I ₂ in an isolated state. Insoluble solids (I ₂ ) mainly contain aluminum oxide, magnesium oxide, and aluminum oxide alloys, as shown in FIGS. 17 and 18, and are thus recycled as ceramic materials, refractory materials, cement materials after further reactivation processes. It is desirable to be. The further recycling step of insoluble solid content (I ₂ ) is not particularly limited. For example, an additional recycling process of insoluble solids may include a spinel manufacturing process in which aluminum oxide and magnesium oxide are calcined at about 2000 ° C. at high temperature to be transferred to spinel (MgAl ₂ O ₄ ).

Next, the gas storage unit 100 is an apparatus for storing the hydrolysis gas G discharged from the condenser 53.

The gas storage unit 100 may be composed of a gas storage chamber which is generally used for storing gas. The gas storage unit 100 is connected to the outlet 53c of the condenser 53 by the gas storage line 110, as shown in FIG. 9. Therefore, the gas storage unit 100 stores the hydrolysis gas G discharged from the discharge part 53c of the condenser 53 through the gas storage line 110. The gas storage unit 100 may supply the hydrolysis gas G stored therein at a predetermined pressure.

The general dross reprocessing machine (indenter) inputs a heating agent flux such as saltpeter (NaNO ₃ ) into the general black dross and reprocesss the general black dross. Water recombination of the reprocessed general black dross generates ammonia gas (NH ₃ ) and silane gas (SiH ₄ ), which are toxic to the human body, from aluminum nitride and aluminum silicide contained in the general black dross. Therefore, the gas generated by water decomposition of the reprocessed general black dross is difficult to recycle.

By the way, the hydrolysis gas G generated by processing the spherical black dross B ₂ by the black dross recycling apparatus 3 includes gases such as hydrogen, methane, ethane, ethene, propane and propene. do. These gases are easy to recycle because they do not have the same toxicity as the ammonia gas and silane gas described above as gases that can be used as energy sources. In addition, since hydrogen and methane having excellent properties as energy sources occupy most of the hydrolysis gas G, the hydrolysis gas G is very excellent in recycling value.

Such hydrolysis gas G is preferably recycled as an energy source for driving the aluminum black dross recycling system 1 according to the present invention. For example, as shown in FIG. 9, the aluminum black dross recycling system 1 may further include a combustion unit 120 combusting the hydrolysis gas G discharged from the gas storage unit 100. Can be. As illustrated in FIG. 9, the combustion unit 120 may receive the gas storage unit 100 by the gas supply line 130 to receive the hydrolysis gas G supplied from the gas storage unit 100. It can be connected with.

As described above, the hydrolysis gas G mainly includes methane gas and hydrogen gas. In general, hydrogen gas is more difficult to meet combustion conditions than methane gas. Therefore, the combustion unit 120 is preferably composed of a burner provided to combust hydrogen gas, but is not limited thereto. The combustion unit 120 is preferably installed so as to preheat the aluminum scrap A supplied to the raw material supply unit 25 of the aluminum melting furnace 1 using the heat of combustion of the hydrolysis gas G. It is not limited to this. Thus preheating the aluminum scrap (A) using the combustion unit 120, it is possible to reduce the cost required to preheat the aluminum scrap (A) using a separate heat source.

On the other hand, the black dross recycling apparatus 3 is preferably to process the above-described spherical black dross (B ₂ ) to be recyclable, but is not limited thereto. That is, the black dross recycling processing apparatus 1 may process the general black dross formed in a different manner from the spherical black dross B ₂ so as to be recyclable.

FIG. 19 is a flowchart schematically showing a method for dissolving aluminum and dross recycling according to another preferred embodiment of the present invention, and FIG. 20 is a detailed view of the aluminum dissolving step and the step of crushing and crushing spherical black dross described in FIG. 19. 21 is a flowchart for explaining the contents, and FIG. 21 is a flowchart for explaining details of the dross powder water decomposition step and the water decomposition product recycling step described in FIG. 19.

Referring to FIG. 19, according to a preferred embodiment of the present invention, the aluminum melting and dross recycling method includes dissolving aluminum (S 100) and crushing spherical black dross (B ₂ ) generated when dissolving aluminum. And pulverizing (S 200), decomposing the dross fine powder (P ₂ ) formed by crushing and crushing the spherical black dross (B ₂ ) (S 300), and dross fine powder (P _2). (S 400) treating at least one of the water decomposition products of) to be recyclable.

First, the step of dissolving aluminum (S 100), as shown in Figure 20, the step of forming a vortex (V) in the aluminum molten metal (M) (S 110) and melting on the surface of the aluminum molten metal (M) Injecting the flux (F) into the vortex (V) to form a flux layer (S 120), Injecting aluminum scrap (A) into the vortex (V) to pass through the molten flux layer (S 130), Recovering the aluminum molten metal (M) in which the aluminum scrap (A) is dissolved and the spherical black dross (B ₂ ) generated when the aluminum scrap (A) is dissolved in the aluminum molten metal (M) (S 140). .

Step (S 110) of forming the vortex (V) in the aluminum molten metal (M), by stirring the aluminum molten metal (M) using the above-described vortex unit 21 that can be rotationally driven, and turning down to the aluminum molten metal (M) This can be done by forming the vortex V.

The step S 120 of injecting the flux F into the vortex V may be performed by introducing a predetermined flux F into the vortex V of the aluminum molten metal M formed in the step S 110. Preferably, the flux (F) may include 93-97 parts by weight of a mixture of sodium chloride (NaCl) and potassium chloride (KCl) in the same parts by weight and 3-7 parts by weight of cryolite (Cryolite, Potassium Cryolite). More preferably, the flux (F) may include 47.5 parts by weight of sodium chloride (NaCl), 47.5 parts by weight of potassium chloride (KCl) and 5 parts by weight of potassium aluminum fluoride (KAlF ₄ ). When the flux F is introduced into the vortex V, a molten flux layer formed by dissolving the flux F is formed on the surface of the aluminum molten metal M, that is, a salt bath layer.

Injecting the aluminum scrap (A) into the vortex (V) (S 130), the predetermined aluminum scrap (A) to the vortex (V) of the aluminum molten metal (M) to pass through the melt flux layer formed in step S 120 Can be done by input. Preferably, the aluminum scrap (A) may be aluminum waste can scrap (UBCs, A 3XXX series, A 5XXXX series) mainly containing aluminum, magnesium and aluminum alloy. The aluminum scrap A injected into the vortex V melt | dissolves in the aluminum molten metal M. As shown to FIG. The same time, the aluminum molten metal that is inclusion molten flux layer containing the (M), the flux (F) are trapped in the formed black dross (B _1), these black dross (B ₁₎ a vortex (V) By repeatedly lowering and floating in the molten aluminum (M) to form a spherical black dross (B ₂ ) in which the black dross (B ₁ ) is spherical.

Recovering the aluminum molten metal (M) and the spherical black dross (B ₂ ) (S 140), the aluminum molten metal (M) in which the aluminum scrap (A) is dissolved through the hot water outlet of the aluminum melting furnace (2) described above. Along with the discharge box, the spherical black dross B ₂ suspended on the surface of the aluminum molten metal M may be carried out from the aluminum molten metal M using the above-described separation unit 27.

Next, the spherical black dross (B ₂₎ the step of grinding and crushing (S 200), the method comprising crushing the spherical black dross (B ₂₎ recovered from the aluminum molten metal (M) (S 210), and aluminum Separating the granules (N) and the dross powder (P ₁ ) (S 220), pulverizing the dross powder (P ₁ ) (S 230), aluminum granules (N) and dross particulate powder ( P ₂ ) is separated (S 240).

Step of crushing the spherical black dross (B ₂₎ (S 210) is a rectangular black dross (B ₂₎ a number of times in step S 140 may be carried out by crushing using the above-described crusher (41).

Separating the aluminum grains (N) and the dross powder (P ₁ ) (S 220), the aluminum grains (N) and dross powder (P) among the crushed products of the spherical black dross (B ₂ ) formed in step S 210. ₁ ) may be performed by using the first separation member 42 described above. For example, the first separating member 42 may be composed of a vibrating screen having a particle size of about 10 mm.

Grinding the dross powder (P ₁ ) (S 230), in step S 220 may be performed by grinding the dross powder (P ₁ ) separated from the aluminum grain (N) using a grinder 43.

Separating the aluminum grains (N) and the dross fine particle powder (P ₂ ) (S 240), the aluminum grains (N) and dross fine particle powder in the pulverized product of the dross powder (P ₁ ) formed in step S230. (P ₂ ) may be performed by using the second separation member 44 described above. For example, the second separating member 44 may be composed of a Trommel Screen having a particle size of about 0.5 mm.

On the other hand, the step of crushing and crushing the spherical black dross (B ₂ ) (200), aluminum granules separated from the dross powder (P ₁ ) and dross fine powder (P ₂ ) in step S 220 and S 240 step. (N) may further include the step (S 250). For example, the recycling step S 250 of the aluminum grains N may be performed by adding the aluminum grains N to the vortex V of the molten aluminum M described above.

Next, the dross particles decomposing the powder (P ₂₎ water (S 300), the use of aluminum grains (N) and re-separating the dross fine powder (P ₂₎ of the reactor 51 in the S 240 step It can be carried out by water decomposition. Preferably, the reactor 51 may agitate the dross fine particle powder P ₂ and water W1 mixed in a 1: 2 ratio to water-decompose the dross fine particle powder P ₂ . In this way dross particles if the degradation of powder (P ₂₎ water, de los particulate powder (P ₂₎ is the water decomposition products including a hydrolysis gas (G), soluble solids content (S) and insoluble solids (I) Decompose to

Next, the step (S 400) of treating at least one of the water decomposition products of the dross fine particle powder (P ₂ ) to be recycled, as shown in Figure 21, to treat the hydrolyzed gas (G) to be recyclable The step (S 410) and the step of separating the aqueous solution (Q) and insoluble solid (I) generated by dissolving the soluble solids (S) in water (W1) from each other (S 420), and the soluble solids (S) Processing (S 430) to be recyclable and processing (S 440) to process insoluble solids (I) to be recyclable.

In operation S 410, the hydrolysis gas G may be treated to be recyclable, as illustrated in FIG. 21, in operation S 411 of removing water and impurities included in the hydrolysis gas G, and moisture. And separating and purifying the hydrolyzed gas G from which impurities are removed (S 412), and storing the separated and purified hydrolyzed gas G (S 413).

Removing the water and impurities contained in the hydrolysis gas (G) (S 411), the trap unit 52 and the aforementioned water and impurities contained in the hydrolysis gas (G) discharged from the reactor 54 and The condenser 53 may be used to remove the condenser.

Separation and purification of the hydrolysis gas (G) (S 412), to increase the purity of the gas that can actually be recycled in the hydrolysis gas (G) from which water is removed in step S 411 or to recycle the gas in the gas decomposition gas (G) The hydrolysis gas G may be separated and purified by using the above-described gas separation purifier 54 so that a specific gas corresponding to the gas may be separated from other gases.

The storing of the hydrolysis gas G (S 413) may be performed by storing the hydrolysis gas G separated and purified at step S 412 in the gas storage unit 100 described above.

Separating the insoluble solids (I) and the aqueous solution (Q) from each other (S 420), as shown in Figure 21, the step of centrifuging the aqueous solution (Q) and insoluble solids (I) (S 421), The step of washing the insoluble solid (I) with distilled water (S 422), and the step of centrifuging the insoluble solid (I) and distilled water (S 423).

Centrifuging the insoluble solids (I) and the aqueous solution (Q) (S 421), the first centrifugation of the insoluble solids (I) and the aqueous solution (Q) separated from the hydrolysis gas (G) in step S410 It can be carried out by centrifugation using the separator (55).

Washing the insoluble solids (I) with distilled water (S 422), by washing the insoluble solids (I) with distilled water so that the chlorine adsorbed to the insoluble solids (I) in step S 421 is separated from the insoluble solids (I) Can be done. Although the insoluble solids (I) and the aqueous solution (Q) are centrifuged in step S 421, some of the aqueous solutions (Q) may remain adsorbed on the insoluble solids (I), and such aqueous solutions (Q) may include chloride salts. Soluble solids (S) are dissolved. Therefore, insoluble solids (I) are washed with distilled water so as to remove the chloride salt adsorbed on the insoluble solids (I). The step (S 422) of washing the insoluble solids (I) with distilled water is preferably performed using distilled water (D) generated in step S445 to be described later, but is not limited thereto.

Centrifuging the insoluble solid (I) and distilled water (S 423), after step S 422, is performed by centrifuging the insoluble solid (I) and distilled water (D) using the first centrifuge (55) described above. can do.

Additionally, steps S 422 and S 423 may be repeatedly performed until the concentration of the chloride salt adsorbed on the insoluble solids (I) is equal to or less than a predetermined reference concentration. The reference concentration is preferably about 300 ppm, but is not limited thereto.

In step (S 430) of treating the soluble solids (S) to be recyclable, the aqueous solution (Q) is distilled under reduced pressure under a predetermined temperature and pressure, as shown in FIG. 21, and the soluble solids (S) from the aqueous solution (Q). ) (S 431), centrifuging the soluble solids (S) and the aqueous solution (Q ₁ ) (S 432), drying the soluble solids (S) (S 433), and soluble solids (S ₁ 434) is stored.

Aqueous distillation of the aqueous solution (Q) under reduced pressure (S 431), in step S 421, the insoluble solid (I) and centrifuged aqueous solution (Q) using the above-described reduced pressure distillation unit 62. It may be carried out by distillation under reduced pressure under a predetermined reduced pressure distillation temperature and a reduced pressure distillation pressure. The vacuum distillation temperature is 40 ℃ ℃ to 70 ℃ ℃, the vacuum distillation pressure is preferably 12 kPa to 40 kPa, but is not limited thereto.

Centrifuging the soluble solids (S) and the aqueous solution (Q ₁ ) (S 432), the soluble solids (S) and soluble solids (S) precipitated from the aqueous solution (Q) in step S 431 is precipitated and the remaining aqueous solution ( Q ₁ ) may be performed by centrifugation using the second centrifuge 66 described above.

Drying the soluble solids (S) (S 433) may be carried out by drying the soluble solids (S) centrifuged with the aqueous solution (Q ₁ ) in step S 432 using the above-described soluble solids dryer (72). . Drying the soluble solids (S) (S 433) is preferably performed until the soluble solids (S) contains less than 0.3% water, but is not limited thereto.

The storing of the soluble solids S ₁ (S 434) may be performed by storing the soluble solids S ₁ dried in the step S 433 in the soluble solids storage chamber 74 described above.

In addition, the step (S 430) of treating the soluble solids (S) to be recyclable may include condensing water vapor (T) generated when the aqueous solution (Q) is distilled under reduced pressure in step S 431 to generate distilled water (D). It may further include (S 435). Generating the distilled water (S) (S 435) may be carried out by condensing the water vapor (T) generated in step S431 using the condenser 64 described above. The distilled water (D) generated in the step (S 435) of producing such distilled water (D) can be used when washing the insoluble solids (I) is transferred to the first centrifuge (55) described above in step S422. .

In addition, the step of distilling the aqueous solution (Q) under reduced pressure to precipitate the soluble solids (S) (S 430), the insoluble solids (I) and the centrifuged aqueous solution (Q) in step S 421 and the soluble solids ( S) and centrifuged aqueous solution (Q ₁ ) may be carried out by distillation under reduced pressure. That is, the aqueous solution of soluble solid material passing into this aqueous solution under reduced pressure distiller 62, the above-mentioned the (Q ₁₎ for recycling to deposit (S) (S 436) dissolved in the (Q ₁₎ for performing re-distilled under reduced pressure will be.

Treatment of the insoluble solid (I) to be recyclable (S 440), as shown in Figure 21, the step of drying the insoluble solid (I) (S 441), and the insoluble solid (I ₁ ) A step S442 and a step S443 of storing insoluble solids I ₂ are included.

Drying the insoluble solid (I) (S 441), the water adsorbed to the insoluble solid (I) without being separated from the insoluble solid (I) in step S 420 is dried using the above-described insoluble solid dryer (92) Can be performed. Drying the insoluble solid (I) (S 441), when recycling the insoluble solid (I) to the cement raw material is preferably performed until the insoluble solid (I) contains 40% or less moisture. In addition, the step of drying the insoluble solids (I) (S 441) is carried out until the insoluble solids (I) contains less than 0.5% water when the insoluble solids (I) are recycled into brick refractory or ceramic material. Preferably, but not limited to.

The step of firing the insoluble solid (I ₁ ) (S 442) may be performed by firing the insoluble solid (I ₁ ) dried in step S 441 using the insoluble solid firing furnace 94 described above. Insoluble solids (I ₁ ) may include hydroxides such as aluminum hydroxide, magnesium hydroxide and aluminum alloy hydrates having unstable properties such that these hydroxides are transferred to aluminum oxide, magnesium oxide, aluminum alloy oxides having relatively stable properties. The insoluble solid content (I ₁ ) is fired.

The storing of the insoluble solid (I ₂ ) (S 443) may be performed by storing the insoluble solid (I ₂ ) fired in step S 442 in the insoluble solid storage chamber 96 described above.

Although the present invention has been described above by means of limited embodiments and drawings, the present invention is not limited thereto and will be described by the person skilled in the art to which the present invention pertains. Of course, various modifications and variations are possible within the scope of the claims.

1: aluminum melting and black dross recycling system
2: aluminum melting furnace
3: black dross recycling unit
10: heating chamber
20: melting chamber
30: flow force giving room
40: split unit
50: water decomposition unit
60: precipitation unit
70: soluble solids storage unit
80: Aluminum Granules Storage Unit
90: insoluble solids storage unit
100: gas storage unit
M: molten aluminum
V: Vortex
A: Aluminum Scrap
F: flux
B ₁ : Black Dross
B ₂ : spherical black dross
P1: Dross Powder
P2: Dross Particulate Powder
N: Aluminum Grain
S, S ₁ : Soluble solids
I, I ₁ , I ₂ : insoluble solids
Q, Q ₁ : aqueous solution
G: hydrolysis gas
T: water vapor
D: distilled water

Claims (18)

In the aluminum black dross recycling system for recycling the black dross generated when dissolving aluminum scrap in the fluxed aluminum molten metal,
A dividing unit for dividing the black dross into aluminum grains and dross particulate powder; And
Reacting the dross fine particle powder with water to divide into a soluble solid solution, insoluble solids and hydrolysis gas, and the water and impurities contained in the hydrolysis gas by passing the hydrolysis gas discharged from the reactor through water A trap for collecting the gas, a condenser for cooling the hydrolysis gas discharged from the trap and condensing water vapor contained in the hydrolysis gas, and the hydrolysis gas separated from the water contained in the trap is transferred to the condenser. And a water cracking unit having a trap-condenser connecting line connecting said trap and said condenser to be delivered. The method of claim 1,
The aluminum scrap comprises at least aluminum waste can scrap,
The flux is aluminum black, characterized in that it comprises 93-97 parts by weight of a mixture of sodium chloride (NaCl) and potassium chloride (KCl) in the same weight parts and 3-7 parts by weight of cryolite (Cryolite, Potassium Cryolite) Ross Recycling System. The method of claim 1,
The dividing unit, the black dross is crushed and pulverized, the aluminum black dross recycling system, characterized in that divided into the aluminum grain and the dross fine powder. The method of claim 1,
The water decomposition unit further comprises a reactor-trap linking line connecting the reactor and the trap such that the hydrolysis gas separated from the water contained in the reactor passes through the water contained in the trap. Aluminum black dross recycling system. The method of claim 4, wherein
The reactor-trap trapping line has an extension provided to be immersed in the water contained in the trapper by a predetermined depth, and an outlet for discharging the hydrolyzed gas passing through the extension to the water contained in the trap. Features aluminum black dross recycling system. The method of claim 5,
And the discharge portion has at least one injection hole perforated to inject the hydrolysis gas passing through the extension portion into the water contained in the trap. The method of claim 1,
The trap machine comprises a plurality of separator plates each having at least one guide hole perforated to guide the hydrolysis gas released from the water contained in the trap to the condenser. . The method of claim 7, wherein
The separation plate, the aluminum black dross recycling system, characterized in that arranged in such a way that the guide holes provided in each of the separation plate alternately. delete The method of claim 1,
The water decomposition unit is connected to each of the trap and the condenser so that the condensed water formed by condensation of the water and the water vapor contained in the trap is introduced, and a negative pressure generated by cooling the hydrolysis gas is transmitted. An aluminum black dross recycling system, further comprising a gas pressure compensation line. The method of claim 10,
And said gas pressure compensation line has a mixed water chamber configured to receive at least a portion of the mixed water mixed with said water and said condensate. The method of claim 11,
The mixed water chamber, the aluminum black dross recycling system, characterized in that it has an observation window formed to observe the level change of the mixed water. The method of claim 11,
The gas pressure compensation line may include a first open / close valve installed between the trap and the mixed water chamber to selectively communicate the trap and the mixed water chamber, and the condenser and the mixed water chamber to selectively communicate with each other. And a second open / close valve installed between the condenser and the mixed water chamber. The method of claim 13,
The gas pressure compensation line, the aluminum black dross recycling system characterized in that it has a drain valve provided to selectively discharge the mixed water mixed with the water and the condensed water to the outside. The method of claim 13,
The gas pressure compensating line has a first inlet connected to the trap so that the water is introduced by water pressure, and a second inlet connected to the condenser so that the condensate is introduced by gravity. . The method of claim 1,
And a combustion unit for combusting the hydrolysis gas discharged from the condenser. The method of claim 16,
Further comprising a gas storage unit for storing the hydrolysis gas discharged from the condenser,
And said combustion unit combusts said hydrolysis gas discharged from said gas storage unit. The method of claim 17,
The combustion unit, the aluminum black dross recycling system, characterized in that the aluminum scrap is provided to be preheatable using the heat of combustion of the hydrolysis gas.

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