JPWO2011007655A1 - Apparatus and method for condensing liquefaction of zinc chloride - Google Patents

Abstract

[Problem] To recover zinc chloride efficiently and continuously for a long time from a gas containing zinc chloride as a main component as a by-product from a process of producing high-purity silicon by reducing silicon tetrachloride with zinc An apparatus and method are provided. [Solution] A condensing and liquefying apparatus according to the present invention includes an introduction portion for introducing a gas, a first mixing weir and a second weir, an inclined mixing portion for storing refrigerant liquid, and connected to the mixing portion. In addition, a heat exchanging unit that removes heat from the refrigerant liquid, an exhaust unit to which a suction exhaust device is connected, and a liquid extracting unit that is provided in the mixing unit and the heat exchanging unit are provided. The condensate liquefaction method of the present invention is characterized by liquefying a condensed component containing zinc chloride from a gas containing zinc chloride and collecting it in a refrigerant liquid.

Description

  The present invention relates to an apparatus and a method for recovering zinc chloride from a gas containing zinc chloride as a main component, which is generated from a step of producing high-purity silicon by reducing silicon tetrachloride with zinc.

  In recent years, interest in solar cells as an effective means for preventing global warming has increased. Silicon-based, compound-based, and organic solar cells have been studied, and silicon-based solar cells are most practically used. In particular, power generation facilities using single-crystal or polycrystalline silicon solar cells made from high-purity silicon have dramatically increased the number of installations from small to large scale, which can reduce power generation costs. If so, the increasing trend is expected to accelerate.

  The supply capacity of high-purity silicon is insufficient for these demands due to the rapid increase in demand for solar cells in recent years, in addition to the demand for semiconductors used in electronic equipment and information equipment. The situation cannot be met. In particular, high-purity silicon may be preferentially supplied to semiconductors. For high-purity silicon used as a raw material for solar cells, the residual crucible after pulling up single-crystal silicon for semiconductors and single-crystal silicon ingots For example, scrap materials such as cutting scraps are used forcibly using materials that vary in quality. For this reason, there is a strong demand for the realization of a stable supply system for high-purity silicon for solar cells, both in terms of quality and quantity, and the development of technology that can be manufactured in large quantities at a lower cost.

  At present, the production of high-purity silicon that is carried out commercially is carried out by the Siemens method. In this method, the power cost occupying the manufacturing cost is large, and the production efficiency is low because batch manufacturing is performed. Furthermore, recovery of unreacted trichlorosilane and hydrogen and by-product silicon tetrachloride are recovered and processed from the cracked gas emitted from the production of high-purity silicon by the Siemens method and the production of trichlorosilane used as a raw material Ancillary facilities must be strengthened. Considering these, the Siemens method is not suitable as a method for producing high-purity silicon in large quantities at a low cost.

  Various methods for producing high-purity silicon at low cost in place of the Siemens method have been studied. Among them, the zinc reduction method for reducing silicon tetrachloride with zinc has the possibility of producing high-purity silicon at low cost. It is attracting attention as. This reduction reaction is performed according to the reaction formula shown in the following formula (1).

SiCl ₄ + 2Zn → Si + 2ZnCl ₂ (1)
However, this method of reducing silicon tetrachloride with zinc requires about 6.1 kg of silicon tetrachloride and about 4.6 kg of zinc in order to obtain 1 kg of high-purity silicon, and about 9.7 kg of zinc chloride. It is a living reaction. Effective utilization of by-product zinc chloride is a major problem that must be solved in order to provide high-purity silicon at low cost by the zinc reduction method.

  As a method of using zinc for the reduction reaction of silicon tetrachloride, for example, Patent Document 1 (Japanese Patent Laid-Open No. 11-11925) discloses a method in which liquid or gaseous silicon tetrachloride is introduced into a molten zinc solution for reduction. Patent Document 2 (Japanese Patent Laid-Open No. 2007-284259) discloses a method in which liquid aluminum or zinc is brought into contact with silicon tetrachloride gas as fine particles, and Patent Document 3 (Japanese Patent Laid-Open No. 2008-037735). Discloses a method in which reaction conditions for various zinc reductions are changed, such as a method in which silicon tetrachloride is injected into a mixed gas of zinc and zinc chloride as a liquid.

  Patent Document 4 (Japanese Patent Application Laid-Open No. 2007-126342) discloses a method in which a reaction gas containing silicon produced by zinc reduction is made to collide with a silicon dissolution wall heated to a melting point of silicon or more and taken out as liquid silicon, Patent Document 5 (Japanese Patent Application Laid-Open No. 2007-223822) discloses a method for producing high-purity silicon such as a method in which high-purity silicon produced by zinc reduction is grown downward from the tip of a silicon tetrachloride supply nozzle in a reaction apparatus. It is disclosed.

  In Patent Document 6 (Japanese Patent Laid-Open No. 2003-034519), high purity silicon tetrachloride and vaporized metallic zinc are brought into gas / gas contact in a reactor at 900 ° C. to 1100 ° C. to obtain high purity silicon. In the gas phase zinc reduction process to be produced, by-product zinc chloride is separated and recovered by electrolysis as chlorine gas and high-purity metal electrolytic zinc. Chlorine gas is reacted with metal silicon as the main raw material after purification, and further refined. There is shown a method for producing high-purity silicon characterized in that it is highly purified by distillation to form silicon tetrachloride, and electrolytic zinc is used as a reducing agent that reacts with silicon tetrachloride. According to this method, by recycling zinc chloride produced as a by-product, waste to the outside of the system can be basically eliminated as a total system, and quality can be stabilized at low cost from metallic silicon as a raw material. It is said that high-purity silicon for solar cells can be produced.

Non-Patent Document 1 (Seifelt DA and Browning MF, “Pilot-Scale Development of the Zinc Reduction for Production of High-Purity Silicon” AIChE Symposium Series (American Institute of Chemical Engineers) No. 216, Vol. 78, p104- 115 (1982) discloses a method for producing high-purity silicon in which silicon tetrachloride is reduced with zinc gas in a fluidized bed and grown on the seed silicon charged with the produced silicon. In this method, by-product zinc chloride gas, unreacted zinc gas and unreacted silicon tetrachloride gas are continuously withdrawn from the upper part of the fluidized bed reactor, and zinc chloride and zinc are captured as a mixed liquid by a condenser. The collected and collected mixed liquid is sent to a molten salt electrolyzer and electrolyzed to recover chlorine and zinc. The recovered zinc is used for the reduction of silicon tetrachloride, and the recovered chlorine is used for the production of silicon tetrachloride using silicic acid (SiO ₂ ) and carbon or metal silicon as raw materials. In addition, a pilot production device that produces 50 tons / year using a zinc reduction method that includes a high-purity silicon production process and a recycling process for by-produced zinc chloride was designed. Production is possible at the lowest cost.

  Furthermore, according to Non-Patent Document 1, when silicon tetrachloride gas is reduced with zinc gas at a reaction temperature of 890 ° C., the conversion rate from silicon tetrachloride gas to silicon is 67%, which is obtained by thermodynamic calculation. A value of 94% of the equilibrium reaction coefficient obtained is obtained. This is because, in addition to zinc chloride by-produced from the reactor, nearly 30% of the introduced amount of unreacted silicon tetrachloride gas and unreacted zinc gas, and dust that could not be recovered in the reactor. A mixed gas containing silicon and an inert gas introduced as necessary is discharged. As an apparatus for recovering zinc chloride and unreacted zinc gas as a mixed liquid from this exhaust gas, Non-Patent Document 1 discloses that the refrigerant flows through the opposite side of the contact surface with the exhaust gas, and the temperature of the contact surface is adjusted by heat transfer. An apparatus using a lowering indirect cooling scheme is shown.

  However, in this method, since there is a limit to the heat transfer determined by the thermal conductivity of the material constituting the contact surface, and the contact area with the gas cannot be essentially secured, zinc chloride is included. Zinc chloride etc. cannot be efficiently recovered from the exhaust gas.

  Zinc chloride gas becomes a liquid at a boiling point of 732 ° C. or lower, increases in viscosity as the temperature is lowered, and becomes a solid at a melting point of 283 ° C. or lower. Zinc gas becomes a liquid at a boiling point of 907 ° C. or lower, the viscosity increases near a melting point of 419 ° C., and becomes a solid at a temperature lower than the melting point. In the recovery of zinc chloride and zinc by the indirect cooling method, it is necessary to lower the temperature of the refrigerant liquid to a temperature well below the boiling point of zinc chloride in order to increase the recovery rate. There is a problem that it is difficult to operate stably for a long period of time.

  Furthermore, in this method, the silicon dust is condensed and recovered in a state where silicon dust is dispersed and mixed in the liquid in which zinc chloride and zinc are mixed. If zinc chloride recovered by this method is used as it is for electrolysis, it causes deterioration of electrolysis efficiency, and in extreme cases, electrolysis becomes impossible. In order to use the recovered zinc chloride as a raw material for electrolysis, it is necessary to perform a process such as a method of filtering as a melt, a method of separating by distillation, or a method of reacting with chlorine gas. Becomes complicated.

  Zinc chloride exhibits a strong hygroscopicity in solids and easily absorbs moisture from the atmosphere. When performing molten salt electrolysis of zinc chloride containing water, the electrolysis voltage of water is lower than the electrolysis voltage of zinc chloride, so water begins electrolysis first. Mixing moisture not only wastes power, but the mixed gas of hydrogen and chlorine generated by electrolysis can react explosively, and this is a method that can control moisture contamination for safety reasons. It will be necessary. If the condensed zinc chloride can be handled in the form of a melt, there is no concern about the mixing of moisture. Therefore, establishment of a method for recovering zinc chloride in the melt and passing it to the subsequent molten salt electrolysis is strongly demanded.

  Various methods described above have been studied for the purpose of obtaining high-purity silicon by reducing silicon tetrachloride with zinc. In any case, regarding the method for condensing and liquefying exhaust gas containing by-product zinc chloride, It does not disclose or suggest a way to solve these inherent problems. There is still a strong demand to establish a method for efficiently recovering zinc chloride and zinc from exhaust gas containing zinc chloride, leading to the subsequent electrolysis process, and enabling a method for recovering and recycling chlorine and zinc. Yes.

  The method of cooling the gas and recovering it as a condensed liquid is a technique commonly practiced in the chemical industry. Condensation methods include an indirect cooling method and a direct cooling method. However, in many chemical devices, the gas to be condensed is separated by a refrigerant liquid and a partition wall and cooled indirectly from the outside of the partition wall, and the condensed liquid and the refrigerant liquid are mixed. There is often no indirect cooling method. The direct cooling method is a method in which the latent heat is directly transferred between the condensed liquid and the refrigerant liquid, so that the speed of heat transfer is fast, but the gas to be introduced is in direct contact with the refrigerant liquid. Use is limited.

  As a few examples using the direct cooling method, for example, Patent Document 7 (US Pat. No. 2,766,114) discloses a method and apparatus for condensing metal from metal vapor, specifically, reducing zinc oxide with carbon. A method and apparatus for condensing and recovering zinc from zinc vapor is disclosed. This method is a method in which liquid zinc is placed in a sloping restricted pipe, a gas containing zinc vapor is passed through the liquid zinc, and the zinc vapor in contact with the moving surface of the liquid zinc is condensed. At the same time, using a lift created by the upward movement of liquid zinc generated by the gas flow, a device that draws a part of the liquid zinc from the restricted pipe line, cools it in an external cooling tank, and returns the part. This method is used. According to this method, it is said that zinc is efficiently and continuously condensed.

  However, Patent Document 7 discloses whether or not zinc chloride can be condensed and collected from a gas containing zinc chloride having physical properties such as vapor pressure and viscosity different from zinc by the above method, or tetrachloride. Zinc chloride from a gas that contains zinc chloride discharged as a main component of silicon and contains multiple components such as unreacted zinc gas and silicon tetrachloride gas that have different physical properties such as vapor pressure and viscosity. Nor does it disclose or suggest whether it is possible to condense. Whether or not this method can be used even in a gas containing zinc gas or silicon tetrachloride gas in addition to zinc chloride gas and whose thermodynamic equilibrium changes with temperature. Furthermore, it does not disclose or suggest whether it is possible to condense a plurality of components such as zinc chloride and zinc as the condensing components and collect them separately for each component.

JP 11-11925 A JP 2007-284259 A JP 2008-037735 A JP 2007-126342 A JP 2007-223822 A JP 2003-034519 A U.S. Pat. No. 2,766,114

Seifelt D.A. and Browning M.F., "Pilot-Scale Development of the Zinc Reduction for Production of High-Purity Silicon" AIChE Symposium Series (American Institute of Chemical Engineers) No.216, Vol.78, p104-115 (1982)

  The present invention recovers zinc chloride efficiently and stably over a long period of time from a gas containing zinc chloride as a main component as a by-product from the process of producing high-purity silicon by reducing silicon tetrachloride with zinc. It is an object of the present invention to provide an apparatus and a method.

  As a result of intensive studies to solve the above problems, the present inventors used a specific condensate liquefaction apparatus, and made a zinc chloride melt, a zinc melt or a melt in which both zinc chloride and zinc coexist as a refrigerant liquid, It has been found that the above problem can be solved by a method in which a condensed component containing zinc chloride is liquefied from a gas containing zinc chloride as a main component and collected in the refrigerant liquid, and the present invention has been completed based on this finding. It was. For example, the present invention has the following configuration.

  [1] (A) An introduction part for introducing gas, (B) an inclined mixing part that has a first weir and a second weir and stores refrigerant liquid, and (C) connected to the mixing part. In addition, a heat exchanging unit for removing heat from the refrigerant liquid, (D) an exhaust unit to which the suction exhaust device is connected, and (E) a liquid extracting unit for extracting the liquid provided in the mixing unit and the heat exchanging unit And a condensate liquefaction device.

  [2] The condensing and liquefying apparatus according to [1], wherein the mixing section is inclined within a range of 10 degrees to 35 degrees from a horizontal plane.

  [3] The condensing and liquefying apparatus according to any one of [1] to [2], wherein the liquid extraction part is provided on the exhaust part side of the mixing part.

  [4] The condensing and liquefying apparatus according to [3], wherein a third weir is provided in front of the liquid extraction part provided on the exhaust part side of the mixing part.

  [5] Using the condensing and liquefying apparatus according to any one of [1] to [4], a step of storing a refrigerant liquid inside the mixing unit and the heat exchange unit, and a gas containing zinc chloride from the introduction unit A condensate liquefaction method comprising a step of introducing, and a step of liquefying a condensing component containing zinc chloride from the introduced gas and collecting it in a refrigerant liquid.

  [6] Using the negative pressure of the exhaust section generated by the suction exhaust apparatus, the gas containing zinc chloride introduced from the introduction section is moved in the upper refrigerant liquid of the mixing section, and between the introduced gas and the refrigerant liquid. A process of performing heat exchange by direct gas-liquid contact, and after condensing the condensed component containing zinc chloride and collecting it in the refrigerant liquid, the refrigerant liquid is sent from the mixing section to the heat exchange section, and the refrigerant liquid is heat exchanged Removing the heat in the unit, returning the refrigerant liquid after heat removal to the mixing unit and circulating the refrigerant liquid; and extracting a part of the refrigerant liquid from the liquid extraction unit provided in the mixing unit or the heat exchange unit; And the step of exhausting the gas exhausted from the mixing part from the exhaust part.

  [7] The condensate liquefaction method according to [6], wherein the liquid extraction part provided in the mixing part is sealed with the extracted refrigerant liquid.

  [8] The refrigerant liquid in which the condensed component is collected forms two layers in a mixing part, a layer made of a refrigerant liquid having a small specific gravity and a layer made of a refrigerant liquid having a large specific gravity. ] The condensate liquefaction method in any one of [7].

  [9] The condensing and liquefying method according to [8], wherein the refrigerant liquid having a large specific gravity is sent from the mixing unit to the heat exchange unit to remove heat, and then returned to the mixing unit for circulation.

  [10] The mixing unit so that the outlet of the refrigerant liquid from the mixing unit to the heat exchange unit and the return port of the refrigerant liquid from the heat exchange unit to the mixing unit are opened in the layer composed of the refrigerant liquid having a large specific gravity. The condensation and liquefaction method according to any one of [8] to [9], wherein the condensation and liquefaction device provided in the apparatus is used.

  [11] The gas containing zinc chloride is a mixed gas containing zinc chloride and one or more gases selected from the group consisting of zinc and silicon tetrachloride, or an inert gas is further included in the mixed gas. It is a mixed gas, The condensate liquefaction method in any one of said [5]-[10] characterized by the above-mentioned.

  [12] The refrigerant liquid according to any one of [5] to [11], wherein the refrigerant liquid is a zinc chloride melt, a zinc melt, or a melt containing both zinc chloride and zinc. Condensed liquefaction method.

  [13] The refrigerant liquid extracted from the liquid extraction part provided in the mixing part is a zinc chloride melt or a mixed melt in which a zinc melt is mixed with a zinc chloride melt, and the heat exchange part Any of the above [6] to [12], wherein the refrigerant liquid extracted from the provided liquid extraction portion is a zinc melt or a mixed melt in which a zinc chloride melt is mixed with a zinc melt. The condensate liquefaction method described in 1.

  [14] The condensation liquefaction method according to any one of [5] to [13], wherein the gas containing zinc chloride is introduced in a temperature range of 800 ° C to 1100 ° C.

  [15] By controlling the circulation amount of the refrigerant liquid circulating through the mixing unit and the heat exchange unit and the heat removal amount of the heat exchange unit, the temperature of the refrigerant liquid returning to the mixing unit is maintained in the range of 420 ° C to 650 ° C, And the temperature of the exhaust gas discharged | emitted from an exhaust part to a suction exhaust apparatus is maintained at 700 degrees C or less, The condensation liquefaction method in any one of said [6]-[14] characterized by the above-mentioned.

  [16] The liquid extracted from the liquid extraction part provided in the mixing part is a mixed melt in which dust-like silicon is further mixed in a zinc chloride melt or a mixed melt in which a zinc melt is mixed in a zinc chloride melt. It is a liquid, The condensation liquefaction method in any one of said [6]-[15] characterized by the above-mentioned.

  [17] The above-mentioned [6], wherein the heat quantity of the refrigerant liquid removed by the heat exchange unit is a heat quantity corresponding to the sum of the latent heat of the condensed component and the heat quantity required for cooling the introduced gas. [16] The condensate liquefaction method according to any one of [16].

  By using the condensing liquefaction apparatus of the present invention from a gas containing zinc chloride as a main component, and using a zinc chloride melt, a zinc melt, or a melt containing both zinc chloride and zinc as a refrigerant liquid, Condensed components containing zinc are liquefied and collected stably without causing problems such as blockage of pipes even when operated for a long time with a high collection rate, high thermal efficiency, and high volumetric efficiency. can do.

  In addition, according to the apparatus and method of the present invention, the condensed component contains a zinc chloride melt, a mixed melt in which a zinc melt is mixed with a zinc chloride melt, or a dust-like silicon contained in the zinc chloride melt. And the melt melt mixed with the zinc melt or the zinc melt melt in the zinc melt can be separated and taken out in the condensing apparatus.

  In addition, the zinc chloride melt, the mixed melt in which zinc melt is mixed with the zinc chloride melt, or the melt containing dusty silicon in the zinc chloride melt, which is condensed and taken out by the apparatus and method of the present invention, It has a quality that allows molten salt electrolysis without performing a special treatment such as distillation or filtration, and can be directly supplied to the subsequent molten salt electrolysis process.

  Further, the zinc melt or the mixed melt obtained by mixing the zinc melt with the zinc melt is reduced by the apparatus and method of the present invention, and the oxidation of zinc is suppressed. By the simple treatment, it can be used for the reduction of silicon tetrachloride.

  Furthermore, by using the apparatus and method of the present invention, zinc chloride produced as a by-product is efficiently collected from the production process of high-purity silicon in which silicon tetrachloride is reduced with zinc, and chlorine and zinc are produced by molten salt electrolysis. The produced chlorine can be directly reacted with metallic silicon or used as a raw material for producing silicon tetrachloride via hydrogen chloride, and the produced zinc can be used as a reducing agent for silicon tetrachloride. It becomes possible to realize the recycling utilization of zinc, and it becomes possible to produce high purity silicon at a relatively low cost.

FIG. 1 is a schematic view of a mixing section of a condensing liquefaction apparatus according to the present invention. FIG. 2 is a schematic view of a heat exchange part of the condensing liquefaction apparatus according to the present invention. FIG. 3 is a schematic diagram showing the arrangement of the mixing section and the heat exchange section in the condensing liquefaction apparatus according to the present invention. FIG. 4 is a schematic view in which a third weir is installed in the mixing section shown in FIG. FIG. 5 is a schematic diagram of a condensate liquefaction test apparatus.

  Hereinafter, the present invention will be described in more detail, but the present invention is not limited thereto.

  The condensing and liquefying apparatus of the present invention includes (A) an introduction portion for introducing gas, (B) an inclined mixing portion that has a first weir and a second weir and stores refrigerant liquid, and (C) the above-mentioned A heat exchanging unit connected to the mixing unit for removing heat from the refrigerant liquid; (D) an exhaust unit connected to the suction exhaust device; and (E) a liquid provided in the mixing unit and the heat exchanging unit. A liquid extraction part for extracting the liquid.

  FIG. 1 is a schematic view of a condensing and liquefying apparatus of the present invention used in a method for liquefying a condensed component containing zinc chloride from a gas containing zinc chloride as a main component and collecting it in a refrigerant liquid.

  The mixing unit 1 is inclined within a range of 10 degrees to 35 degrees from a horizontal plane, and has a first weir 5 and a second weir 6 therein. The inlet 3 side of the first weir 5 has a refrigerant liquid return port 8 that receives the refrigerant liquid from the heat exchanger 20 shown in FIG. 2, and the heat exchanger on the exhaust part 4 side of the second weir 6. 20 has a refrigerant liquid outlet 7 for sending out the refrigerant liquid. In addition, the mixing unit 1 includes a liquid extraction unit 15 that extracts a refrigerant liquid containing a condensed component. An upper gap 10, an upper gap 11, a lower gap 12, and a lower gap 13 are provided above and below the first weir 5 and the second weir 6. A zinc chloride gas discharge source A (not shown) such as a step of reducing silicon tetrachloride with zinc is connected to the introduction unit 3. A suction / exhaust device B (not shown) is connected to the exhaust unit 4, and the suction / exhaust device B is further equipped with ancillary equipment (not shown) for processing a non-condensable gas and a gas containing zinc chloride that could not be recovered. ). The introduction unit 3, the mixing unit 1, the exhaust unit 4, and the refrigerant liquid pipe circulating between the mixing unit 1 and the heat exchange unit 20 are surrounded by a heat insulating material or heated from the outside by a usual method. In other words, it is configured to be maintained within a predetermined operating temperature range.

  Collection of the condensed component containing zinc chloride from the gas containing zinc chloride is performed as follows. That is, the gas containing zinc chloride introduced from the introduction unit 3 is bubbled through the upper part of the refrigerant liquid stored in the inclined mixing unit 1 due to the negative pressure of the exhaust unit provided by the suction exhaust unit B. Or moving from the introduction unit 3 toward the exhaust unit 4 while spraying. At this time, the gas containing zinc chloride and the refrigerant liquid come into direct contact to exchange heat. The gas containing zinc chloride is rapidly cooled to near the temperature of the refrigerant liquid, the latent heat of the condensed component contained in the gas containing zinc chloride is taken away, and the condensed component containing zinc chloride is condensed and collected in the refrigerant liquid. .

  Attracted by the gaseous stream containing the introduced zinc chloride, the refrigerant liquid also produces a flow. This flow is emphasized by the first weir 5 and the second weir 6 installed in the mixing unit 1. A part of the flow passes through the upper gap 10 of the first weir 5, changes direction before the second weir 6, and circulates from the lower gap 12 of the first weir 5 to the introduction part side of the mixing unit 1. Form a flow. The other flow is further lifted further along the gas flow through the upper gap 11 of the second weir 6. Due to the flow lifted upward, a difference L in the storage height occurs between the refrigerant liquid on the exhaust portion 4 side of the second weir 6 and the refrigerant liquid on the introduction portion 3 side of the first weir 5. The difference L in the storage height becomes a driving force for circulating the refrigerant liquid between the mixing unit 1 and the heat exchange unit 20.

  The size and tilt angle of the mixing unit main body are determined by the degree of bubbles and spray, the gas-liquid contact time between the introduced gas and the refrigerant liquid, the circulation of the refrigerant liquid in the mixing unit 1 and the circulation with the heat exchange unit 20. Affect. For example, when a mixing unit having the same size is used, bubbles and sprays are gently generated at a low inclination angle inclined by 10 degrees from the horizontal plane, the gas-liquid contact time becomes long, and the circulation of the refrigerant liquid becomes gentle. At a high inclination angle inclined 35 degrees from the horizontal plane, bubbles and sprays are generated violently, and the gas-liquid contact time is shortened, but the circulation of the refrigerant liquid is strengthened. If the inclination angle of the mixing unit 1 is in the range of 10 to 35 degrees from the horizontal plane, it is preferable because both the degree of bubbles and spraying and the degree of gas-liquid contact time and the degree of circulation of the refrigerant liquid can be achieved. The inclination angle is more preferably in the range of 15 to 30 degrees. The length of the mixing unit main body is determined in consideration of the scattering distance of bubbles and spray generated in the mixing unit 1 to the exhaust unit 4 side. Since the size and inclination angle of the mixing unit main body and the size and position of each weir affect the difference L between the circulation of the refrigerant liquid and the storage height of the refrigerant liquid, the height of the weir, the position of the weir, and the position of the weir It is preferable to determine the tilt angle by performing an optimal adjustment by performing a test.

  FIG. 2 is a schematic view of a heat exchange part of a condensing and liquefying apparatus used in a method for liquefying and collecting a condensed component containing zinc chloride from a gas containing zinc chloride as a main component of the present invention. 2 includes a refrigerant liquid inlet 21 that receives the refrigerant liquid sent from the mixing unit 1 in FIG. 1, a refrigerant liquid outlet 22 that returns the heat-removed refrigerant liquid to the mixing unit 1, and heat removal from the refrigerant liquid. This is an example in which a heat removal device 23 that performs the above operation, a liquid extraction unit 24 that extracts the refrigerant liquid, and a liquid extraction unit 25 are provided. A refrigerant liquid whose temperature has risen is received from the refrigerant liquid inlet 21, and a heat quantity corresponding to the sum of the latent heat of the condensed component from the refrigerant liquid and the quantity of heat required for cooling the introduced gas is removed by the heat removal device 23, and the refrigerant liquid outlet The refrigerant liquid removed from the heat is returned to the mixing unit 1. The heat removal performed by the heat exchanging unit 20 can be performed by using a heat removal device 23 of an indirect cooling system that circulates a gas, a liquid, or a metal melt as the heat removal medium. The heat transfer area, the temperature and flow rate of the heat removal medium may be controlled to remove the necessary heat, and the capacity and structure of the heat exchanging unit 20 can ensure the necessary amount of heat transfer and storage of refrigerant liquid, The shape is not particularly limited as long as it does not hinder the circulation of the refrigerant liquid.

  When the refrigerant liquid that collects the condensed components contains a plurality of condensed components such as zinc chloride and zinc, and the condensed components do not melt together and can be separated by specific gravity, the mixing unit 1 and heat Separation of condensed components can also be performed by the exchange unit 20. The refrigerant liquid collected by condensing the condensed components immediately begins to separate by condensation and specific gravity for each condensed component within the mixing unit 1, and a condensed component having a small specific gravity is present in the upper part of the mixing unit 1 and a specific gravity is present in the lower part. Large condensed components gather, and the components having a large specific gravity become a refrigerant liquid that circulates between the heat exchanger 20. When sufficient separation is not completed inside the mixing unit 1, the refrigerant liquid can be sent from the mixing unit 1 to the heat exchange unit 20 and further separated by the heat exchange unit 20, and then returned to the mixing unit 1. In this case, the storage volume of the heat exchange unit 20 is increased to increase the residence time, and the condensed component having a small specific gravity is separated and stored in the upper part of the heat exchange unit 20 and the condensed component having a large specific gravity is separated and stored in the lower part. The separated condensed component is extracted from the liquid extraction unit 24 or the liquid extraction unit 25.

  As shown in FIG. 3, the mixing unit 1 and the heat exchange unit 20 are arranged. A pipe 27 and a pipe 28 are connected between the refrigerant liquid return port 8 and the refrigerant liquid outlet 22 and between the refrigerant liquid outlet 7 and the refrigerant liquid inlet 21, respectively. Thereby, the refrigerant liquid is circulated between the mixing unit 1 and the heat exchange unit 20. The refrigerant liquid outlet 7 and the refrigerant liquid return port 8 are preferably provided in the mixing unit 1 so as to open into a layer made of refrigerant liquid having a large specific gravity in the refrigerant liquid separated by the specific gravity described above.

  The cross-sectional shape of the mixing unit 1 can take a circular shape, an elliptical shape, a polygonal shape, or the like. In order to efficiently perform gas-liquid contact and liquid circulation performed in the mixing unit 1, the cross-sectional shape of the mixing unit may be an elliptical shape that becomes narrower from the upper part to the lower part, or from the introduction part 3 to the exhaust part 4 A shape with a changed cross-sectional area may be used. The shape of the heat exchanging unit 20 can be a cylindrical shape, a box shape, an ellipsoid, etc., as long as the configuration accepts the refrigerant liquid, removes a necessary amount of heat with a heat removal device, and can be returned to the mixing unit 1. It can take a shape and is not particularly limited.

  The material used for the condensing device is zinc chloride, zinc or silicon tetrachloride contained in a gas containing zinc chloride as a main component, or zinc chloride or zinc melt or mixed melt constituting the refrigerant liquid. Quartz, silicon carbide, or a ceramic material having resistance in the temperature range to be used can be used, and the inner surface of the outer iron material can be covered with these materials.

  A method for liquefying and collecting a condensed component containing zinc chloride from a gas containing zinc chloride as a main component by using the above-described condensing liquefaction apparatus of the present invention will be described in detail below. The physicochemical properties of zinc chloride and zinc are shown in Table 1 and Table 2, respectively.

  As shown in the following formula (1), 2 mol of zinc reacts with respect to 1 mol of silicon tetrachloride, and 1 mol of silicon is produced by a zinc reduction reaction in which silicon tetrachloride gas reacts with zinc gas. It is an exothermic reaction that produces silicon and 2 moles of zinc chloride.

SiCl ₄ + 2Zn → Si + 2ZnCl ₂ (1)
The equilibrium reaction coefficient of this reduction reaction obtained from thermodynamic calculation under a pressure of 1 atm was 62% at 1027 ° C, 72% at 927 ° C, 81% at 827 ° C, and below the boiling point of zinc chloride at 732 ° C. It is known that the value is 88% at 727 ° C. and 100% at 700 ° C. or less, and that the reaction coefficient increases when the temperature is lowered, and the equilibrium reaction coefficient decreases when a diluent gas such as argon gas is present. ing. From the equilibrium reaction coefficient, it is considered advantageous to carry out the reaction at a temperature of 700 ° C. or less and without a diluent gas, but when the reaction temperature is lowered, the reaction rate is drastically decreased and a long reaction time is required. The boiling point of zinc is 907 ° C., and it is difficult to continuously supply zinc as a gas at a temperature below the boiling point. When the reaction temperature is set to a low temperature below the boiling point, the zinc gas condenses, and the generated silicon contains zinc. The reaction is substantially carried out at 910 ° C. or higher and 1100 ° C. or lower because of incorporation.

  For example, the equilibrium reaction coefficient when reacting 1 mol of silicon tetrachloride gas and 2 mol of zinc gas at 900 ° C. and 1 atm is about 74%. In the reaction performed under these conditions, even if it is assumed that the reaction was ideally performed, the exhaust gas discharged from the reactor (zinc chloride gas emission source A) is 26% of unreacted silicon tetrachloride gas, The composition contains 26% of unreacted zinc gas and zinc chloride gas produced as a by-product. Further, a mixed gas containing an inert gas introduced as necessary is introduced into the condensing liquefaction apparatus. Even if the reduction reaction is performed under reaction conditions in which silicon tetrachloride gas is excessive with respect to zinc gas, or in contrast, reaction conditions in which zinc gas is excessive with respect to silicon tetrachloride, the exhaust gas discharged from the reactor is discharged. Although the gas contains zinc chloride as a main component and the ratio changes, it is not changed that it is a mixed gas containing zinc gas or silicon tetrachloride gas and further containing an inert gas introduced as necessary.

  Further, the exhaust gas discharged from the reaction apparatus may contain dusty silicon. Dust-like silicon is generated when the exhaust gas containing unreacted silicon tetrachloride and unreacted zinc gas discharged from the reactor is placed under conditions such that the temperature of the exhaust gas decreases. For example, when exhaust gas is transported through a pipe with a negative temperature gradient, or when zinc chloride is recovered using an indirect cooling method that gradually cools from the outside, unreacted zinc gas and unreacted under low temperature conditions In particular, it is often observed when the silicon tetrachloride gas coexists for a long time. As the exhaust gas temperature decreases, the thermodynamic equilibrium changes and it is thought that dusty silicon is produced. The exhaust gas discharged from the reaction apparatus is quickly sent to the condensing and liquefying apparatus without changing the temperature, and the exhaust gas containing zinc chloride is rapidly cooled to a temperature at which the reaction rate is low, and the zinc chloride is condensed and liquefied. The method of the present invention, which condenses liquefied unreacted zinc gas and quickly separates it from unreacted silicon tetrachloride gas, is also advantageous in reducing the production of dusty silicon.

  More specifically, the temperature of the gas containing zinc chloride to be introduced needs to be kept at a sufficiently high temperature not lower than the boiling point of zinc chloride of 732 ° C. until it is introduced into the condensing liquefaction apparatus, so as to prevent the zinc chloride from condensing. Yes. Moreover, even if it falls from reaction temperature, it is preferable to suppress a temperature change to about 100 degreeC. With such a temperature change, the change in thermodynamic equilibrium falls within a small range. Usually, the exhaust gas from the zinc reduction reaction apparatus in which the reaction is carried out at 900 ° C. or higher and 1100 ° C. or lower is kept in a liquefied state within the range of 800 ° C. or higher and 1100 ° C. or lower by keeping warm or heating from the surroundings as necessary It is preferably introduced into the apparatus. More preferably, it is introduced while maintaining a temperature equivalent to a temperature range of 910 ° C. or more and 1000 ° C. or less, which is a more preferable reaction temperature, and more preferably a temperature higher than the reaction temperature but not exceeding 1000 ° C.

  Prior to receiving the exhaust gas from the zinc chloride gas discharge source A, the refrigerant liquid in the melt state is stored in the mixing unit 1 and the heat exchanging unit 20 of the condensing liquefaction apparatus and is kept at a predetermined temperature. . The method is not particularly limited, but a method in which a refrigerant liquid previously melted or a powder or solid refrigerant liquid raw material is charged through a charging port or an inspection port provided in the mixing unit 1 or the heat exchanging unit 20 Then, it can be performed by a method of heating from the outside to obtain a melt. Thereby, inside the mixing part 1, the gas flow which flows from the introducing | transducing part 3 to the exhaust part 4 is interrupted | blocked by a refrigerant | coolant liquid, and it will be in the state which does not flow gas directly.

  When a zinc chloride melt is used as the refrigerant liquid before the start of the operation of the condensing liquefaction apparatus, it is maintained at a temperature at which the melting point of zinc chloride is not less than 283 ° C. and sufficiently lower than the boiling point of 732 ° C. and does not significantly evaporate zinc chloride. When a zinc melt is used as the refrigerant liquid before the start of operation, the temperature is kept at a melting point of 419 ° C. or higher and sufficiently lower than the boiling point of 732 ° C. of zinc chloride. Since the temperature of the refrigerant liquid suddenly increases when the introduction of the exhaust gas is started, it is preferable to start the operation with the refrigerant liquid at the start of operation at a temperature close to the lower limit of the temperature range. When the condensate liquefaction apparatus is operated, the refrigerant liquid condenses and takes in zinc chloride and zinc in the exhaust gas, and the composition of the refrigerant liquid gradually changes to a mixed melt of zinc chloride and zinc. That is, the refrigerant liquid when the condensing liquefaction apparatus is in a normal operation is a mixed melt of zinc chloride and zinc. When the condensing and liquefying apparatus is temporarily stopped or restarted in this state, the temperature of the refrigerant liquid is maintained at a temperature at which the melting point of zinc is not lower than 419 ° C. and the evaporation of zinc chloride is not significant.

  The suction / exhaust device B is moved to make the exhaust part 4 have a negative pressure. From the zinc chloride discharge source A, unreacted silicon tetrachloride, unreacted zinc gas, and by-product zinc chloride in a temperature range of 800 ° C. to 1100 ° C. Is introduced into the introduction part 3 of the condensing liquefaction apparatus. The liquid level on the introduction part 3 side of the refrigerant liquid is lowered, the liquid level on the exhaust part 4 side is raised, and the introduced gas generates bubbles and sprays in the refrigerant liquid near the upper part of the mixing part 1. Moving. At this time, the heat quantity of the gas rapidly moves to the refrigerant liquid, and the temperature of the gas rapidly decreases. As a result, unreacted zinc and by-produced zinc chloride are condensed and collected in the refrigerant liquid. The unreacted silicon tetrachloride gas as a non-condensed component and the inert gas introduced as necessary are cooled to a temperature close to that of the refrigerant liquid, and then separated from the refrigerant liquid and passed through the exhaust unit 4 to the suction exhaust apparatus B. Led. The refrigerant liquid receives the amount of heat required to cool the introduced gas and the amount of heat corresponding to the latent heat of condensation of zinc chloride and zinc, and the temperature rises.

  Liquid circulation between the mixing unit 1 and the heat exchanging unit 20 is started by the difference L in the storage height inside the mixing unit 1 caused by the introduced gas flow. The refrigerant liquid that has entered the heat exchanging unit 20 and whose temperature has risen is cooled by moving the heat removal device 23 and returned to the mixing unit 1. By adjusting the heat removal amount of the heat removal device 23 according to the exhaust amount of the suction exhaust device B, the temperature of the refrigerant liquid returning from the heat exchange unit 20 to the mixing unit 1 can be controlled.

  The temperature of the refrigerant liquid suitable for condensing the gas containing zinc chloride is preferably in the temperature range of 420 ° C. or higher and 650 ° C. or lower when the state becomes stable. A temperature of 650 ° C. or lower is preferable because both the zinc chloride gas and the unreacted zinc gas can be substantially condensed and liquefied. A temperature of 550 ° C. or lower is more preferable because the vapor pressure of zinc chloride is 10% or less of the saturated vapor pressure and 1% or less of zinc. A temperature of 520 ° C. or lower is particularly preferable because the vapor pressure of zinc chloride is 2% or lower of the saturated vapor pressure. Moreover, if it is the temperature of 420 degreeC or more, since zinc does not solidify, it is preferable. A temperature of 450 ° C. or higher is more preferable because the viscosity of zinc chloride is lowered and the fluidity is improved. As described above, if the refrigerant liquid returning from the heat exchanging unit 20 to the mixing unit 1 is in a temperature range of 420 ° C. or higher and 650 ° C. or lower, zinc chloride gas and zinc gas can be stably condensed and liquefied. In the temperature range of 450 ° C. or more and 520 ° C. or less, zinc chloride is close to 98% estimated from the vapor pressure, and zinc is close to 99% estimated from the vapor pressure and can be condensed and collected. Since it becomes possible, it is further preferable.

  After collecting condensed components from the introduced gas into the refrigerant liquid, silicon tetrachloride gas that does not condense at this temperature, or gas that contains zinc chloride or zinc that could not be collected is at a temperature close to the temperature range of the refrigerant liquid. Then, it is discharged from the mixing section 1 and exhausted to the suction exhaust apparatus B through the exhaust section 3. The suction exhaust apparatus B is connected to incidental equipment for separating and recovering silicon tetrachloride gas from this gas, or for treating zinc chloride, zinc, etc. that could not be collected. When the temperature of the gas discharged to the suction exhaust device B exceeds 700 ° C., the energy required for the separation and recovery of the silicon tetrachloride gas increases, and the amount of zinc chloride contained in the gas increases rapidly. Therefore, the load on incidental equipment for processing these increases, which is not preferable. The exhaust temperature is preferably maintained at a temperature of 700 ° C. or less by adjusting the heat removal amount of the heat removal device 23 according to the exhaust amount of the suction exhaust device B. In addition, the temperature difference between the refrigerant liquid temperature and the exhaust gas temperature is introduced within 50 ° C., that is, by changing the configuration such as the thickness, length, weir position, etc. of the mixing unit 1 and the inclination of the mixing unit 1. It is more preferable that the heat exchange of the gas is performed well.

  The refrigerant liquid that has taken in the condensed liquid component of zinc chloride and zinc causes separation of the condensed component due to the difference in specific gravity inside the mixing unit 1. In the zinc melt and the zinc chloride melt, the specific gravity of the zinc melt is twice or more larger and the zinc melt does not melt together. Is formed as an upper layer. The lower layer is a zinc melt or a mixed melt in which a zinc chloride melt is mixed with a zinc melt, and the upper layer is a mixed melt in which a zinc melt is mixed with a zinc chloride melt or a zinc chloride melt. A refrigerant liquid composed of this zinc melt or a mixed melt in which zinc chloride melt is mixed with the zinc melt is sent to the heat exchanging section 20 from the refrigerant liquid outlet 7 located in the lower layer thus formed, and the heat exchanging section. Heat is removed at 20 and returned to the mixing unit 1 from the refrigerant liquid return port 8 located in the lower layer. By continuously introducing gas from the introduction part 3, it is condensed and taken into the refrigerant liquid, and the increase in the zinc melt separated by specific gravity or the mixed melt in which zinc chloride melt is mixed in the zinc melt is The liquid is extracted from the liquid extraction unit 24 or the liquid extraction unit 25 provided in the heat exchange unit 20.

  The upper layer formed in the mixing unit 1 may be a layer containing dusty silicon that is generated without being suppressed. The zinc chloride melt, the mixed melt in which the zinc melt is mixed with the zinc chloride melt, or the increased amount of the mixed melt in which the dusty silicon is mixed with these are extracted from the liquid extraction portion 15 provided in the mixing portion 1. Continuously extracted. The liquid extraction part 15 is sealed with the extracted refrigerant liquid as in the structural example 16 shown in FIG. 1, so that the negative pressure of the exhaust part 4 is maintained and the zinc chloride melt and zinc chloride fusion are maintained. A mixed melt in which zinc melt is mixed in the liquid, or a mixed melt in which dust-like silicon is mixed with these can be continuously extracted. Further, in order to prevent the splashes and bubbles of the refrigerant liquid from directly scattering and mixing into the liquid extraction unit 15, a baffle plate or a submerged weir is used as the third weir 17 shown in FIG. It can also be set as the structure installed in front of the part 15.

  Formation of a zinc chloride-based melt, such as a zinc chloride melt or a zinc melt mixed with a zinc chloride melt, in the upper layer of the mixed layer 1 suppresses generation of dusty silicon. It works even more effectively. As is apparent from the reaction formula for reducing silicon tetrachloride with zinc shown in the above formula 1, the reduction reaction is suppressed when the reaction conditions are such that zinc chloride is excessively present, that is, the reaction in a direction in which the production of silicon is reduced. The equilibrium of moves.

  In the condensate liquefaction method using the condensate liquefaction apparatus of the present invention, the contact between the introduced gas and the refrigerant liquid is performed in the liquid formed in the upper layer, that is, the gas-liquid contact is performed in the melt mainly composed of zinc chloride. It will be a condition. This is also an important and advantageous feature of the method of the present invention along with the realization of a method for recovering zinc chloride efficiently and stably from a gas containing zinc chloride as a main component.

  EXAMPLES Hereinafter, although an Example is shown and this invention is demonstrated concretely, this invention is not limited by these description.

Example 1
Using a condensing liquefaction apparatus as shown in FIG. 1 and FIG. 5, zinc chloride is put into the mixing unit 1 and the heat exchanging unit 20 and heated so that the zinc chloride melt has a height L1 in the mixing unit 1. I made it. While flowing nitrogen gas heated to 500 ° C., the mixing unit 1 was maintained at 493 ° C. and the heat exchange unit 20 was maintained at 502 ° C. by heating from the outside with a heater.

  Next, 23.9 kg of zinc chloride was placed in the evaporating pot shown in FIG. 5, and the temperature of the evaporating pot was gradually raised while flowing nitrogen gas heated to 700 ° C. After the temperature of the evaporating pot reaches 689 ° C. near the boiling point of zinc chloride, the evaporating pot is further heated to generate zinc chloride as a gas, and the mixed gas of the generated zinc chloride gas and heated nitrogen gas is introduced into the introduction section. 3 was introduced into the mixing section 1. By introducing air as a heat removal medium into the heat removal device 23, heat removal in the heat exchange unit 20 is started, and suction is performed while checking the internal pressure of the exhaust unit 4 and the differential pressure between the exhaust unit 4 and the introduction unit 3. A liquid circulation was generated in the mixing section 1 by adjusting the load of the exhaust device B. The internal temperature of the mixing unit 1 at the start of the condensation liquefaction test was 478 ° C., and the internal temperature of the heat exchange unit 20 was 502 ° C.

  Change the heating intensity of the evaporation kettle, change the evaporation amount of zinc chloride between 5kg / hr and 13.6kg / hr, change the temperature of the thermometers TR1 to TR8, the inlet pressure, the exhaust pressure, the difference The pressure was confirmed. In the heat exchange part 20, the state which flows air to the heat removal apparatus 23 as a heat removal medium, and performed heat removal was maintained. The internal temperature of the mixing unit 1 showed a tendency to decrease with the evaporation amount of zinc chloride of 5 kg / hr, while it showed an increasing tendency with the evaporation amount of zinc chloride of 13.6 kg / hr. When the evaporation amount of zinc chloride was 10.6 kg / hr, the change in the internal temperature of the mixing unit 1 was reduced and stabilized. The condensed zinc chloride melt was extracted from the liquid extraction part 15, and its weight increased with the passage of time. Two hours and 20 minutes after the start of the condensate liquefaction test, the remaining amount of zinc chloride in the evaporation kettle was reduced, so the test was terminated with the heating strength of zinc chloride lowered. The evaporation rate of zinc chloride was determined from the change in the liquid level of zinc chloride.

  Table 3 shows the mass balance of zinc chloride by this condensation liquefaction test. When the total amount of zinc chloride introduced into the apparatus before the test was compared with the total amount of zinc chloride recovered after the test, 97% of the zinc chloride was collected after the test. Zinc chloride gas introduced at a high temperature above the boiling point of zinc chloride was also reliably condensed and collected, indicating that the method of collecting zinc chloride using this condensing liquefaction device was effective. . The amount of zinc chloride which was not collected by the condensing liquefaction device and was condensed in the trap portion was 2% or less of the introduced zinc chloride amount. Since this amount is the same as the amount that cannot be collected with nitrogen gas, calculated from the vapor pressure, the collection of zinc chloride using this condensing liquefaction device calculates the mass balance as theoretically. Thus, it can be understood that the apparatus can be designed.

(Example 2)
For the purpose of confirming the behavior of liquefaction condensation in a mixed state of zinc chloride and zinc, the same device as in Example 1 (however, a zinc gas supply device (not shown) in the same manner as the zinc chloride evaporation kettle is added)) The following tests were conducted using Note that a mixed gas of zinc chloride, zinc, silicon tetrachloride and an inert gas is exhausted from the step of producing high-purity silicon by reducing silicon tetrachloride with zinc. The reaction rate when zinc gas is reacted at an excess rate of 20% with silicon tetrachloride at 950 ° C. is about 60%, and as exhaust gas, by-produced zinc chloride, unreacted zinc and silicon tetrachloride and inert Gas is exhausted. In order to simulate this condition, a test was conducted in which zinc chloride was vaporized at an average rate of 6.4 kg / hr and zinc was vaporized at an average rate of 2.0 kg / hr, and these were heated to 950 ° C. and introduced. . Further, nitrogen gas was introduced as an inert gas in an amount corresponding to the gas volume of unreacted silicon tetrachloride.

The test was conducted according to the following procedure. The mixing part 1 and the heat exchanging part 20 are charged with about 1/20 of the zinc chloride melt, and then the zinc melt is added, so that the zinc chloride melt reaches the height of the throat part of the mixing part 1. The mixing unit 1 was heated to 520 ° C., and the heat exchanging unit 20 was heated to 500 ° C. and held so as to be L1. The density of zinc chloride is 2.9 g / cm ³ (25 ° C.), the zinc is 7.2 g / cm ³ (25 ° C.), 6.5 g / cm ³ (450 ° C.), and the density of zinc is the density of zinc chloride. Since the melt is not mixed with each other more than twice, the zinc chloride melt separates into the upper part and the zinc melt separates into the lower part inside the mixing unit 1 and the heat exchange unit 20. Nitrogen gas heated to 950 ° C. is introduced from the introduction unit 3, air is introduced as a heat removal medium into the heat removal device 23, heat removal in the heat exchange unit 20 is started, the internal pressure of the exhaust unit 4 and the exhaust unit 4 While confirming the differential pressure with the introduction unit 3, the load of the suction / exhaust device B was increased to generate liquid circulation in the mixing unit 1. The flow rate of the heat removal medium was adjusted to wait for the internal temperature of the mixing unit 1 and the internal temperature of the heat exchange unit 20 to stabilize. Immediately after the start of the liquid circulation, the outflow of zinc chloride was observed from the liquid extraction part 15, but the outflow of zinc chloride stopped with the passage of time, and both the liquid extraction part 15 and the liquid extraction part 24 were melted with zinc. Liquid outflow was not confirmed. The internal temperature of the mixing part 1 was in the range of 520 to 540 ° C., and the internal temperature of the heat exchange part 20 was almost stable in the range of 500 to 530 ° C.

  Next, increase the heating strength of the evaporating pot containing zinc chloride and the evaporating pot containing zinc so that zinc chloride and zinc each have a predetermined evaporation rate, and mix the evaporated zinc chloride and zinc with nitrogen gas. The mixed gas was heated to 950 ° C. and introduced from the introduction part 3. The heating of the mixing unit 1 and the heat exchange unit 20 was stopped, the amount of heat removal was increased by increasing the flow rate of the heat removal medium, and zinc chloride and zinc were continuously introduced for 3 hours while observing the temperature change. When the introduction of the zinc chloride gas and the zinc gas was started, the outflow started from the liquid extraction part 15. Although the effluent contained a small amount of residue, it was judged that the effluent was mainly composed of zinc chloride because it was well dissolved in water. The outflow from the liquid withdrawal portion 15 continued until the introduction of zinc chloride and zinc was stopped. On the other hand, no outflow of liquid was observed from the liquid extraction part 24 for a while, but outflow began as time passed. Since the initial effluent from the liquid extraction part 24 was well dissolved in water, it was determined that the main component was zinc chloride. Over time, the effluent turned into a liquid with a metallic luster, which was determined to be based on zinc. This result shows that when zinc chloride and zinc are condensed in a mixed state, the zinc melt having a high specific gravity becomes a refrigerant liquid that circulates through the mixing unit 1 and the heat exchange unit 20. The amounts of zinc chloride and zinc introduced in the test were 20.5 kg of zinc chloride and 6.5 kg of zinc. During the test, the temperature of the mixing unit 1 was in the temperature range of 510 to 570 ° C, the internal temperature of the heat exchange unit 20 was in the temperature range of 490 to 550 ° C, and the exhaust gas temperature was changed in the temperature range of 520 to 570 ° C.

  Even when zinc chloride and zinc are condensed in a mixed state, zinc chloride and zinc can be condensed and collected, and further, zinc chloride and zinc melt are separated inside the mixing unit 1, The refrigerant liquid circulates between the mixing unit 1 and the heat exchange unit 20, the zinc chloride melt is extracted from the liquid extraction unit 15 provided in the mixing unit 1, and the zinc melt is supplied from the liquid extraction unit 24 provided in the heat exchange unit 20. It can be seen that it can be extracted.

  According to the present invention, a basic technique and method for efficiently recovering zinc chloride by-produced from a production process of high-purity silicon in which silicon tetrachloride is reduced with zinc is realized. As a result, the recovered zinc chloride is subjected to molten salt electrolysis to produce chlorine and zinc, and the produced chlorine is directly used for reaction with metal silicon or used as a raw material for producing silicon tetrachloride via hydrogen chloride. By using electrolytic zinc as a reducing agent for silicon tetrachloride, it becomes possible to circulate and use the by-produced chloride, so that high-purity silicon can be produced at low cost.

1: Mixing unit 2: Refrigerant liquid 3: Introduction unit 4: Exhaust unit 5: First weir 6: Second weir 7: Refrigerant liquid outlet 8: Refrigerant liquid return port 9: Bubbles and spray 10: Upper clearance 11: Upper clearance 12: Lower clearance 13: Lower clearance 15: Liquid extraction unit 16: Liquid sealed liquid extraction example 17: Third weir 20: Heat exchange unit 21: Refrigerant liquid inlet 22: Refrigerant liquid outlet 23: Heat removal device 24: Liquid extraction part 25: Liquid extraction part 26: Pressure equalization connection and inert gas seal connection hole 27: Refrigerant liquid pipe 28: Refrigerant liquid return pipe A: Zinc chloride gas discharge source (zinc tetrachloride zinc reduction device)
B: Suction / exhaust device L: Storage height difference L1: Throat height L2: Upper height of second weir 6 TR1 to TR10: Thermometers M1 to M3: Manometer

Claims (17)

(A) an introduction part for introducing gas;
(B) an inclined mixing section having a first weir and a second weir and storing the refrigerant liquid;
(C) a heat exchange unit connected to the mixing unit for removing heat from the refrigerant liquid;
(D) an exhaust unit to which a suction exhaust device is connected;
(E) A condensing and liquefying apparatus, comprising: a liquid extraction section that is provided in the mixing section and the heat exchange section and extracts liquid.   The condensing and liquefying apparatus according to claim 1, wherein the mixing portion is inclined within a range of 10 to 35 degrees from a horizontal plane.   The condensing and liquefying apparatus according to claim 1, wherein the liquid extraction unit is provided on the exhaust unit side of the mixing unit.   The condensing and liquefying apparatus according to claim 3, wherein a third weir is provided in front of the liquid extraction portion provided on the exhaust portion side of the mixing portion.   Using the condensing and liquefying apparatus according to any one of claims 1 to 4, a step of storing a refrigerant liquid inside the mixing unit and the heat exchange unit, and a step of introducing a gas containing zinc chloride from the introduction unit, And a step of liquefying a condensed component containing zinc chloride from the introduced gas and collecting it in a refrigerant liquid.   Utilizing the negative pressure of the exhaust part generated by the suction exhaust system, the gas containing zinc chloride introduced from the introduction part is moved in the refrigerant liquid of the mixing part, and direct gas-liquid contact between the introduced gas and the refrigerant liquid A heat exchange step using the method, and a condensed component containing zinc chloride is liquefied and collected in a refrigerant liquid, and then the refrigerant liquid is sent from the mixing unit to the heat exchange unit to remove heat from the refrigerant liquid in the heat exchange unit. Further, the step of returning the refrigerant liquid after heat removal to the mixing unit to circulate the refrigerant liquid, the step of extracting a part of the refrigerant liquid from the liquid extraction unit provided in the mixing unit or the heat exchange unit, and the mixing unit 6. The condensate liquefaction method according to claim 5, further comprising a step of exhausting the exhausted gas from the exhaust unit.   The condensing and liquefying method according to claim 6, wherein a liquid extraction portion provided in the mixing portion is sealed with the extracted refrigerant liquid.   The refrigerant liquid which collected the condensing component forms two layers of a layer made of a refrigerant liquid having a low specific gravity and a layer made of a refrigerant liquid having a high specific gravity in the mixing portion. The condensate liquefaction method according to any one of the above.   9. The condensing and liquefying method according to claim 8, wherein the refrigerant liquid having a large specific gravity is sent from the mixing section to the heat exchange section to remove heat, and then returned to the mixing section for circulation.   A refrigerant liquid outlet from the mixing unit to the heat exchange unit and a refrigerant liquid return port from the heat exchange unit to the mixing unit are provided in the mixing unit so as to open into the layer composed of the refrigerant liquid having a large specific gravity. The condensate liquefaction method according to claim 8 or 9, wherein a condensate liquefaction apparatus is used.   The gas containing zinc chloride is a mixed gas containing zinc chloride and one or more gases selected from the group consisting of zinc and silicon tetrachloride, or a mixed gas containing an inert gas in the mixed gas. It is, The condensate liquefaction method as described in any one of Claims 5-10 characterized by the above-mentioned.   The condensate liquefaction method according to claim 5, wherein the refrigerant liquid is a zinc chloride melt, a zinc melt, or a melt containing both zinc chloride and zinc.   The refrigerant liquid extracted from the liquid extraction part provided in the mixing part is a zinc chloride melt or a mixed melt in which a zinc melt is mixed with a zinc chloride melt, and provided in the heat exchange part. The condensation liquid according to any one of claims 6 to 12, wherein the refrigerant liquid withdrawn from the liquid withdrawal portion is a zinc melt or a mixed melt in which a zinc chloride melt is mixed with a zinc melt. Liquefaction method.   The condensed liquefaction method according to any one of claims 5 to 13, wherein the gas containing zinc chloride is introduced in a temperature range of 800 ° C to 1100 ° C.   By controlling the circulation amount of the refrigerant liquid that circulates between the mixing unit and the heat exchange unit and the heat removal amount of the heat exchange unit, the temperature of the refrigerant liquid that returns to the mixing unit is maintained in the range of 420 ° C. to 650 ° C., and the exhaust unit The condensate liquefaction method according to any one of claims 6 to 14, wherein the temperature of the exhaust gas discharged from the exhaust gas to the suction exhaust device is maintained at 700 ° C or lower.   The liquid extracted from the liquid extraction part provided in the mixing part is a mixed melt in which dust-like silicon is further mixed in a zinc chloride melt or a mixed melt in which zinc melt is mixed in zinc chloride melt. The condensate liquefaction method according to any one of claims 6 to 15.   The amount of heat from which the refrigerant liquid is removed by a heat exchange section is a heat amount corresponding to the sum of the latent heat of the condensed component and the amount of heat required for cooling the introduced gas. The condensate liquefaction method according to one item.

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