Gas supply system and leaching system

Abstract

The present application discloses a gas supply system and a leaching system, comprising: a first buffer tank, into which the gas is injected through the gas inlet of the first buffer tank; a gas compression device, wherein the gas inlet of the gas compression device is connected to the gas outlet of the first buffer tank; a second buffer tank, wherein the gas inlet of the second buffer tank is connected to the gas outlet of the gas compression device; a liquid storage device, wherein the liquid inlet is connected to the gas outlet of the second buffer tank through a first return line, and the liquid outlet is connected to the gas inlet of the second buffer tank through a second return line, wherein the first return line is provided with a cooler, which liquefies the gas output from the second buffer tank, and the second return line is provided with a heater, which vaporizes the liquid output from the liquid storage device. Thus, the gas supply system can provide gas with stable pressure and flow to the external system.

Description

Technical Field

[0001] The invention belongs to the field of metallurgy, and in particular relates to a gas supply system and a leaching system. Background Art

[0002] Typically, gas-based reaction devices require the gas introduced into the reactor to meet certain flow rates, pressures, and temperatures. For example, in hydrometallurgical processes, when sulfur dioxide gas is used for reduction leaching of zinc slag, the pressure and flow of the sulfur dioxide gas introduced into the reactor must be stable to promote efficient leaching. However, current sulfur dioxide gas supply systems suffer from unstable pressure and flow rates during the gas supply process, resulting in low leaching efficiency.

[0003] Therefore, the current gas supply system and leaching system still need to be improved. Summary of the Invention

[0004] The present invention is based on the inventor's discovery of the following problems:

[0005] The inventors discovered that when sulfur dioxide gas is used as a reducing agent to reduce zinc slag during leaching, if the pressure of the sulfur dioxide gas entering the reactor is too high, it can cause the reactor's safety valve to trip. If the pressure is too low, the slurry in the reactor can backflow into the sulfur dioxide gas supply line. Excessive sulfur dioxide gas injection can lead to corrosion of the reactor, while too low a level can reduce the efficiency of the leaching reaction.

[0006] The present invention aims to alleviate or solve at least one of the above-mentioned problems to a certain extent.

[0007] In one aspect of the present invention, a gas supply system is proposed, comprising: a first buffer tank, the first buffer tank having a first buffer tank gas inlet and a first buffer tank gas outlet, the gas being injected into the first buffer tank through the first buffer tank gas inlet; a gas compression device, the gas compression device having a gas compression device gas inlet and a gas compression device gas outlet, the gas compression device gas inlet being connected to the first buffer tank gas outlet; a second buffer tank, the second buffer tank having a second buffer tank gas inlet and a second buffer tank gas outlet, the second buffer tank gas inlet being connected to the gas compression device gas outlet; a liquid storage device, the liquid storage device having a liquid inlet and a liquid outlet, the liquid inlet being connected to the second buffer tank gas outlet via a first return line, the liquid outlet being connected to the second buffer tank gas inlet via a second return line, the first return line having a cooler, the cooler liquefying the gas outputted from the second buffer tank, the second return line having a heater, the heater vaporizing the liquid outputted from the liquid storage device. Thus, the gas supply system can provide gas with stable pressure and flow to an external system.

[0008] According to an embodiment of the present invention, the gas compression device includes multiple compressors connected in parallel, wherein the gas inlets of the multiple compressors are connected to the gas outlet of the first buffer tank, and the gas outlets of the multiple compressors are connected to the gas inlet of the second buffer tank. This can further promote the stability of the gas pressure in the gas supply system.

[0009] According to an embodiment of the present invention, the pressure of the gas after being compressed by the compressor is 0.35 MPa-0.8 MPa, thereby further providing gas at a moderate pressure, thereby further promoting the stability of the gas pressure in the gas supply system.

[0010] According to an embodiment of the present invention, the liquid storage device includes multiple parallel liquid storage tanks, the liquid inlets of each of the multiple liquid storage tanks being connected to the gas outlet of the second buffer tank via the first return line, and the liquid outlets of each of the multiple liquid storage tanks being connected to the gas inlet of the second buffer tank via the second return line. This further promotes the stability of gas flow in the gas supply system.

[0011] According to an embodiment of the present invention, the cooling medium of the cooler includes cooling water having a temperature of 20°C-30°C, and the heating medium of the heater includes evaporated condensed water having a temperature of 90°C-95°C. As a result, more liquefied gas can be stored in the storage device, thereby promoting the stability of the gas flow in the gas supply system.

[0012] In another aspect, the present invention provides a leaching system comprising the aforementioned gas supply system, wherein the gas comprises sulfur dioxide gas. Thus, the leaching system has all the features and advantages of the aforementioned gas supply system, which will not be further elaborated here.

[0013] According to an embodiment of the present invention, the leaching system further includes: a supply pipe having a gas flow valve installed thereon, one end of the supply pipe being connected to the gas outlet of the second buffer tank; and a reaction unit having a reaction unit gas inlet connected to the other end of the supply pipe. This improves the efficiency of the leaching reaction in the reaction unit.

[0014] According to an embodiment of the present invention, a pressure reducing valve is installed at one end of the supply pipeline connected to the gas outlet of the second buffer tank. After being reduced by the pressure reducing valve, the pressure of the sulfur dioxide gas is reduced to 0.3 MPa-0.4 MPa. This provides a stable pressure gas to the reaction device, thereby improving the efficiency of the leaching reaction within the reaction device.

[0015] According to an embodiment of the present invention, the reaction apparatus includes multiple reactors connected in series via a slurry pipeline. Each reactor has a reactor gas inlet connected to the end of the supply pipeline remote from the second buffer tank. The gas flow valve on the supply pipeline corresponding to at least one reactor at the end of the slurry pipeline where slurry flows is closed. The pressure in the reactor is lower than the pressure of the sulfur dioxide gas after being reduced by the pressure reducing valve. This further provides a stable pressure gas for the leaching system, preventing slurry from the reactors in the leaching system from flowing back into the supply pipeline.

[0016] According to an embodiment of the present invention, the temperature of the sulfur dioxide gas after compression by the compressor is 90°C-130°C; the temperature of the sulfur dioxide liquid formed after the sulfur dioxide gas is cooled by the cooler is 35°C-45°C; and the temperature of the sulfur dioxide gas formed after the sulfur dioxide liquid is vaporized by the heater is 45°C-60°C. Thus, the reaction efficiency of the leaching reaction in the reaction device can be improved. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 is a schematic structural diagram of a gas supply system according to one embodiment of the present invention;

[0018] Figure 2 is a schematic structural diagram of a gas supply system according to one embodiment of the present invention;

[0019] Figure 3 is a schematic structural diagram of a leaching system according to one embodiment of the present invention;

[0020] Figure 4 is a schematic structural diagram of a leaching system according to one embodiment of the present invention;

[0021] Figure 5 Schematic diagram of the structure of a leaching system according to one embodiment of the present invention.

[0022] Reference numerals:

[0023] 10: First buffer tank; 11: First buffer tank gas inlet; 12: First buffer tank gas outlet; 20: Gas compression device; 21: Gas compression device gas inlet; 22: Gas compression device gas outlet; 30: Second buffer tank; 31: Second buffer tank gas inlet; 32: Second buffer tank gas outlet; 40: Cooler; 41: Cooler gas inlet; 42: Cooler gas outlet; 43: Cooling medium inlet; 44: Cooling medium outlet; 50: Liquid storage device; 51: Liquid inlet; 52: Liquid outlet; 60: Heater; 61: Heater liquid inlet; 62: Heater gas outlet; 63: Heating medium inlet; 64: Heating Medium outlet; 70: Pressure reducing valve; 71: Pressure reducing valve gas inlet; 72: Pressure reducing valve gas outlet; 80: Reactor; 81: Reactor gas inlet; Slurry pipeline: 90; External system: 100; 200: Compressor; 201: Compressor gas inlet; 202: Compressor gas outlet; 500: Liquid storage tank; 501: Liquid inlet of liquid storage tank; 502: Liquid outlet of liquid storage tank; 800: Reactor; 801: Reactor gas inlet; 1001: First reflux pipeline; 1001: Second reflux pipeline; 2000: Supply pipeline; 2001: Gas flow valve; 2002: Main supply pipeline; 2003: Sub-supply pipeline. DETAILED DESCRIPTION

[0024] The following describes in detail embodiments of the present application. Examples of the embodiments are shown in the accompanying drawings, wherein the same or similar reference numerals throughout represent the same or similar elements or elements having the same or similar functions. The embodiments described below with reference to the accompanying drawings are exemplary and are only used to explain the present application and are not to be construed as limiting the present application.

[0025] In one aspect of the present invention, the present invention provides a gas supply system. According to some embodiments of the present invention, referring to Figure 1 The system includes a first buffer tank 10 , a gas compression device 20 , a second buffer tank 30 , a cooler 40 , a liquid storage device 50 and a heater 60 .

[0026] According to some embodiments of the present invention, reference Figure 1The first buffer tank 10 has a first buffer tank gas inlet 11 and a first buffer tank gas outlet 12. Gas enters the first buffer tank 10 through the first buffer tank gas inlet and enters the gas compression device 20 through the first buffer tank gas outlet 12. As a gas buffer unit, the first buffer tank can reduce downtime of the gas supply system caused by fluctuations in gas flow at the first buffer tank gas inlet.

[0027] According to some embodiments of the present invention, reference Figure 1 The gas compression device 20 has a gas compression device gas inlet 21 and a gas compression device gas outlet 22. The gas compression device gas inlet 21 is connected to the first buffer tank gas outlet 12, wherein the gas in the first buffer tank 10 enters the gas compression device 20 through the gas compression device gas inlet 21. After the gas entering the gas compression device 20 is compressed, it enters the second buffer tank 30 through the gas compression device gas outlet 22. The gas compression device, as the source of gas pressure in the gas supply system, can increase the pressure of the compressed gas, thereby enabling the gas compression device to provide gas with stable pressure to the external system, wherein the external system refers to a system that uses the gas supply system to supply gas.

[0028] According to some embodiments of the present invention, reference Figure 1 The second buffer tank 30 has a second buffer tank gas inlet 31 and a second buffer tank gas outlet 32. The second buffer tank gas inlet 31 is connected to the gas outlet 22 of the gas compression device. Specifically, the gas in the compression device 20 enters the second buffer tank 30 through the second buffer tank gas inlet 31, and the gas in the second buffer tank 30 is transported to the external system 100 through the second buffer tank gas outlet 32. On the other hand, the gas in the second buffer tank 30 enters the cooler 40 through the second buffer tank gas outlet 32 and is liquefied to form liquefied gas. The liquefied gas enters the liquid storage device 50 and is stored. Specifically, the gas compressed by the compression device is transmitted to the second buffer tank for temporary storage. Part of the gas in the second buffer tank is transported to the external system for use, and the other part of the gas is transported to the heater 40 for liquefaction and then enters the liquid storage device for storage. When the gas flow in the first buffer tank is insufficient, the liquefied gas in the liquid storage device can be used as a source of gas flow, so that the gas supply system can continuously provide the external system with gas with stable flow and pressure.

[0029] According to some embodiments of the present invention, reference Figure 1The liquid storage device 50 has a liquid inlet 51 and a liquid outlet 52. A cooler 40 is provided on the first return line 1001 between the liquid inlet 51 and the second buffer tank gas outlet 32. The cooler 40 has a cooler gas inlet 41, a cooler liquid outlet 42, a cooling medium inlet 43 and a cooling medium outlet 44. A heater 60 is provided on the second return line 1002 between the liquid outlet 52 and the second buffer tank gas inlet 31. The heater 60 has a heater liquid inlet 61, a heater gas outlet 62, a heating medium inlet 63 and a heating medium outlet 64. Specifically, the gas in the second buffer tank 30 enters the cooler 40 through the cooler gas inlet 41 and enters the cooler 40. The gas in the cooler exchanges heat with the cooling medium entering through the cooler cooling medium inlet 43 and liquefies to form liquefied gas. The cooling medium after heat exchange is discharged from the cooler cooling medium outlet 44. The liquefied gas is output from the cooler liquid outlet 42 through the first return pipe 1001 and enters the liquid storage device 50. The liquid stored in the liquid storage device 50 is output through the liquid storage device liquid outlet 52 and enters the heater 60. The liquid entering the heater 60 exchanges heat with the heating medium entering through the heater heating medium inlet 63 and vaporizes to form gas. The heating medium after heat exchange is discharged from the heater heating medium outlet 64. The vaporized gas enters the second buffer tank 30 through the second return pipe 1002 to be utilized. The liquefied gas stored in the liquid storage device enters the heater and is vaporized to form gas. The vaporized gas enters the second buffer tank for use by the external system, thereby reducing the risk of gas supply system shutdown caused by insufficient gas volume in the first buffer tank and fluctuations in gas volume at the gas inlet of the first buffer tank.

[0030] According to some embodiments of the present invention, reference Figure 2 The gas compression device includes multiple parallel compressors 200, each of which has a compressor gas inlet 201 and a compressor gas outlet 202. The gas inlets of the multiple compressors 200 are all connected to the first buffer tank gas outlet 12, and the multiple compressor gas outlets 202 are all connected to the second buffer tank gas inlet 31. Since the compressor can increase the temperature and pressure of the compressed gas, the compressor can provide gas with stable pressure and appropriate temperature to the external system.

[0031] According to some embodiments of the present invention, the type of compressor is not particularly limited. For example, the compressor can be a piston compressor. A piston compressor increases the pressure and temperature of the gas through three processes: suction, compression, and exhaust. In the present invention, the number of compression stages of the piston compressor is also not particularly limited. For example, the number of compression stages of the piston compressor can be two, wherein each compression stage is equipped with a pressure detection device, which can monitor the pressure of the gas online in real time to ensure the stability of the pressure of the gas in the gas supply system. It should be noted that the pressure of the gas compressed by the compressor remains unchanged during the transportation process within the gas supply system. Therefore, the gas compressed by the compressor is a gas with a stable pressure supplied by the gas supply system to the external system.

[0032] According to other embodiments of the present invention, the compressor may be at least one of a positive displacement compressor, a rotary compressor, a vane compressor, a speed compressor and a centrifugal compressor, thereby providing gas with a certain pressure to the external system.

[0033] According to some embodiments of the present invention, the compressor increases the pressure and temperature of the gas through the three processes of suction, compression and exhaust. The pressure of the gas compressed by the compressor is not particularly limited. For example, the pressure of the gas compressed by the compressor can be 0.35MPa-0.8MPa. When the pressure of the compressed gas is 0.35MPa-0.8MPa, the risk of shutdown of the gas supply system and the external system due to excessively high or low pressure can be reduced.

[0034] According to some embodiments of the present invention, the compressor can increase the temperature of the compressed gas. The gas with increased temperature enters the second buffer tank and is transported to the external system, which can meet the external system's requirements for gas temperature and thereby improve the external system's gas utilization rate.

[0035] According to some embodiments of the present invention, reference Figure 2 The liquid storage device includes multiple parallel liquid storage tanks 500, and the liquid inlets 501 of the multiple liquid storage tanks are all connected to the gas outlet 32 of the second buffer tank through a first return pipe 1001, and the liquid outlets 502 of the multiple liquid storage tanks are all connected to the gas inlet 31 of the second buffer tank through a second return pipe 1002. Specifically, the gas in the second buffer tank enters the cooler and is liquefied to form liquefied gas. The liquefied gas enters the liquid storage tank for storage through the first return pipe. When the gas flow of the first buffer tank is insufficient and / or the gas flow at the gas inlet of the first buffer tank fluctuates, the liquefied gas in the liquid storage tank enters the heater and is vaporized to form gas. The vaporized gas enters the second buffer tank through the second return pipe and is then used by the external system, so that the gas supply system can provide a stable gas flow for the external system.

[0036] In the description of this application, "A and / or B" may include the case of A alone, the case of B alone, or any of the cases of A and B, where A and B are only used for example, and may be any technical feature connected by "and / or" in this application.

[0037] According to some embodiments of the present invention, the number of liquid storage tanks is not particularly limited. For example, there can be multiple liquid storage tanks. When the liquid storage tanks are enabled as the gas source in the gas supply system, the gas supply system can further provide a stable gas flow to the external system.

[0038] According to some embodiments of the present invention, the cooler can liquefy the gas transported from the second buffer tank. The cooling medium of the cooler is not particularly limited. For example, the cooling medium can be cooling water. When the cooling medium is cooling water, refer to Figure 2 The cooler further includes a cooling medium inlet 43 and a cooling medium outlet 44. Specifically, cooling water enters the cooler from the cooling medium inlet 43 and exchanges heat with the gas entering the cooler gas inlet 41. The cooling water return water after heat exchange is discharged from the cooling medium outlet 44, and the liquefied gas after heat exchange enters the liquid storage tank 500 from the cooler liquid outlet 42. The temperature of the cooling water is not particularly limited. For example, the temperature of the cooling water can be 20℃-30℃. When the temperature of the cooling water is 20℃-30℃, it can promote the liquefaction of the gas in the cooler into liquefied gas, thereby allowing as much liquefied gas as possible to be stored in the liquid storage tank.

[0039] According to some embodiments of the present invention, the purpose of the heater is to vaporize the liquid transported from the liquid storage tank to the heater to form a gas. The heating medium of the heater is not particularly limited. For example, the heating medium can be evaporated condensed water. When the heating medium is evaporated condensed water, refer to Figure 2 The heater further includes a heater medium inlet 63 and a heater medium outlet 64. Specifically, evaporated condensed water enters the heater from the heater medium inlet 63 and exchanges heat with the liquid in the heater. The evaporated condensed water return water after heat exchange is discharged from the heater medium outlet 64, and the gas after heat exchange enters the second buffer tank from the heater gas outlet 62 to be utilized. The temperature of the aforementioned evaporated condensed water is not particularly limited. For example, the temperature of the evaporated condensed water can be 90℃-95℃. When the temperature of the evaporated condensed water is 90℃-95℃, on the one hand, it can promote the liquid entering the heater to vaporize into gas, which is beneficial for the vaporized gas to enter the second buffer tank and then be supplied to the external system for utilization. On the other hand, the evaporated condensed water can also increase the temperature of the vaporized gas, thereby further promoting the stability of the gas flow in the gas supply system and improving the utilization rate of the gas transported to the external system by the gas supply system.

[0040] In a second aspect of the present invention, the present invention provides a leaching system, comprising the aforementioned gas supply system. Thus, the leaching system has all the features and advantages of the aforementioned gas supply system, which will not be described in detail here.

[0041] According to some embodiments of the present invention, the type of gas in the leaching system is not particularly limited. For example, the gas in the device can be sulfur dioxide gas, and the reaction in the reaction device can be sulfur dioxide leaching valuable metals in zinc slag and Fe in the leachate. 3+ Reduction to Fe 2+ To promote the decomposition of ferrite, the leaching process includes the following steps: the leaching agent diffuses to the solid surface through the diffusion layer, the leaching agent further diffuses through the solid layer, the leaching agent reacts chemically with the mineral particles, and an adsorption and desorption process is accompanied. The insoluble product layer generated by the reaction thickens the solid film, and the generated soluble product diffuses through the solid film into the solution to complete the leaching reaction. Increasing the temperature can increase the diffusion of the leaching agent to the solid surface and increase the apparent activation energy of the chemical reaction, thereby promoting the reaction efficiency of the leaching reaction. Increasing the pressure can promote the speed at which the leaching agent infiltrates the mineral particles, thereby promoting the reaction efficiency of the leaching reaction. In the present invention, the reduction leaching process in which sulfur dioxide gas is used as a reducing agent can leach the valuable metals copper, zinc and indium in the zinc slag, as well as Fe in the leachate. 3+ Reduction to Fe 2+ In order to promote the decomposition of ferrite, the aforementioned gas supply system is used to provide sulfur dioxide gas for the leaching reaction. When the leaching reaction temperature is controlled at 105°C-120°C and the pressure of the reactor is controlled at 0.15MPa-0.3MPa, the leaching rate of zinc in the reduction leaching section can reach 90%-95%, the leaching rate of indium can reach 70%-80%, the leaching rate of copper can reach 70%-80%, and the leaching rate of Fe can reach 100%. 3+ Reduction to Fe 2+ The reduction rate can reach 100%. It can be seen that whether sulfur dioxide can be stably introduced into the reaction device plays a key role in the reaction efficiency of the leaching reaction.

[0042] According to some embodiments of the present invention, the concentration of sulfur dioxide injected from the gas inlet of the first buffer tank is not particularly limited. For example, the molar ratio concentration of sulfur dioxide can be 90%-99%. The molar ratio concentration of sulfur dioxide is 90%-99%, which can further improve the reaction efficiency of the leaching reaction.

[0043] According to some embodiments of the present invention, reference Figure 3The device for leaching reaction using gas further includes a supply pipeline 2000 and a reaction device 80. The reaction device 80 has a reaction device gas inlet 81. The supply pipeline 2000 is provided with a gas flow valve 2001. Specifically, one end of the supply pipeline 2000 is connected to the gas outlet 32 of the second buffer tank, and the other end of the supply pipeline 2000 is connected to the reaction device gas inlet 81. In the present invention, the flow rate of sulfur dioxide gas in the supply pipeline can be controlled by adjusting the gas flow valve according to the requirements of the sulfur dioxide leaching slurry reaction in the reaction device to improve the reaction efficiency of the leaching reaction.

[0044] According to some embodiments of the present invention, reference Figure 3 A pressure reducing valve 70 is provided at one end of the supply pipe 2000 connected to the gas outlet 32 of the second buffer tank. The pressure reducing valve 70 has a pressure reducing valve gas inlet 71 and a pressure reducing valve gas outlet 72. The pressure reducing valve reduces the pressure at the pressure reducing valve gas inlet to a desired pressure at the pressure reducing valve gas outlet, automatically maintaining a stable pressure at the pressure reducing valve gas outlet by relying on the energy of the medium itself. In the present invention, sulfur dioxide gas output from the second buffer tank 30 enters the pressure reducing valve 70 through the pressure reducing valve gas inlet 71. The decompressed sulfur dioxide gas is then output from the pressure reducing valve gas outlet 72 through the supply pipe and enters the reactor. The pressure of the sulfur dioxide gas after decompression by the pressure reducing valve can be stabilized at 0.3 MPa to 0.4 MPa. This further improves the efficiency of the leaching reaction in the reactor.

[0045] According to some embodiments of the present invention, reference Figure 4 The reaction device includes a plurality of reactors 800 connected in series via a slurry pipeline 90. The reactors 800 have a reactor gas inlet 801, wherein the reactor gas inlet 801 is connected to the end of the supply pipeline 2000 away from the second buffer tank 30. The gas flow valve 2001 on the supply pipeline corresponding to at least one reactor 801 at the end of the slurry pipeline in the slurry pipeline 90 is in a closed state. Specifically, the gas after being reduced in pressure by the pressure reducing valve enters the reactor through the supply pipeline, wherein the gas flow valve corresponding to the reactor at the end of the slurry pipeline flowing to the end is in a closed state. Therefore, the reactor at the end can be used as a decomposition kettle to decompose the waste slurry transported through the slurry pipeline, so that the discharged waste slurry meets environmental protection requirements. Specifically, refer to Figure 5The supply pipeline may include a main supply pipeline 2002 and a sub-supply pipeline 2003, wherein a gas flow valve 2001 is provided on the sub-supply pipeline. Specifically, one end of the main supply pipeline 2002 is connected to the second buffer tank 30, and the end of the main supply pipeline 2002 connected to the second buffer tank 30 is provided with a pressure reducing valve 70. One end of the sub-supply pipeline 2003 is connected to the gas inlet 801 of the reactor, and the other end of the sub-supply pipeline 2003 is connected to the end of the main supply pipeline 2002 away from the pressure reducing valve 70 and the pipeline portion of the main supply pipeline. In the present invention, the gas flow valve 2001 on the sub-supply pipeline corresponding to at least one reactor 801 at the end of the slurry pipeline 90 where the slurry flows to is closed. Specifically, the gas after being reduced in pressure by the pressure reducing valve enters the reactor through the supply pipeline, wherein the gas flow valve on the sub-supply pipeline corresponding to the reactor at the end of the slurry pipeline where the slurry flows to is closed. Therefore, the reactor at the end can be used as a desorption reactor to decompose the waste slurry transported through the slurry pipeline, so that the discharged waste slurry meets environmental protection requirements.

[0046] According to some embodiments of the present invention, the leaching reaction device for leaching zinc slag using sulfur dioxide reduction is a high-temperature pressurized reactor, wherein the pressure requirement of the reactor is 0.15MPa-0.3MPa. The compressor can increase the pressure of the sulfur dioxide gas during the compression process. The pressure of the increased sulfur dioxide gas after being reduced by a pressure reducing valve is greater than the pressure of the reactor. For example, the pressure of the sulfur dioxide after being reduced by the pressure reducing valve is greater than the pressure of the reactor by 0.1MPa-0.2MPa. When the pressure of the sulfur dioxide after being reduced by the pressure reducing valve is greater than the pressure of the reactor by 0.1MPa-0.2MPa, the backflow of zinc slag in the reactor into the supply pipeline can be prevented, thereby improving the reaction efficiency of the leaching reaction.

[0047] According to some embodiments of the present invention, the leaching reactor for leaching zinc slag using sulfur dioxide reduction is a high-temperature, high-pressure reaction device, wherein the reaction temperature is required to be 105°C-120°C. The temperature of the sulfur dioxide gas can be increased during the compression process of the compressor. The temperature of the compressed sulfur dioxide gas is not particularly limited. For example, the temperature of the compressed sulfur dioxide can be 90°C-130°C. When the temperature of the compressed sulfur dioxide is 90°C-130°C, the diffusion of the leaching agent to the zinc slag surface can be accelerated, the apparent activation energy of the chemical reaction can be increased, and thus the reaction efficiency of the leaching reaction can be improved.

[0048] According to some embodiments of the present invention, the purpose of the cooler is to liquefy the sulfur dioxide gas therein to form sulfur dioxide liquid. The temperature of the sulfur dioxide liquid is not particularly limited. For example, the temperature of the sulfur dioxide liquid may be 35°C-45°C.

[0049] According to some embodiments of the present invention, the temperature of the vaporized sulfur dioxide gas after heating by the heater is not particularly limited. For example, the temperature of the vaporized sulfur dioxide gas can be 45°C-60°C. When the temperature of the vaporized sulfur dioxide gas is 45°C-60°C, the efficiency of the leaching reaction can be improved. It should be noted that the temperature of the sulfur dioxide gas after compression by the compressor is higher than the temperature of the sulfur dioxide gas after vaporization by the heater. However, since both the sulfur dioxide gas compressed by the compressor and the sulfur dioxide gas vaporized by the heater have a certain temperature, they can both promote the efficiency of the leaching reaction.

[0050] The present invention is described below with reference to specific examples. It should be noted that these examples are merely illustrative and do not limit the present invention in any way.

[0051] refer to Figure 5 The leaching system is used to carry out the reaction of sulfur dioxide leaching valuable metals in zinc slag, and the Fe 3+ Reduction to Fe 2+ Table 1 shows the process parameters of the leaching system when the gas flow rate of the first buffer tank is sufficient, and Table 2 shows the process parameters of the leaching system when the pressure of the first buffer tank is insufficient.

[0052] Inductively coupled plasma emission spectrometry was used to quantitatively analyze the valuable metal content in the zinc slag before and after the leaching reaction during the sulfur dioxide reduction leaching of zinc slag, and then the leaching rates of zinc, indium and copper in Tables 1 and 2, as well as Fe 3+ Reduction to Fe 2+ The reduction rate.

[0053] Table 1

[0054]

[0055] Table 2

[0056]

[0057] Therefore, the gas supply system is used to supply sulfur dioxide gas for the leaching reaction in the reaction device. When the gas flow in the first buffer tank is sufficient or insufficient, the zinc leaching rate in the zinc slag can reach 90%-95%, the copper leaching rate can reach 70%-80%, the indium leaching rate can reach 70%-80%, and the Fe leaching rate can reach 90%-95%. 3+ Reduction to Fe 2+ The reduction rate can reach 100%; and when the pressure of the first buffer tank is insufficient, the liquefied gas in the liquid storage tank is enabled as the source of gas in the gas supply system, and the gas supply system can continuously provide gas for the reaction device in the leaching system.

[0058] In the present invention, unless otherwise expressly specified or limited, the terms "mounted," "connected," "connect," "fixed," etc. should be understood broadly. For example, they may refer to fixed connection, detachable connection, or integration; mechanical connection or electrical connection; direct connection or indirect connection through an intermediate medium; internal communication between two components or interaction between two components. Those skilled in the art will understand the specific meanings of the above terms in the present invention based on specific circumstances.

[0059] In the description of this specification, the reference terms "one embodiment", "some embodiments", "example", "specific example", or "some examples" mean that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described can be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art can combine and combine different embodiments or examples described in this specification and features of different embodiments or examples without contradiction.

[0060] Although the embodiments of the present invention have been shown and described above, it will be understood that the above embodiments are illustrative and are not to be construed as limitations on the present invention. A person skilled in the art may change, modify, replace and modify the above embodiments within the scope of the present invention.

Claims

1. A gas supply system for providing sulfur dioxide gas as a reducing agent when reducing zinc leaching slag, characterized in that: include: a first buffer tank, wherein the first buffer tank has a first buffer tank gas inlet and a first buffer tank gas outlet, and the gas is injected into the first buffer tank through the first buffer tank gas inlet; a gas compression device, the gas compression device having a gas compression device gas inlet and a gas compression device gas outlet, the gas compression device gas inlet being connected to the first buffer tank gas outlet; a second buffer tank, the second buffer tank having a second buffer tank gas inlet and a second buffer tank gas outlet, the second buffer tank gas inlet being connected to the gas outlet of the gas compression device; a liquid storage device having a liquid inlet and a liquid outlet, the liquid inlet being connected to the gas outlet of the second buffer tank via a first return line, the liquid outlet being connected to the gas inlet of the second buffer tank via a second return line, the first return line being provided with a cooler for liquefying the gas output from the second buffer tank, and the second return line being provided with a heater for vaporizing the liquid output from the liquid storage device; The gas compression device includes multiple parallel compressors, the gas inlets of the multiple compressors are connected to the gas outlet of the first buffer tank, and the gas outlets of the multiple compressors are connected to the gas inlet of the second buffer tank. The pressure of the gas compressed by the compressors is 0.35MPa-0.8MPa. The liquid storage device includes multiple parallel liquid storage tanks, the liquid inlets of the multiple liquid storage tanks are connected to the gas outlet of the second buffer tank through the first reflux pipeline, and the liquid inlets of the multiple liquid storage tanks are connected to the gas inlet of the second buffer tank through the second reflux pipeline.

2. The gas supply system according to claim 1, wherein: The cooling medium of the cooler includes cooling water, the temperature of the cooling water is 20℃-30℃, The heating medium of the heater includes evaporated condensed water, and the temperature of the evaporated condensed water is 90°C-95°C.

3. A leaching system, characterized in that: The gas supply system comprises the gas according to any one of claims 1 to 2, wherein the gas comprises sulfur dioxide gas.

4. The leaching system according to claim 3, characterized in that Further including: A supply pipeline is provided with a gas flow valve, one end of which is connected to the gas outlet of the second buffer tank. The reaction device has a reaction device gas inlet, and the reaction device gas inlet is connected to the other end of the supply pipeline.

5. The leaching system according to claim 4, characterized in that A pressure reducing valve is provided at one end of the supply pipe connected to the gas outlet of the second buffer tank. The pressure of the sulfur dioxide gas after being reduced by the pressure reducing valve is 0.3 MPa-0.4 MPa.

6. The leaching system according to claim 5, characterized in that The reaction device comprises a plurality of reactors connected in series via a slurry pipeline, each reactor having a reactor gas inlet connected to an end of the supply pipeline away from the second buffer tank, and the gas flow valve on the supply pipeline corresponding to at least one reactor at the end of the slurry pipeline to which the slurry flows is closed; The pressure of the reactor is lower than the pressure of the sulfur dioxide gas after being decompressed by the pressure reducing valve.

7. The leaching system according to claim 3 or 4, characterized in that: The temperature of the sulfur dioxide gas after being compressed by the compressor is 90°C-130°C; The temperature of the sulfur dioxide liquid formed by the sulfur dioxide gas after being cooled by the cooler is 35°C-45°C; The temperature of the sulfur dioxide gas formed by vaporizing the sulfur dioxide liquid through the heater is 45° C.-60° C.

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