Oxygen pressure leaching system
By introducing a connecting main pipe and branch pipes into the oxygen pressure leaching system, and using the supernatant to reduce the temperature of the discharge pipe and reactor, the problems of long oxygen pressure leaching process time and nickel sulfate precipitation were solved, thus shortening the reaction time and protecting the equipment.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- MORIMATSU (JIANGSU) HEAVY IND CO LTD
- Filing Date
- 2025-06-04
- Publication Date
- 2026-05-26
AI Technical Summary
The existing oxygen pressure leaching process takes a long time. Increasing the leaching temperature will cause nickel sulfate to precipitate in large quantities in the discharge pipe in crystal form, causing the flash valve to be eroded and damaged.
By introducing a connecting main pipe into the oxygen pressure leaching system, the supernatant from the solid-liquid separation mechanism enters the discharge pipe. The low temperature characteristics of the supernatant are used to reduce the material temperature in the discharge pipe. The supernatant is then returned to the reactor through a connecting branch pipe, which reduces the material temperature at the reactor outlet and prevents precipitation in the discharge pipe.
It effectively shortens reaction time, prevents nickel sulfate precipitation in the discharge pipe, extends equipment life, increases reactor temperature and pressure, and prevents combustion.
Smart Images
Figure CN224280391U_ABST
Abstract
Description
Technical Field
[0001] This utility model relates to the field of nickel hydrometallurgical technology, and in particular to an oxygen pressure leaching system. Background Technology
[0002] Nickel in nickel sulfide ore and high-grade nickel matte extracted from laterite exists in the form of nickel sulfide. In order to produce nickel sulfate, a leaching process is required. Atmospheric pressure leaching has a very low nickel leaching rate, so oxygen pressure leaching is required under high temperature and high pressure. Increasing the operating temperature will accelerate the leaching rate.
[0003] Current oxygen pressure leaching processes operate at temperatures between 150 and 180 degrees Celsius and typically require a reaction time of 4 to 10 hours. The relatively low temperature results in a longer leaching process time.
[0004] However, if the temperature in the discharge pipe exceeds 180 degrees Celsius, the solubility of nickel sulfate will drop sharply, causing a large amount of nickel sulfate to precipitate in the form of crystals in the discharge pipe, resulting in premature flash evaporation. This will cause the discharge pipe and flash valve to be eroded and damaged. Utility Model Content
[0005] The purpose of this invention is to provide an oxygen pressure leaching system to alleviate the technical problems in the prior art, such as the long oxygen pressure leaching process time and the fact that increasing the leaching temperature would cause a large amount of nickel sulfate to precipitate in the discharge pipe in the form of crystals, resulting in premature flash evaporation.
[0006] In a first aspect, the oxygen pressure leaching system provided by this utility model includes: a reaction vessel, a discharge pipeline, a solid-liquid separation mechanism, and a connecting main pipe;
[0007] The discharge pipeline is connected to the reactor and the solid-liquid separation mechanism respectively. The discharge pipeline is used to transport the material in the reactor to the solid-liquid separation mechanism. The solid-liquid separation mechanism is used to separate the solid and liquid of the material discharged from the reactor to form a supernatant.
[0008] The main connecting pipe is connected to the solid-liquid separation mechanism and the discharge pipeline, respectively. The main connecting pipe is used to transport the supernatant in the solid-liquid separation mechanism to the discharge pipeline.
[0009] In an optional implementation,
[0010] The oxygen pressure leaching system also includes connecting branch pipes;
[0011] The connecting branch pipe is connected to the connecting main pipe and the reaction vessel respectively, and the connecting branch pipe is used to transport the supernatant in the connecting main pipe to the reaction vessel.
[0012] In an optional implementation,
[0013] The reactor has multiple reaction chambers, which are arranged sequentially at intervals along the material flow direction inside the reactor.
[0014] Both the connecting branch pipe and the discharge pipe are connected to the reaction chamber located at the downstream end along the material flow direction inside the reactor.
[0015] In an optional implementation,
[0016] The solid-liquid separation mechanism includes a flash evaporation device;
[0017] The end of the discharge pipeline away from the reactor is connected to the flash evaporation device, which is used to reduce the temperature and pressure of the material.
[0018] In an optional implementation,
[0019] The solid-liquid separation mechanism also includes a buffer device;
[0020] The oxygen pressure leaching system also includes a first feed pipe;
[0021] The first conveying pipe is connected to the inlet of the buffer device and the outlet of the flash evaporation device.
[0022] In an optional implementation,
[0023] The solid-liquid separation mechanism also includes a thickening device;
[0024] The thickening device is used for solid-liquid separation of the material to form a supernatant and a waste residue;
[0025] The end of the main connecting pipe furthest from the discharge pipe extends into the thickening device.
[0026] In an optional implementation,
[0027] The oxygen pressure leaching system also includes a second feed pipe;
[0028] The second feed pipe is connected to both the thickening device and the buffer device.
[0029] In an optional implementation,
[0030] The thickening device is equipped with a slag discharge pipe for discharging waste residue.
[0031] In an optional implementation,
[0032] The end of the discharge pipe away from the solid-liquid separation mechanism extends into the reaction vessel.
[0033] In an optional implementation,
[0034] The reaction temperature of the reactor is 200°C to 210°C.
[0035] The oxygen pressure leaching system provided by this utility model connects the solid-liquid separation mechanism and the discharge pipeline through a connecting main pipe. The supernatant separated in the solid-liquid separation mechanism can enter the discharge pipeline through the connecting main pipe. Since the temperature of the supernatant is lower than that of the material in the discharge pipeline, the supernatant can reduce the temperature of the material in the discharge pipeline after entering the discharge pipeline, thus preventing the material temperature in the discharge pipeline from being too high and causing a large amount of nickel sulfate to precipitate in the form of crystals in the discharge pipeline. This can increase the reaction temperature of the reactor, thereby reducing the reaction time and alleviating the technical problems of the existing oxygen pressure leaching process being too long and the increased leaching temperature causing a large amount of nickel sulfate to precipitate in the form of crystals in the discharge pipeline, resulting in premature flash evaporation. Attached Figure Description
[0036] To more clearly illustrate the specific embodiments of this utility model or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this utility model. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.
[0037] Figure 1 This is a schematic diagram of the overall structure of the oxygen pressure leaching system provided in an embodiment of the present invention.
[0038] Icons: 100-Reaction vessel; 110-Reaction chamber; 200-Discharge pipeline; 300-Solid-liquid separation mechanism; 310-Flash evaporator; 311-First feed pipe; 320-Buffer device; 321-Second feed pipe; 330-Thickening device; 331-Slag discharge pipe; 400-Main connecting pipe; 500-Branch connecting pipe. Detailed Implementation
[0039] The technical solution of this utility model will now be clearly and completely described with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of this utility model. Based on the embodiments of this utility model, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this utility model.
[0040] In the description of this utility model, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," etc., indicating the orientation or positional relationship, are based on the orientation or positional relationship shown in the accompanying drawings and are only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this utility model. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.
[0041] In the description of this utility model, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "joining" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model according to the specific circumstances.
[0042] The specific embodiments of this utility model will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for illustration and explanation only and are not intended to limit the scope of this utility model.
[0043] like Figure 1 As shown, the oxygen pressure leaching system provided in this embodiment includes: a reactor 100, a discharge pipe 200, a solid-liquid separation mechanism 300, and a connecting main pipe 400; one end of the discharge pipe 200 is connected to the reactor 100, and the other end of the discharge pipe 200 is connected to the solid-liquid separation mechanism 300, thereby connecting the reactor 100 and the solid-liquid separation mechanism 300 through the discharge pipe 200, so as to transport the material in the reactor 100 to the solid-liquid separation mechanism 300.
[0044] The solid-liquid separation unit 300 is used to separate the solid and liquid of the material discharged from the reactor 100. After solid-liquid separation, a supernatant is formed, and a solid residue is formed at the bottom of the supernatant.
[0045] One end of the main connecting pipe 400 is connected to the solid-liquid separation mechanism 300, and the other end of the main connecting pipe 400 is connected to the discharge pipe 200. The connection between the solid-liquid separation mechanism 300 and the discharge pipe 200 is achieved through the main connecting pipe 400, so as to transport the supernatant in the solid-liquid separation mechanism 300 to the discharge pipe 200.
[0046] The oxygen pressure leaching system provided in this embodiment connects the solid-liquid separation mechanism 300 and the discharge pipe 200 through the connecting main pipe 400. The supernatant separated in the solid-liquid separation mechanism 300 can enter the discharge pipe 200 through the connecting main pipe 400. Since the supernatant is formed after solid-liquid separation, its temperature is lower than that of the material in the discharge pipe 200. After the supernatant enters the discharge pipe, it can reduce the temperature of the material in the discharge pipe 200, avoiding excessively high material temperature in the discharge pipe 200, which would cause nickel sulfate to precipitate in large quantities in the form of crystals in the discharge pipe 200. This can increase the reaction temperature of the reactor 100 to 200-210 degrees Celsius, thereby reducing the reaction time and alleviating the technical problems of the prior art where the oxygen pressure leaching process is too long and increasing the leaching temperature will cause a large amount of nickel sulfate to precipitate in the form of crystals in the discharge pipe, resulting in premature flash evaporation.
[0047] Based on the above embodiments, in an optional embodiment, the oxygen pressure leaching system provided in this embodiment further includes a connecting branch pipe 500; one end of the connecting branch pipe 500 is connected to the connecting main pipe 400, and the other end of the connecting branch pipe 500 is connected to the reactor 100, so as to transport the supernatant in the connecting main pipe 400 to the reactor 100. It should be noted that the connection position between the connecting branch pipe 500 and the reactor 100 is located at the discharge end inside the reactor 100, so that the supernatant can enter the discharge end inside the reactor 100, effectively reducing the material temperature at the discharge end inside the reactor 100, thereby reducing the material temperature entering the discharge pipe 200 and preventing the material from precipitating in the discharge pipe 200.
[0048] Furthermore, in order to pressurize the material, the reactor 100 is specifically configured as a pressurized reactor. The reactor 100 has multiple reaction chambers 110, which are arranged sequentially at intervals along the material flow direction inside the reactor 100. The connecting branch pipe 500 and the discharge pipe 200 are both connected to the reaction chamber 110 located at the downstream end along the material flow direction inside the reactor 100.
[0049] Regarding the structure of reactor 100, specifically:
[0050] The reactor 100 is equipped with a feed pipe and multiple partitions are arranged sequentially and at intervals along the material flow direction. These partitions divide the internal space of the reactor 100 into multiple reaction chambers 110. The feed pipe is positioned in the upstream front reaction chamber 110 along the material flow direction within the reactor 100, allowing the material entering from the feed pipe to flow sequentially along the multiple reaction chambers 110 within the reactor 100. The height of the partitions is lower than the height of the internal space of the reactor 100, creating a certain gap between the top of the partitions and the top surface of the reactor 100. The material in the reaction chamber 110 flows into the next reaction chamber 110 through the gaps in the top overflow manner.
[0051] Regarding the structure of the solid-liquid separation mechanism 300, specifically:
[0052] The solid-liquid separation mechanism 300 includes a flash evaporation device 310; the end of the discharge pipe 200 away from the reactor 100 is connected to the flash evaporation device 310. The flash evaporation device 310 is used to reduce the temperature and pressure of the material. The flash evaporation device 310 is specifically configured as a flash tank. The high-temperature and high-pressure material in the reactor 100 is transported to the flash evaporation device 310 through the discharge pipe 200. The high-temperature and high-pressure liquid enters the low-pressure environment in the flash evaporation device 310 and is rapidly cooled and depressurized.
[0053] In an optional embodiment, the solid-liquid separation mechanism 300 further includes a buffer device 320; the oxygen pressure leaching system further includes a first feed pipe 311; one end of the first feed pipe 311 is connected to the feed inlet of the buffer device 320, and the other end of the first feed pipe 311 is connected to the discharge outlet of the flash evaporation device 310. The buffer device 320 is specifically a flash evaporation sealing tank. The material after flash evaporation by the flash evaporation device 310 enters the flash evaporation sealing tank. The flash evaporation sealing tank plays a buffering role, so that the material after pressure reduction and temperature reduction can be stable in the flash evaporation sealing tank for subsequent solid-liquid separation.
[0054] In an optional embodiment, the solid-liquid separation mechanism 300 further includes a thickening device 330; the thickening device 330 is capable of solid-liquid separation of the material after cooling and depressurization by the flash evaporator 310 to form a supernatant and a waste residue; the end of the connecting main pipe 400 away from the discharge pipe 200 extends into the thickening device 330. It should be noted that the position of the connecting main pipe 400 extending into the thickening device 330 should be in the supernatant and should not extend into the waste residue layer, so that the supernatant in the thickening device 330 can enter the connecting main pipe 400. The connecting main pipe 400 transports the supernatant to the discharge pipe 200 and the connecting branch pipe 500, thereby cooling the material in the discharge pipe 200 and the material in the reactor 100.
[0055] It should be noted that the thickening device 330 can be directly connected to the flash evaporator 310. The material in the flash evaporator 310 enters the thickening device 330 and remains still for a period of time to allow the material to stabilize before the thickening device 330 is started to separate the solid and liquid materials. Alternatively, a second conveying pipe 321 can be provided. The second conveying pipe 321 is connected to both the thickening device 330 and the buffer device 320. The material after being buffered by the buffer device 320 enters the thickening device 330 through the second conveying pipe 321. Since the material has already been buffered by the buffer device 320, the thickening device 330 can be directly started to separate the solid and liquid materials.
[0056] In an optional embodiment, the thickening device 330 is further provided with a slag discharge pipe 331, which is connected to the bottom of the thickening device 330, and the waste residue in the thickening device 330 is discharged through the slag discharge pipe 331.
[0057] In an optional embodiment, the end of the discharge pipe 200 away from the solid-liquid separation mechanism 300 extends into the reactor 100 and comes into contact with the material. Even if the liquid level inside the reactor 100 fluctuates, it will not interfere with the material flow in the discharge pipe 200. This is because the pipe extends into the material and is always in the liquid phase region, ensuring the continuity and stability of the material flow.
[0058] The oxygen pressure leaching system provided in this embodiment has the following technical advantages:
[0059] 1. By setting up the main pipe 400, the supernatant formed after solid-liquid separation in the thickening device 330 is transported to the discharge pipe 200, thereby reducing the material temperature in the discharge pipe 200 and effectively avoiding the precipitation of material in the discharge pipe 200 due to the increase in the reaction temperature of the reactor 100.
[0060] 2. By setting up the connecting branch pipe 500, the supernatant formed after solid-liquid separation in the thickening device 330 is transported to the reaction chamber 110 in the reactor 100, which is connected to the discharge pipe 200. This reduces the material in the reaction chamber 110 connected to the discharge pipe 200, thereby reducing the temperature of the material when it enters the discharge pipe 200 and further preventing the material from precipitating in the discharge pipe 200.
[0061] 3. Since the material will not precipitate in the discharge pipe 200, the operating temperature of the reactor 100 can be increased, the reaction rate can be accelerated, and the reaction time can be shortened.
[0062] 4. As the temperature of the reactor 100 increases, the pressure inside the reactor 100 increases, thereby reducing the pressure of oxygen injected into the reactor 100, thus preventing the materials in the reactor 100 from burning due to excessive oxygen pressure.
[0063] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this utility model, and are not intended to limit it. Although the utility model has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of this utility model.
Claims
1. An oxygen pressure leaching system characterised in that, include: The reactor (100), discharge pipeline (200), solid-liquid separation mechanism (300) and connecting main pipe (400); The discharge pipe (200) is connected to the reactor (100) and the solid-liquid separation mechanism (300) respectively. The discharge pipe (200) is used to transport the material in the reactor (100) to the solid-liquid separation mechanism (300). The solid-liquid separation mechanism (300) is used to separate the solid and liquid of the material discharged from the reactor (100) to form a supernatant. The main connecting pipe (400) is connected to the solid-liquid separation mechanism (300) and the discharge pipe (200) respectively. The main connecting pipe (400) is used to transport the supernatant in the solid-liquid separation mechanism (300) to the discharge pipe (200).
2. The oxygen pressure leaching system according to claim 1, characterized in that, The oxygen pressure leaching system also includes a connecting branch pipe (500); The connecting branch pipe (500) is connected to the connecting main pipe (400) and the reaction vessel (100) respectively. The connecting branch pipe (500) is used to transport the supernatant in the connecting main pipe (400) to the reaction vessel (100).
3. The oxygen pressure leaching system according to claim 2, characterized in that, The reactor (100) has multiple reaction chambers (110), which are arranged sequentially at intervals along the material flow direction inside the reactor (100); Both the connecting branch pipe (500) and the discharge pipe (200) are connected to the reaction chamber (110) located at the downstream end along the material flow direction inside the reactor (100).
4. The oxygen pressure leaching system according to any one of claims 1-3, characterized in that, The solid-liquid separation mechanism (300) includes a flash evaporation device (310); The end of the discharge pipeline (200) away from the reactor (100) is connected to the flash evaporation device (310), which is used to reduce the temperature and pressure of the material.
5. The oxygen pressure leaching system according to claim 4, characterized in that, The solid-liquid separation mechanism (300) also includes a buffer device (320); The oxygen pressure leaching system also includes a first feed pipe (311); The first conveying pipe (311) is connected to the inlet of the buffer device (320) and the outlet of the flash evaporator (310), respectively.
6. The oxygen pressure leaching system according to claim 5, characterized in that, The solid-liquid separation mechanism (300) also includes a thickening device (330); The thickening device (330) is used for solid-liquid separation of the material to form a supernatant and a waste residue; The end of the main connecting pipe (400) away from the discharge pipe (200) extends into the thickening device (330).
7. The oxygen pressure leaching system according to claim 6, characterized in that, The oxygen pressure leaching system also includes a second feed pipe (321); The second feed pipe (321) is connected to the thickening device (330) and the buffer device (320) respectively.
8. The oxygen pressure leaching system according to claim 6, characterized in that, The thickening device (330) is equipped with a slag discharge pipe (331) for discharging waste residue.
9. The oxygen pressure leaching system according to claim 1, characterized in that, The end of the discharge pipe (200) away from the solid-liquid separation mechanism (300) extends into the reaction vessel (100).
10. The oxygen pressure leaching system according to claim 1, characterized in that, The reaction temperature of the reactor is 200°C to 210°C.