Oxygen pressure leaching adjusting tank and production method

Abstract

The invention discloses an oxygen pressure leaching adjusting tank and a production method. The oxygen pressure leaching adjusting tank comprises an adjusting tank body, an adjusting tank bracket and an adjusting tank cover, and the adjusting tank body adopts a liquid inlet and outlet mode of bottom inlet and top outlet; the production method comprises the steps that after zinc sulfide concentrate is subjected to oxygen pressure leaching and flash evaporation, leached ore pulp is fed into the adjusting tank body through the adjusting tank liquid inlet pipe, the leached ore pulp is discharged from bottom to top in the adjusting tank body through the first adjusting tank liquid outlet pipe, and during the period, a stirrer continuously stirs; the retention time of leached ore pulp in the adjusting tank body is 1.5-2.5 h, the pulp inlet temperature of a liquid inlet of the adjusting tank is controlled to be 120-125 DEG C, and the discharging temperature of a liquid outlet pipe of the first adjusting tank is controlled to be not higher than 95 DEG C. The method is used for temperature regulation and pressure reduction of the leached ore pulp solution after oxygen pressure leaching flash evaporation, a bottom-in and top-out leached liquid mode is adopted, the phenomenon of overflow is avoided, meanwhile, the retention time of leached ore pulp in the tank is prolonged, the cooling gradient is formed, sulfur crystals are promoted to grow and generate, and follow-up dense settling separation and sulfur flotation separation are facilitated.

Description

Technical Field

[0001] The invention belongs to the technical field of nonferrous metal hydrometallurgy, and in particular relates to an oxygen pressure leaching regulating tank and a production method. Background Art

[0002] The oxygen pressure leaching process of zinc sulfide concentrate is to place the zinc sulfide concentrate in an autoclave without roasting, fill it with oxygen, and add waste electrolyte under high temperature and high pressure conditions of 140~160℃ and 350~700kPa, so that the sulfide is directly converted into sulfate and elemental sulfur. This process overcomes the shortcomings of the traditional "roasting-leaching-electrodeposition" process, such as complexity, long process and sulfur dioxide flue gas pollution, and has the advantages of less environmental pollution, recovery of sulfur in the form of elemental sulfur, high zinc recovery rate and strong process adaptability.

[0003] The oxygen pressure leaching process includes material preparation, pressure leaching, flash adjustment and sulfur recovery. In the flash tank, the molten sulfur can be used to recover steam for production, and then the slurry will enter the cooling adjustment tank. The cooled slurry will be sent to the thickener for concentration, and the concentrated supernatant will be further processed for purification, electrolytic deposition and casting to produce electrolytic zinc, while the underflow will be transported to the sulfur recovery process. However, the leached slurry in the regulating tank of the traditional oxygen pressure leaching process often overflows and can only be discharged by direct pumping from the bottom of the regulating tank. Although the overflow phenomenon has been improved, the particle size of the sulfur concentrate is small and the sulfur content is low, which is not conducive to the subsequent thickening and clearing separation and sulfur flotation.

[0004] Therefore, it is very necessary to develop an oxygen pressure leaching adjustment tank and a production method that can avoid the bubbling phenomenon and increase the particle size and sulfur content of the sulfur concentrate. Summary of the invention

[0005] In order to solve the technical problems that the corresponding sulfur crystallization growth process in the oxygen pressure leaching adjustment process is too short, sulfur and slag materials are mixed, and the flotation process cannot be effectively separated, the first purpose of the present invention is to provide an oxygen pressure leaching adjustment tank.

[0006] The second object of the present invention is to provide a method for producing an oxygen pressure leaching adjustment tank.

[0007] The first object of the present invention is achieved in this way, comprising an adjusting tank body, an adjusting tank bracket is provided on the top of the adjusting tank body, an adjusting tank cover is provided on the adjusting tank bracket, an adjusting tank liquid inlet is provided at the bottom of one side of the adjusting tank body, and a bottom liquid drain port is provided at the bottom of the other side, the adjusting tank liquid inlet is connected to the adjusting tank liquid inlet pipe, and the adjusting tank liquid inlet pipe is provided with an adjusting tank inlet valve, the bottom liquid drain port is connected to the bottom liquid drain pipe, and the bottom liquid drain pipe is provided with a bottom drain valve, a first adjusting tank liquid outlet pipe and a second adjusting tank liquid outlet pipe are provided on the upper part of the section tank body, the second adjusting tank liquid outlet pipe is located below the first adjusting tank liquid outlet pipe, the vertical height difference between the first adjusting tank liquid outlet pipe and the adjusting tank liquid inlet is 10m~12m, the upper adjusting tank cover is provided with a feeding port, a stirring device interface, a thermometer and a liquid level gauge port, and a gas discharge pipe, the stirring device interface is connected with a stirrer, and the stirring part of the stirrer is located in the adjusting tank body, and the thermometer and the liquid level gauge port are connected with a thermometer and a liquid level gauge.

[0008] The regulating tank body can be made of stainless steel + carbon steel composite plate or stainless steel + lined with anti-corrosion bricks or ordinary steel + lined with anti-corrosion bricks.

[0009] Preferably, the inner diameter of the adjustment tank is 6.5m~7.5m.

[0010] Preferably, the distance between the first regulating tank liquid outlet pipe and the second regulating tank liquid outlet pipe is 30 cm to 50 cm.

[0011] The second object of the present invention is achieved in that the leached slurry after oxygen pressure leaching and flash evaporation of zinc sulfide concentrate is sent into the regulating tank body through the regulating tank liquid inlet pipe, and the leached slurry is discharged from the bottom to the top in the regulating tank body through the first regulating tank liquid outlet pipe, during which the agitator continuously stirs; the residence time of the leached slurry in the regulating tank body is 1.5h~2.5h, the slurry inlet temperature of the regulating tank liquid inlet is controlled at 120℃~125℃, and the discharge temperature of the first regulating tank liquid outlet pipe is controlled at no more than 95℃.

[0012] Preferably, the material discharged through the liquid outlet pipe of the first regulating tank directly enters the thickener in a gravity flow manner.

[0013] Compared with the prior art, the present invention has the following technical effects: 1. The present invention is used for temperature regulation and pressure reduction of the leached pulp solution after oxygen pressure leaching flash evaporation. It adopts the bottom-in-top-out leaching liquid method, which effectively prolongs the residence time of the leached pulp in the tank while avoiding the bubbling phenomenon, forms a temperature reduction gradient, and promotes the growth of sulfur crystals. The particle size can grow from 20μm to more than 50μm, which is beneficial to the subsequent dense sedimentation and clear separation and sulfur flotation effective separation.

[0014] 2. The liquid out of the oxygen pressure leaching regulating tank of the present invention directly enters the thickener by high-level gravity flow, without the need for a delivery pump and a matching delivery pipeline valve. This method not only reduces the site occupation area, reduces investment costs, but also saves production and operation costs.

[0015] 3. The present invention solves the problem of sulfur and slag materials being mixed during the oxygen pressure leaching adjustment process, and fully meets the conditions for the crystal growth of sulfur in non-ferrous metallurgical hydrometallurgy, so as to achieve the subsequent dense sedimentation separation and sulfur flotation effective separation. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Figure 1 It is a structural schematic diagram of the oxygen pressure leaching adjustment tank of the present invention; Figure 2 It is a schematic diagram of the structure of the adjustment slot cover; Figure 3 This is a microscopic photo of sulfur concentrate produced by the conventional method in Example 7; Figure 4 This is a microscopic photograph of the sulfur concentrate implemented according to the present invention in Example 7; In the figure: 1-adjusting tank body, 2-adjusting tank bracket, 3-adjusting tank cover, 4-adjusting tank liquid inlet, 5-bottom liquid drain port, 6-adjusting tank liquid inlet pipe, 7-adjusting tank inlet valve, 8-bottom liquid drain pipe, 9-bottom drain valve, 10-first adjusting tank liquid outlet pipe, 11-second adjusting tank liquid outlet pipe, 12-feeding port, 13-stirring device interface, 14-thermometer and liquid level gauge port, 15-gas discharge pipe, 16-stirrer. DETAILED DESCRIPTION

[0017] The present invention is further described below in conjunction with the embodiments and drawings, but the present invention is not limited in any way. Any changes or substitutions made based on the teachings of the present invention belong to the protection scope of the present invention.

[0018] Example 1 As attached Figure 1~Figure 2As shown, the oxygen pressure leaching regulating tank of this embodiment includes a regulating tank body 1, a regulating tank bracket 2 is provided on the top of the regulating tank body 1, and a regulating tank cover 3 is provided on the regulating tank bracket 2. A regulating tank liquid inlet 4 is provided at the bottom of one side of the regulating tank body 1, and a bottom liquid drain port 5 is provided at the bottom of the other side. The regulating tank liquid inlet 4 is connected to the regulating tank liquid inlet pipe 6, and the regulating tank liquid inlet pipe 6 is provided with a regulating tank inlet valve 7. The bottom liquid drain port 5 is connected to the bottom liquid drain pipe 8, and the bottom liquid drain pipe 8 is provided with a bottom drain valve 9. The upper part of the node tank body 1 is provided with a first regulating tank liquid outlet pipe 10 and a second regulating tank outlet pipe 11. Liquid pipe 11, the second regulating tank liquid outlet pipe 11 is located below the first regulating tank liquid outlet pipe 10, the vertical height difference between the first regulating tank liquid outlet pipe 10 and the regulating tank liquid inlet 4 is 10m, the upper regulating tank cover 3 is provided with a feeding port 12, a stirring device interface 13, a thermometer and a liquid level gauge port 14, and a gas exhaust pipe 15, the stirring device interface 13 is connected to a stirrer 16, and the stirring part of the stirrer 16 is located in the regulating tank body 1, and the thermometer and the liquid level gauge port 14 are connected to the thermometer and the liquid level gauge; the inner diameter of the regulating tank body 1 is 6.5m; the first regulating tank liquid outlet pipe 10 and the second regulating tank liquid outlet pipe 11 are 30cm apart.

[0019] Example 2 The oxygen pressure leaching adjustment tank of this embodiment is based on the embodiment 1, and the difference from the embodiment 1 is that the vertical height difference between the first adjustment tank outlet pipe 10 and the adjustment tank liquid inlet 4 is 12m, the inner diameter of the adjustment tank body 1 is 7.5m, and the distance between the first adjustment tank outlet pipe 10 and the second adjustment tank outlet pipe 11 is 50cm.

[0020] Example 3 The oxygen pressure leaching adjustment tank of this embodiment is based on the embodiment 1, and the difference from the embodiment 1 is that the vertical height difference between the first adjustment tank outlet pipe 10 and the adjustment tank liquid inlet 4 is 11m, the inner diameter of the adjustment tank body 1 is 7m, and the distance between the first adjustment tank outlet pipe 10 and the second adjustment tank outlet pipe 11 is 40cm.

[0021] Example 4 This embodiment is a production method of an oxygen pressure leaching adjusting tank in embodiment 1, wherein the zinc sulfide concentrate is oxygen pressure leached and flashed, and the leached slurry is fed into the adjusting tank body 1 through the adjusting tank liquid inlet pipe 6, and the leached slurry is discharged from bottom to top in the adjusting tank body 1 through the first adjusting tank liquid outlet pipe 10, during which the agitator 16 continuously stirs; the residence time of the leached slurry in the adjusting tank body 1 is 1.5h, the slurry inlet temperature of the adjusting tank liquid inlet 4 is controlled at 120°C, and the discharge temperature of the first adjusting tank liquid outlet pipe 10 is controlled at no more than 95°C.

[0022] Example 5 This embodiment is the production method of the oxygen pressure leaching adjusting tank of embodiment 2, except that the residence time of the leached slurry in the adjusting tank body 1 is 2.5 hours and the inlet slurry temperature is controlled at 125°C, the rest is the same as embodiment 4.

[0023] Example 6 This embodiment is the production method of the oxygen pressure leaching adjusting tank of embodiment 3, except that the residence time of the leached slurry in the adjusting tank body 1 is 2 hours and the inlet slurry temperature is controlled at 122.5°C, the rest is the same as embodiment 4.

[0024] Example 7 When the leached slurry produced by oxygen pressure leaching of a company is sent to the regulating tank, it often overflows. Later, it is discharged by direct pumping from the bottom of the regulating tank. Although the overflow phenomenon is improved, the solution residence time is less than the design value, resulting in a small particle size of the sulfur concentrate and a low sulfur content (attached Figure 3 ), the particle size is 23μm, and the sulfur content is 35%~40%; According to the oxygen pressure leaching adjustment tank of Example 2 and the production method of Example 5, sulfur crystals grew and grew, and the sulfur particle size grew from 20μm to more than 50μm, containing 60% to 65% sulfur. The micrograph is shown in the attached Figure 4 , to achieve the subsequent effective separation of dense sedimentation and sulfur flotation.

Claims

1. An oxygen pressure leaching adjustment tank, comprising an adjustment tank body (1), characterized in that The regulating tank body (1) is provided with a regulating tank bracket (2) on the top, and a regulating tank cover (3) is provided on the regulating tank bracket (2). The bottom of one side of the regulating tank body (1) is provided with a regulating tank liquid inlet (4), and the bottom of the other side is provided with a bottom liquid drain (5). The regulating tank liquid inlet (4) is connected to a regulating tank liquid inlet pipe (6), and the regulating tank liquid inlet pipe (6) is provided with a regulating tank inlet valve (7). The bottom liquid drain (5) is connected to a bottom liquid drain pipe (8), and the bottom liquid drain pipe (8) is provided with a bottom drain valve (9). The upper part of the section tank body (1) is provided with a first regulating tank liquid outlet pipe (1 0), a second regulating tank liquid outlet pipe (11), the second regulating tank liquid outlet pipe (11) is located below the first regulating tank liquid outlet pipe (10), the vertical height difference between the first regulating tank liquid outlet pipe (10) and the regulating tank liquid inlet (4) is 10m~12m, the upper regulating tank cover (3) is provided with a feed port (12), a stirring device interface (13), a thermometer and a liquid level gauge port (14), and a gas discharge pipe (15), the stirring device interface (13) is connected to a stirrer (16), and the stirring part of the stirrer (16) is located in the regulating tank body (1), and the thermometer and the liquid level gauge port (14) are connected to a thermometer and a liquid level gauge.

2. The oxygen pressure leaching adjustment tank according to claim 1, characterized in that The inner diameter of the regulating tank body (1) is 6.5 m to 7.5 m.

3. The oxygen pressure leaching adjustment tank according to claim 1, characterized in that The distance between the first regulating tank liquid outlet pipe (10) and the second regulating tank liquid outlet pipe (11) is 30 cm to 50 cm.

4. A method for producing an oxygen pressure leaching adjustment tank according to any one of claims 1 to 3, characterized in that The zinc sulfide concentrate is oxygen-pressure leached and flash-evaporated to obtain a leached slurry which is fed into the regulating tank body (1) through the regulating tank liquid inlet pipe (6). The leached slurry flows from bottom to top in the regulating tank body (1) and is discharged through the first regulating tank liquid outlet pipe (10), during which the agitator (16) continuously stirs the leached slurry. The residence time of the leached slurry in the regulating tank body (1) is 1.5 hours to 2.5 hours. The slurry inlet temperature at the regulating tank liquid inlet (4) is controlled at 120° C. to 125° C., and the discharge temperature at the first regulating tank liquid outlet pipe (10) is controlled at no more than 95° C.

5. The oxygen pressure leaching adjustment tank according to claim 4, characterized in that The material discharged through the liquid outlet pipe (10) of the first regulating tank directly enters the thickener in a gravity flow manner.

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