Optimization method of zinc sulfide concentrate autoclave

Abstract

The invention relates to an optimization method of a zinc sulfide concentrate autoclave, the optimization method is used for a zinc sulfide concentrate autoclave system, the zinc sulfide concentrate autoclave system comprises a jarosite slag input pipeline and a waste liquid pipeline, and the optimization method comprises the following steps: introducing mixed ore pulp of zinc sulfide concentrate and jarosite slag into a first chamber of the autoclave; waste liquid is introduced into the first chamber, the second chamber, the third chamber and the fourth chamber of the autoclave, sulfuric acid is further introduced into the first chamber, and scrap iron is added for soaking after the waste liquid is settled through electrolytic waste liquid; and adding the jarosite slag into a fifth chamber of the autoclave. The optimization method optimizes the switching mode of the acid liquid pressure pump, operation of the pressure pump does not need to be stopped during fault switching of the pressure pump, anode mud deposits on the inner wall of a coil pipe are cleaned, the operation condition of the autoclave is stabilized, the operation risk of the autoclave is reduced, the stable operation period of the autoclave is prolonged, and the control technical advantage of the zinc autoclave is well converted into the economic advantage. And the economic benefit and the safety benefit of an enterprise are obviously improved.

Description

Technical Field

[0001] The present application relates to the technical field of pressure leaching process, and in particular to an optimization method and system for a zinc sulfide concentrate pressure autoclave. Background Art

[0002] In the traditional process, the three unit operations of zinc concentrate roasting, spent electrolyte leaching roasted sand and sulfuric acid generation are gradually replaced by the unit operations of zinc sulfide concentrate pressure leaching process as the pressure leaching process becomes more mature.

[0003] The main device used in the pressure leaching process is the pressure kettle. The following problems exist in the current use of the pressure kettle: due to the high iron and sulfur content in the zinc sulfide concentrate, the treatment process is easy to wrap and agglomerate, the treatment difficulty increases, and the operation risk of the pressure kettle increases; the acid pressure pump failure switching takes a long time and the operation is complicated. Each time the pressure kettle is switched, the pressure kettle is stuffy for more than 40 minutes, which seriously affects the stable operation of the pressure kettle; during the electrolysis process, due to the presence of manganese ions, a large amount of anode mud will be precipitated on the anode, especially when the plate is replaced and the new anode plate is put into use in large quantities, the amount of anode mud in the electrolytic waste liquid increases and becomes more turbid. After the electrolytic waste liquid enters the preheating coil and the external heat exchanger of the pressure kettle 3-4 chamber, the anode mud will be deposited on the inner wall of the coil to form a pipe blockage, which will reduce the heat exchange flow of the waste liquid in the pressure kettle heat exchange coil and increase the pressure of the pressure pump, which has a greater operation risk.

[0004] As the service life of pressure leaching process equipment increases, the average annual operation cycle of the pressure autoclave shortens, resulting in increased equipment maintenance costs and increased labor intensity. Appropriate measures need to be taken to optimize the pressure leaching process, reduce equipment failure rate and maintenance costs, and increase the operation time of the pressure autoclave to reduce safety risks. Summary of the invention

[0005] In order to solve or partially solve the problems existing in the related art, the present application provides an optimization method for a zinc sulfide concentrate pressure kettle, which realizes the dynamic switching of the pressure pump, cleans the anode mud deposits on the inner wall of the coil, and stabilizes the operating condition of the pressure kettle.

[0006] In a first aspect, the present application provides an optimization method for a zinc sulfide concentrate pressure autoclave, which is used for a zinc sulfide concentrate pressure autoclave system. The zinc sulfide concentrate pressure autoclave system comprises a filter press discharge pipe, a ball mill, a pressure autoclave with five chambers, an electrolytic circulation tank and a waste liquid tank, wherein the filter press discharge pipe, the ball mill and the fifth chamber of the pressure autoclave are connected through an additional iron alum slag input pipeline, so that the iron alum slag enters the ball mill and the fifth chamber of the pressure autoclave through the iron alum slag input pipeline respectively, thereby mixing with the zinc sulfide concentrate in the ball mill and performing secondary leaching on the iron alum slag in the fifth chamber of the pressure autoclave; one side of the electrolytic circulation tank is connected to the pressure autoclave, and the other side is connected to the waste liquid tank through the additional waste liquid pipeline, and a sedimentation system is provided in the electrolytic circulation tank; the optimization method comprises the following steps:

[0007] A mixed slurry of zinc sulfide concentrate and iron alum slag is introduced into the first chamber of the autoclave, wherein the ratio of zinc sulfide concentrate to iron alum slag is 0.5:1, and the mass concentration of the mixed slurry is 1.20-1.35 mg / l;

[0008] And, waste liquid is introduced into the first to fourth chambers of the autoclave, sulfuric acid is also introduced into the first chamber, and iron filings are added for immersion after the waste liquid is precipitated by electrolysis;

[0009] Add iron alum slag into the fifth chamber of the autoclave, the leaching liquid-solid ratio of the autoclave is 3.6-4.2:1, and the acidity of the fourth chamber of the autoclave is 28-35 g / L.

[0010] Among them, the iron filings make the concentration of ferrous ions in the waste liquid not less than 0.2g / L.

[0011] Among them, the amount of iron alum slag added is 15m 3 / sky.

[0012] Among them, the zinc sulfide concentrate pressure kettle system also includes a pressure pump pipeline, the pressure pump pipeline includes a first pressure pump outlet pipeline, a second pressure pump outlet pipeline, a heat exchanger connecting pipeline, and a three-way pipeline. The first pressure pump outlet pipeline and the second pressure pump outlet pipeline are respectively connected to the heat exchanger connecting pipeline and the connecting port is located on the front side of the flow meter. The first pressure pump outlet pipeline and the second pressure pump outlet pipeline are connected based on the three-way pipeline. The three-way pipeline is also connected to the heat exchanger connecting pipeline at the front end of the flow meter. Two stop valves are respectively installed on the first pressure pump outlet pipeline and the second pressure pump outlet pipeline.

[0013] The zinc sulfide concentrate autoclave system further comprises a displacement pipeline, the displacement liquid inlet is arranged in the third chamber of the autoclave, and the displacement liquid inlet and the supernatant liquid are connected through the displacement pipeline to supply the displacement pipeline so that the temperature of the third chamber of the autoclave is less than 140°C.

[0014] Among them, in the zinc sulfide concentrate autoclave system, the feeding temperature of the first chamber of the autoclave is higher than 115°C.

[0015] Among them, in the zinc sulfide concentrate autoclave system, the heat exchange temperature of the heat exchanger connecting pipe is less than 100°C.

[0016] The technical solution provided by this application may have the following beneficial effects:

[0017] The present application provides an optimization method for a zinc sulfide concentrate pressure kettle, optimizes the switching mode of an acid pressure pump, realizes switching when a pressure pump fails without stopping the pressure pump, cleans anode mud deposits on the inner wall of a coil, stabilizes the operating condition of the pressure kettle, reduces the operating risk of the pressure kettle, and extends the stable operation period of the pressure kettle, so that the control technology advantages of the zinc pressure kettle are well converted into economic advantages, and the economic and safety benefits of the enterprise are significantly improved.

[0018] It should be understood that the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the present application. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] The above and other objects, features and advantages of the present application will become more apparent through a more detailed description of exemplary embodiments of the present application in conjunction with the accompanying drawings, wherein the same reference numerals generally represent the same components in the exemplary embodiments of the present application.

[0020] Figure 1 It is a schematic flow chart showing a method for optimizing a zinc sulfide concentrate autoclave according to an embodiment of the present application. DETAILED DESCRIPTION

[0021] The embodiments of the present application will be described in more detail below with reference to the accompanying drawings. Although the embodiments of the present application are shown in the accompanying drawings, it should be understood that the present application can be implemented in various forms and should not be limited by the embodiments described herein. On the contrary, these embodiments are provided to make the present application more thorough and complete, and to fully convey the scope of the present application to those skilled in the art.

[0022] It should be understood that although the terms "first", "second", "third", etc. may be used in this application to describe various information, this information should not be limited to these terms. These terms are only used to distinguish the same type of information from each other. For example, without departing from the scope of this application, the first information may also be referred to as the second information, and similarly, the second information may also be referred to as the first information. Thus, the features defined as "first" and "second" may explicitly or implicitly include one or more of the features. In the description of this application, the meaning of "multiple" is two or more, unless otherwise clearly and specifically defined.

[0023] In the description of the present application, it should be understood that the terms "length", "width", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", etc., indicating the orientation or position relationship, are based on the orientation or position relationship shown in the drawings, and are only for the convenience of describing the present application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as a limitation on the present application.

[0024] Unless otherwise clearly specified and limited, the terms "installed", "connected", "connected", "fixed" and the like should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements. For ordinary technicians in this field, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0025] The technical solution of the embodiments of the present application is described in detail below with reference to the accompanying drawings.

[0026] The unit operation of the zinc sulfide concentrate pressure leaching process replaces the three unit operations of zinc concentrate roasting, spent electrolyte leaching roasted sand and sulfuric acid generation in the traditional process. The main chemical reactions of pressure leaching are as follows:

[0027] 2ZnS+2H2SO4+O2→2ZnSO4+2H2O+2S0 (1)

[0028] This reaction consists of the following four steps:

[0029] Step 1: Acid decomposition of zinc and iron sulfides

[0030] FeS+H2SO4→FeSO4+H2S (2)

[0031] ZnS+H2SO4→ZnSO4+H2S (3)

[0032] Step 2: Ferrous sulfate is oxidized to ferric sulfate

[0033] 4FeSO4+2H2SO4+O2→2Fe2(SO4)3+2H2O (4)

[0034] Step 3: Ferric sulfate oxidizes H2S to elemental sulfur

[0035] Fe2(SO4)3+H2S→2FeSO4+H2SO4+S0 (5)

[0036] When the oxygen partial pressure is high enough, the second step is the key step of the leaching reaction.

[0037] Step 4: After the three reactions above reach equilibrium quickly, the concentration of iron in the solution remains constant, and zinc dissolves at a constant rate. In the absence of a carrier that can transfer oxygen, reaction (1) actually reacts very slowly. When iron dissolves, the following reactions occur:

[0038] ZnS+Fe2(SO4)3→ZnSO4+2FeSO4+S0 (6)

[0039] 4FeSO4+2H2SO4+O2→2Fe2(SO4)3+2H2O (7)

[0040] When leaching zinc concentrate under pressure, iron in sphalerite, pyrrhotite and pyrite may be dissolved. Under high pressure and temperature conditions, pyrite may undergo the following reactions:

[0041] 2FeS2+7.5O2+H2O→Fe2(SO4)3+H2SO4 (8)

[0042] 2FeS2+7.5O2+4H2O→Fe2O3+4H2SO4 (9)

[0043] The iron element in the zinc sulfide concentrate partially dissolves into the zinc sulfate solution under high temperature and strong oxidation. The iron ions become a substance that transfers oxygen to zinc sulfide, which can promote the leaching reaction of zinc sulfide.

[0044] like Figure 1 The optimization method of a zinc sulfide concentrate autoclave is shown, which is used for a zinc sulfide concentrate autoclave system. The optimization method comprises the following steps:

[0045] S1. A mixed slurry of zinc sulfide concentrate and iron alum slag is introduced into the first chamber of the autoclave.

[0046] S2. Waste liquid is introduced into the first to fourth chambers of the autoclave, sulfuric acid is also introduced into the first chamber, and iron filings are added for immersion after the waste liquid is precipitated by electrolysis.

[0047] The amount of iron filings added is based on the concentration of ferrous ions in the acid solution being no less than 0.2 g / L.

[0048] The experiment found that direct circulating immersion of high-leaching supernatant containing high Fe3+ had no leaching effect on the anode mud deposited in the coil; after using sodium sulfite or iron to convert Fe3+ into Fe2+, the anode mud deposited in the coil can be leached without causing corrosion to the titanium coil.

[0049] Therefore, a large amount of iron filings are soaked in the waste liquid used in the oxygen pressure process to increase the iron content in the waste liquid. Secondly, iron filings are added to the waste liquid acid supply tank to increase the iron content of the acid entering the kettle, and the oxidized Fe3+ is reduced to Fe2+, thereby cleaning the heat exchange coil of the autoclave and the coil of the external heat exchanger.

[0050] After 48 hours of continuous treatment, the blockage of the heat exchange coils in the autoclave chambers 3 and 4 was eliminated, the flow rate of the preheating coils in the autoclave chambers 3 and 4 was increased to 7m3 / h, and the pressure of the booster pump dropped from 2.3Mpa to 1.8Mpa. After carrying out the experiment of cleaning the anode mud deposits on the inner wall of the coil, a method for cleaning the anode mud deposits on the inner wall of the coil was found.

[0051] S3. Add iron alum slag into the fifth chamber of the autoclave.

[0052] The ratio of zinc sulfide concentrate to iron alum slag is 0.5:1, and the mass concentration of the mixed slurry is 1.20-1.35 mg / l, which is convenient for controlling the temperature of the pressure kettle. Under the conditions of this ratio and slurry concentration, the sulfur content of the slurry entering the kettle reaches 20-25%, and the iron content reaches 7-10%. Under this reaction condition, it is conducive to the rapid release of the reaction heat of the zinc sulfide concentrate, so that the leaching solution temperature quickly reaches 130-165°C. The iron alum slag ensures that the leaching rate of the main metal zinc and other co-existing valuable metals reaches more than 98%, and the iron is precipitated into the slag phase as much as possible.

[0053] Under the above raw material ratio and the conditions of stable operation of the pressure autoclave and pressure pump, the liquid-solid ratio of the pressure autoclave leaching is controlled to be 3.6-4.2:1, and the acidity of the fourth chamber of the pressure autoclave is controlled to be 28-35g / L.

[0054] The zinc sulfide concentrate pressure kettle system includes an iron alum slag input pipeline, a waste liquid pipeline, a pressure pump pipeline, and a displacement pipeline.

[0055] The booster pump pipeline includes a first booster pump outlet pipeline, a second booster pump outlet pipeline, a heat exchanger connecting pipeline, and a three-way pipeline. The first booster pump outlet pipeline and the second booster pump outlet pipeline are respectively connected to the heat exchanger connecting pipeline and the connecting ports are located on the front side of the flow meter. The first booster pump outlet pipeline and the second booster pump outlet pipeline are connected based on the three-way pipeline. The three-way pipeline is also connected to the heat exchanger connecting pipeline at the front end of the flow meter. Two stop valves are respectively installed on the first booster pump outlet pipeline and the second booster pump outlet pipeline.

[0056] The specific transformation is: connect the outlet pipes of the original B18 pump and B19 pump in series with the heat exchanger connection pipes in front of the flow meter, install two DN50 titanium stop valves on each, and then use a three-way pipe to connect the flow meter. In this way, when the booster pump fails, it is not necessary to stop the booster pump operation or disassemble the flow meter. Just reduce the stroke of the faulty pump and start the standby pump, raise the pressure of the standby pump feed pipe to 0.05-0.15Mpa or more, then open the stop valve in front of the flow meter to complete the liquid supply, and then reduce the stroke of the faulty pump until the faulty pump stops, close the stop valve in front of the flow meter, and open the pressure relief valve of the faulty pump pipeline. In this way, the acid booster pump fault switching can be realized. This process completes the switching operation during the operation of the autoclave, shortens the fault handling time by more than 40 minutes each time, and improves the equipment operation efficiency.

[0057] The iron alum slag is put into the pipeline to maximize the operation of the autoclave in the wet process. The pipeline from the ball milling process to the original oxidation tank section of the oxygen pressure process is set up, so that the iron alum slag is connected in series from the normal pressure 9# working tank - ball mill - oxidation tank - fifth chamber equipment to form a complete production process chain. When part of the iron alum slag is added to the original ore, the excess iron alum slag is put into the fifth chamber to the maximum extent, and the high temperature, high acid, oxygen-rich and pressurized conditions are used to carry out secondary leaching of the iron alum slag, that is, to replace the original neutralizer water extraction slag, reduce the acid content of the oxygen pressure leaching solution, and control the leaching slurry temperature, thereby increasing the recovery rate of zinc metal in the iron alum slag. The amount of iron alum slag added is 15m 3 / sky.

[0058] The discharge pipe of the filter press is connected to the ball mill and the fifth chamber of the autoclave through the iron alum slag input pipeline, so that the iron alum slag enters the ball mill and the fifth chamber of the autoclave through the iron alum slag input pipeline respectively, thereby mixing with the zinc sulfide concentrate in the ball mill and performing secondary leaching on the iron alum slag in the fifth chamber of the autoclave.

[0059] The electrolytic circulation pool is connected to the waste liquid pool through a waste liquid pipeline. The electrolytic circulation pool is also connected to the pressure autoclave. A sedimentation system is set up in the electrolytic circulation pool. A pipeline is set up from the electrolytic circulation pool to the 3# waste liquid pool of the normal pressure process to achieve clean and dirty diversion of the electrolytic waste liquid. The waste liquid from the electrolytic circulation pool is supplied to the pressure autoclave after the first-level sedimentation using a new waste liquid pipe pump. The waste liquid from the electrolytic trough is supplied to the intermediate leaching and zinc oxide powder leaching through the original waste liquid chute, thereby minimizing the mud content of the electrolytic waste liquid, reducing the amount of anode mud brought into the coil in the autoclave from the source, and finding a way to improve the quality of the electrolytic waste liquid, effectively avoiding the risk of shutdown of the pressure autoclave and ensuring the smooth operation of the pressure autoclave.

[0060] The replacement fluid inlet is arranged in the third chamber of the autoclave, and the replacement fluid inlet and the supernatant are connected through a replacement pipe to supply the replacement pipe so that the temperature of the third chamber of the autoclave is less than 140°C.

[0061] Specific pipeline modification: Change the original secondary filtrate supply replacement pipeline to the supernatant supply replacement pipeline, use qualified supernatant to match water and waste liquid, and explore the best ratio. This can not only eliminate the risk of coil burning in the kettle caused by the replacement liquid entering the sulfide ore, but also quickly reduce the viscosity of the slurry in the kettle, ensuring the leaching effect of the slurry in the kettle during the replacement process.

[0062] Due to the large temperature difference between the inner and outer walls of the three-chamber preheating coil of the autoclave, coil wrapping often occurs, causing the current in the three chambers to increase, bringing risks to safe operation. If the replacement operation is carried out according to the original process, it will take too long, the feeding temperature will be too low, and it will take a long time to resume production. By installing the replacement fluid inlet of the three chambers of the autoclave, the original method of first injecting replacement fluid into one chamber to dilute the sulfur content and solution viscosity of the slurry in the autoclave, and then controlling the temperature of the three chambers below 140°C, is changed to directly pumping replacement fluid into the three chambers, stopping the entry of replacement fluid into one chamber, and locking the feeding temperature of one chamber above 115°C to ensure that production can be quickly resumed after feeding. Under this operating condition, explore the various operating technical conditions of the replacement operation, shorten the replacement operation time, and reduce or eliminate the impact of the autoclave replacement operation on the insufficient supply of preheating supernatant in the purification process.

[0063] The gas phase and liquid phase heat exchange coils in the autoclave have high operating temperatures, which poses operational risks. Therefore, the coil heat exchange temperature is strictly controlled to be less than 100°C. This measure ensures the smooth operation of the pressure pump, reduces equipment failure rate, and improves equipment productivity.

[0064] This method was put into production on September 1 of that year. After application, the average operation cycle of the autoclave reached 85.3 days / time. By June 26 of the following year, the production had been running normally for 341 days. The autoclave was maintained 4 times in total. The operation cycle was extended by 32.9 days / time compared with the average operation of 52.4 days / time before the project was launched. After implementation and application, the autoclave maintenance was reduced by 2.5 times. Each maintenance was calculated as 8 shifts, and the number of working days per year could be increased by 6.66 days. The autoclave processing capacity is calculated as 30 tons of metal per day, and the metal that can be added to the system is 6.66×30=199.8 tons.

[0065] The output of zinc ingots is 199.8×0.8×0.94×0.968=145.44 tons.

[0066] The profit per ton of metal is 23000-13501.88=9498.12 yuan.

[0067] The direct income after the implementation of the project will be 145.44×0.9498=1.3814 million yuan.

[0068] The dosage of iron alum slag in the fifth chamber of the autoclave is 15m3 / day, and the concentration is 1.0g / ml (the average zinc content of the iron alum slag from January to October of the same year is 9.62%, and the average zinc content of the oxygen pressure leaching slag is 4.43%). The additional metal that can be recovered every day is: 15×1.0×(9.62%-4.43%)=0.7785 tons of metal.

[0069] The amount of metal recovered from the slag after the project is applied is: 0.7785×341=267.69 tons.

[0070] The value of metals in the recovered slag is: 267.69×0.6646=1.7791 million yuan.

[0071] The direct income after the project is applied is: 138.14+177.91=3160500 yuan.

[0072] The economic benefits generated by the application of the method are: 316.05-30.65=285.40 million yuan

[0073] Finally, it should be noted that, in this article, relationships such as first and second, etc. are used only to distinguish one entity or operation from another entity or operation, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Moreover, the terms include, include or any other variations are intended to cover non-exclusive inclusion, so that a process, method, article or device that includes a series of elements includes not only those elements, but also other elements not explicitly listed, or also includes elements inherent to such process, method, article or device.

[0074] The units described as separate components may or may not be physically separated, and the components shown as units may or may not be physical units, that is, they may be located in one place or distributed on multiple network units. Some or all of the units may be selected according to actual needs to achieve the purpose of the solution of this embodiment.

[0075] The embodiments of the present application have been described above, and the above description is exemplary, not exhaustive, and is not limited to the disclosed embodiments. Many modifications and changes will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments. The selection of terms used herein is intended to best explain the principles of the embodiments, practical applications, or improvements to the technology in the market, or to enable other persons of ordinary skill in the art to understand the embodiments disclosed herein.

Claims

1. A method for optimizing a zinc sulfide concentrate autoclave, characterized in that: Used for a zinc sulfide concentrate pressure kettle system, the zinc sulfide concentrate pressure kettle system comprises a filter press discharge pipe, a ball mill, a pressure kettle with five chambers, an electrolytic circulation tank and a waste liquid tank, wherein the filter press discharge pipe, the ball mill and the fifth chamber of the pressure kettle are connected through an additional iron alum slag input pipeline, so that the iron alum slag enters the ball mill and the fifth chamber of the pressure kettle through the iron alum slag input pipeline respectively, thereby mixing with the zinc sulfide concentrate in the ball mill and performing secondary leaching on the iron alum slag in the fifth chamber of the pressure kettle; one side of the electrolytic circulation tank is connected to the pressure kettle, and the other side is connected to the waste liquid tank through the additional waste liquid pipeline, and a sedimentation system is provided in the electrolytic circulation tank; the optimization method comprises the following steps: A mixed slurry of zinc sulfide concentrate and iron alum slag is introduced into the first chamber of the autoclave, wherein the ratio of the zinc sulfide concentrate to the iron alum slag is 0.5:1, and the mass concentration of the mixed slurry is 1.20-1.35 mg / l; And, introducing waste liquid into the first to fourth chambers of the autoclave, sulfuric acid is also introduced into the first chamber, and iron filings are added to soak the waste liquid after the waste liquid is precipitated by electrolysis; Add iron alum slag into the fifth chamber of the autoclave, the leaching liquid-solid ratio of the autoclave is 3.6-4.2:1, and the acidity of the fourth chamber of the autoclave is 28-35 g / L.

2. The method for optimizing the zinc sulfide concentrate autoclave according to claim 1, characterized in that: The iron filings make the concentration of ferrous ions in the waste liquid not less than 0.2 g / L.

3. The method for optimizing the zinc sulfide concentrate autoclave according to claim 1, characterized in that: The amount of iron alum slag added is 15m 3 / sky.

4. The method for optimizing the zinc sulfide concentrate autoclave according to claim 1, characterized in that: The zinc sulfide concentrate pressure kettle system also includes a pressure pump pipeline, which includes a first pressure pump outlet pipeline, a second pressure pump outlet pipeline, a heat exchanger connecting pipeline, and a three-way pipeline. The first pressure pump outlet pipeline and the second pressure pump outlet pipeline are respectively connected to the heat exchanger connecting pipeline and the connecting port is located at the front side of the flow meter. The first pressure pump outlet pipeline and the second pressure pump outlet pipeline are connected based on the three-way pipeline, and the three-way pipeline is also connected to the heat exchanger connecting pipeline at the front end of the flow meter. Two stop valves are respectively installed on the first pressure pump outlet pipeline and the second pressure pump outlet pipeline.

5. The method for optimizing the zinc sulfide concentrate autoclave according to claim 1, characterized in that: The zinc sulfide concentrate autoclave system further comprises a displacement pipeline, a displacement liquid inlet is arranged in the third chamber of the autoclave, and the displacement liquid inlet and the supernatant liquid are connected through the displacement pipeline to make the temperature of the third chamber of the autoclave less than 140°C.

6. The method for optimizing the zinc sulfide concentrate autoclave according to claim 1, characterized in that: In the zinc sulfide concentrate autoclave system, the feeding temperature of the first chamber of the autoclave is higher than 115°C.

7. The method for optimizing the zinc sulfide concentrate autoclave according to claim 1, characterized in that: In the zinc sulfide concentrate autoclave system, the heat exchange temperature of the heat exchanger connecting pipe is less than 100°C.

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