System for preparing manganese monoxide from pyrolusite

Abstract

The utility model discloses a system for preparing manganese monoxide from pyrolusite. The system comprises a crushing and grinding device, a pyrolysis device, a hydrothermal reaction device, an oxidation reaction device and a reduction reaction device. The crushing and ore grinding device, the pyrolysis device, the hydrothermal reaction device, the oxidation reaction device and the reduction reaction device are sequentially arranged in series. The pyrolusite is subjected to pretreatment such as pyrolysis, hydrothermal reaction and oxidation reaction, manganous-manganic oxide and manganic oxide contained in the pyrolusite are efficiently converted into manganese dioxide at low cost, the quality of a manganese monoxide product subjected to follow-up fluidization reduction is improved, and a foundation is laid for follow-up efficient leaching of manganese. And carbon dioxide released in the pyrolusite fluidization reduction process is recycled to prepare CO capable of being recycled for reduction, carbon resources are utilized to the maximum extent, and carbon emission is greatly reduced. The device has the characteristics of simple structure, convenience in operation, small equipment investment, small occupied field and the like.

Description

Technical Field

[0001] The utility model relates to a manganese monoxide production and processing technology, in particular to a system for preparing manganese monoxide by using pyrolusite, and belongs to the technical field of manganese monoxide production and processing. Background Art

[0002] Manganese ore is one of the scarce resources in my country, and the existing resources are more poor than rich, with rich ore resources accounting for only 6.43%, and the impurity content of the resources is high. Therefore, it is necessary to make full use of the poor manganese oxide ore resources and improve the quality of manganese ore products. How to use these manganese oxide ore resources at low cost and high efficiency to provide high-quality raw materials for electrolytic manganese metal has become a bottleneck restricting the development of the manganese industry.

[0003] Pyrolusite is an important raw material for producing manganese sulfate. About 60% of manganese sulfate in the world is processed by pyrolusite. Pyrolusite is insoluble in sulfuric acid. It must be reduced to manganese monoxide (MnO) before it can react with sulfuric acid to produce manganese sulfate. The traditional process is to roast with coal as a reducing agent to convert MnO2 in pyrolusite into MnO, and then leach it with sulfuric acid. However, this method has the problems of high energy consumption, poor operating conditions, and serious environmental pollution. The two-ore roasting method also has many disadvantages. For example, the pyrolusite roasting method converts MnO2 into MnSO4 and FeS2 into Fe2O3, and then leaches it with water. It needs to be roasted for a long time under a high sulfur-manganese ratio, which not only causes FeS2 to fail to be fully utilized, but also has a large amount of slag and is difficult to handle. There are also problems such as flue gas treatment. In the direct acid leaching method, there are often disadvantages such as low manganese leaching rate, difficult slag treatment, and large amount of sulfuric acid.

[0004] In my country, the process of reducing roasting-sulfuric acid leaching-concentration crystallization is mainly used to produce manganese sulfate with pyrolusite (MnO2·nH2O) as raw material. The reduction roasting equipment for producing manganese monoxide by traditional process is the traditional reverberatory furnace, which has high heat consumption, small bed capacity, low manganese recovery rate and poor working conditions. In the 1980s, Yunnan, Hunan, Xiangxi and Guangdong and other places had successively built rotary kilns to try this aspect, but due to the fine particle size of raw materials, rotary kiln structure and technical problems, the kiln had a serious sticking phenomenon, and most rotary kilns could not be used normally for production. In recent years, a heat recovery type manganese oxide ore microwave reduction roasting process has been developed. The microwave heating furnace is used for the reduction roasting process of manganese oxide ore. Due to the high power consumption (210-240kw·h) and coal consumption (180kg / ton), as well as the microwave source, processing capacity and labor protection issues have not been properly resolved, it is currently difficult to promote and apply it in production. Utility Model Content

[0005] Aiming at the problems of high energy consumption, low manganese recovery rate, serious environmental pollution, etc. in the prior art of using pyrolusite to prepare manganese monoxide, the utility model provides a system for preparing manganese monoxide by using pyrolusite, wherein the pyrolusite is pretreated by a pyrolysis device, a hydrothermal reaction device and an oxidation reaction device arranged in series, so that manganese elements of different valence states in the pyrolusite are almost converted into the form of manganese dioxide, and then a fluidized reduction roasting device is used to directly reduce the manganese dioxide to manganese monoxide in a reducing atmosphere, and the system has the characteristics of high production efficiency, high manganese recovery rate, low energy consumption, little environmental pollution, etc.

[0006] In order to achieve the above technical objectives, the technical solutions adopted by the present utility model are specifically described as follows:

[0007] A system for preparing manganese monoxide using pyrolusite, the system comprising a crushing and grinding device, a pyrolysis device, a hydrothermal reaction device, an oxidation reaction device and a reduction reaction device. The crushing and grinding device, the pyrolysis device, the hydrothermal reaction device, the oxidation reaction device and the reduction reaction device are sequentially arranged in series.

[0008] Preferably, the crushing and grinding device comprises a crusher, a grinding machine and a screening machine. The crusher, the grinding machine and the screening machine are arranged in series in sequence. The under-screen material outlet of the screening machine is connected to the feed end of the pyrolysis device through a feeding mechanism, and the over-screen material outlet of the screening machine is connected to the feed end of the grinding machine through a return mechanism.

[0009] Preferably, the sieve hole diameter of the screening machine is not greater than 1 mm, preferably 0.5-1 mm.

[0010] Preferably, the pyrolysis device is one of a pyrolysis furnace, a rotary kiln, and a pyrolysis furnace tube.

[0011] Preferably, the hydrothermal reaction device and the oxidation reaction device are independently one of a reaction kettle, a reaction tank, a reaction tower, and a reaction tube (furnace tube).

[0012] Preferably, the reduction reaction device is a vertical fluidized reduction furnace (generally with an electric heating device inside), a reduction feed port connected to the discharge end of the oxidation reaction device is provided at the lower part of the side wall of the reduction furnace, a reduction gas inlet is provided on the bottom wall of the reduction furnace, and a reduction discharge port is provided at the top of the reduction furnace.

[0013] Preferably, the pyrolysis device, the hydrothermal reaction device, and the oxidation reaction device are arranged outside the side wall of the reduction reaction device from top to bottom, and the pyrolysis device, the hydrothermal reaction device, and the oxidation reaction device are sequentially connected in series to form a three-stage reaction furnace tube, a protective gas inlet and outlet are provided on the tube wall of the upper section of the furnace tube corresponding to the pyrolysis (i.e., the pyrolysis device section), a water vapor inlet and outlet are provided on the tube wall of the middle section of the furnace tube corresponding to the hydrothermal reaction (i.e., the hydrothermal reaction device section), and an oxygen-containing gas inlet and outlet are provided on the tube wall of the lower section of the furnace tube corresponding to the oxidation reaction (i.e., the oxidation reaction device section, the discharge end of which is connected to the reduction feed port of the reduction reaction device). Preferably, the reaction furnace tube is spirally coiled from top to bottom and arranged outside the side wall of the reduction reaction device.

[0014] Preferably, the system further comprises a material water cooling device, wherein the feed end of the material water cooling device is connected to the reduction discharge port through a discharge pipe.

[0015] Preferably, the system further comprises a reducing gas generating device, the air inlet of the reducing gas generating device is connected to the upper chamber of the reducing reaction device through an air extraction pipe, and the exhaust port of the reducing gas generating device is connected to the reducing gas air inlet through an exhaust pipe. A carbon powder adding pipeline is also provided on the reducing gas generating device. Preferably, a gas composition detector is also provided in the upper chamber of the reducing reaction device. A filter is provided at the air inlet end of the air extraction pipe.

[0016] In the utility model, by adopting the fluidized reduction roasting process, pyrolusite is used as raw material for fluidized reduction roasting to produce manganese monoxide. The fluidized rapid preheating and reduction reaction with the characteristics of efficient mass transfer and heat transfer has many advantages, and the cumbersome agglomeration process is omitted. Compared with the traditional reduction roasting technology, its biggest difference is that the original stacked gas-solid heat exchange and mass transfer are changed into a suspended gas-solid transfer process. After the material enters the reduction furnace tube, a suspended flow is formed under the action of the tangential wind force of the cyclone. The transfer process in the dilute phase suspension state has the following advantages over the transfer process in the stacked state: ① a large transfer area; ② a large comprehensive transfer coefficient; ③ a large transfer power. Fluidized reduction roasting of pyrolusite to produce manganese monoxide is a gas-solid phase non-catalytic reaction. Due to the high density, small pores, fast reaction rate and the generation of solid products of pyrolusite, the unreacted core shrinkage model with unchanged particle size can be used to describe the entire reaction process of a single particle. The macroscopic rate of roasting is not only related to the chemical rate, but also to heat and mass transfer. In the actual production process, the total reaction rate is mainly determined by the reaction temperature, particle size, relative movement speed of the gas-solid phase, gas-solid contact area, etc. The fundamental way to increase the reaction rate is to increase the reaction temperature, reduce the particle size of the ore, and increase the relative movement speed of the gas and the ore particles. The preparation of manganese monoxide by fluidized reduction roasting of pyrolusite with electrical heating has the characteristics of low fossil energy consumption, stable product quality, high quality, and environmental friendliness.

[0017] In the utility model, the reducing agent used in the fluidized reduction roasting of pyrolusite is generally a reducing gas, such as CO and hydrogen. Hydrogen, as a clean energy source, can avoid the generation of waste gas and polluting the environment, but the relative cost of hydrogen is relatively high. Therefore, CO is generally used as a gas reduction medium, and the reduction of 1 mol MnO2 emits about 1 mol CO2, which has a large carbon emission and does not meet the national policy of low-carbon production. Therefore, in view of the disadvantage that the fluidized reduction process of pyrolusite has a large carbon emission due to the use of CO as a reducing medium, it is planned to collect the CO2 emitted by the reduction reaction into a gas storage tank (i.e., a reducing gas generating device), and introduce a small amount of solid carbon powder into the tank so that it reacts with CO2 gas to generate CO gas (C+CO2=2CO), and the reducing gas returns to the fluidized reduction system of pyrolusite, and repeats this process to achieve carbon circulation and reduce the carbon emission of the system. First, the pipe of the reduction roasting furnace tube is cleaned by blowing with inert gas nitrogen, and then a certain weight of pyrolusite raw material is added into the roasting furnace tube from the reduction feed port at the bottom; a mixed gas of CO and nitrogen is used as fluidizing gas, and roasting is performed according to the set fluidized reduction roasting temperature, time and gas fluidization speed (the reducing gas enters the system from the bottom of the furnace tube at a certain gas flow speed, and the running direction is from bottom to top; the pyrolusite is suspended in the furnace tube under the blowing of the gas flow, and reacts with CO at high temperature to generate MnO, and CO2 gas is discharged during the reaction process), after the reaction is completed, the gas fluidization speed is increased, and the material is blown into the reduction discharge port by the gas and enters the material water cooling device for cooling, and MnO is obtained after water cooling for hydrometallurgy; the gas generated during the reaction is transported to the gas reaction tank by the gas pipeline (i.e., the exhaust pipe) at the upper part of the furnace tube, and a small amount of solid carbon powder is introduced to convert CO2 into CO before returning to the system. The method utilizes the characteristics that the fluidized reduction of pyrolusite requires a low CO concentration (generally 3 to 10 wt%) and the emitted CO2 can react with carbon powder to regenerate the reducing gas CO. Only a small amount of carbon powder needs to be added to complete the continuous reduction reaction of the pyrolusite, thereby realizing the recycling and efficient utilization of carbon elements. After recycling, 1 mol of carbon resources can reduce 10 to 33 mol of pyrolusite, thereby maximizing the utilization of carbon resources and significantly reducing carbon emissions, which is in line with the national low-carbon and low-energy consumption industrial policy.

[0018] In the utility model, a gas composition detector is also provided in the upper chamber of the reduction reaction device, and the CO content in the gas at the upper part of the furnace tube is detected in real time by the gas composition detector. When the detected CO gas concentration range is 3-10wt%, it meets the requirements of fluidized reduction of pyrolusite, and the amount of C powder added to the reducing gas generating device remains unchanged; when the detected CO gas concentration range is <3wt%, the reducing gas content in the system is insufficient, and the amount of C powder needs to be increased, and the increased amount of C powder b=5.0*(a+3)*100%; when the detected CO gas concentration range is >10wt%, the reducing gas content in the system is excessive, and the amount of C powder needs to be reduced, and the reduced amount of C powder b=3.0*(a+1)*100%. The C powder used in the utility model is coal powder, coke, graphite powder, etc., and its fixed carbon content is ≥60wt%, and the particle size is -1mm, preferably coke powder.

[0019] In the utility model, it is found in the process of fluidized reduction roasting of pyrolusite that although fluidized reduction roasting can quickly and efficiently reduce manganese dioxide to manganese monoxide, some intermediate valence manganese (such as trimanganese tetraoxide and dimanganese trioxide) still exists in the pyrolusite. Compared with manganese dioxide, trimanganese tetraoxide and dimanganese trioxide have relatively weak oxidizability, and the reduction reaction with reducing gas is relatively slow. Moreover, trimanganese tetraoxide and dimanganese trioxide are both relatively stable oxides of manganese and are difficult to be directly reduced to manganese monoxide (in addition, it has been found through research that it is also difficult to completely convert dimanganese trioxide and trimanganese tetraoxide into manganese dioxide through high-temperature oxidation). This makes it possible for a certain amount of trimanganese tetraoxide and dimanganese trioxide to remain in the reduction product, which affects the product quality and reduces the subsequent leaching efficiency of manganese element. Therefore, in the utility model, by pre-treating the pyrolusite, the manganese tetroxide and manganese trioxide contained in it are first converted into manganese dioxide and then reduction roasted with reducing gas, so that the obtained manganese monoxide product has higher quality and the subsequent leaching efficiency of manganese element can also be guaranteed.

[0020] In the utility model, the steps of pre-treating pyrolusite include crushing and grinding, pyrolysis treatment, hydrothermal reaction and oxidation reaction, wherein the pyrolusite is refined into powder by crushing and grinding treatment, and the powdery ore powder is conducive to the rapid progress of pyrolysis treatment, hydrothermal reaction and oxidation reaction, and also provides a corresponding basis for subsequent fluidized reduction roasting. The refined manganese ore powder is first subjected to pyrolysis treatment, that is, in an oxygen-poor (or oxygen-free) environment (filled with nitrogen or vacuum conditions), at a high temperature (900-100°C) to thermally decompose manganese trioxide into manganese tetraoxide and release oxygen (Mn2O3→Mn3O4+O2). At the same time, a small amount of manganese dioxide is thermally decomposed into manganese tetraoxide (MnO2→Mn3O4+O2). It should be noted that the pyrolysis temperature should not be too low, otherwise the pyrolysis of manganese trioxide will be incomplete and the manganese dioxide will not be completely pyrolyzed and converted into manganese trioxide. If the pyrolysis temperature is too high, the pyrolysis cost will increase and more manganese dioxide will be easily pyrolyzed, which increases the difficulty of subsequent treatment. After pyrolysis treatment, the manganese trioxide in the pyrolusite is basically converted into manganese tetraoxide (the sampling test results show that the manganese trioxide content is below the detection limit), so the manganese tetraoxide is further converted into MnOOH (Mn3O4+MnO2+H2O→MnOOH) by hydrothermal reaction under the oxidation of manganese dioxide, that is, in a water-containing environment (passing water vapor or directly placing in hot water) at a temperature of 80-200°C through manganese dioxide (it can also be other oxidants, manganese dioxide is used here because the raw material itself contains The invention discloses a method for preparing a pyrolusite ore having a manganese dioxide-containing ore (manganese dioxide, which will not introduce new impurities and can reduce cost investment) to convert almost all manganese tetraoxide into MnOOH through oxidation. Further, the material containing MnOOH is subjected to oxidation treatment so that it is oxidized into manganese dioxide. The temperature of the oxidation treatment is 200-500°C. The oxidant is an oxygen-containing gas (such as air or oxygen-rich gas). When the oxidation reaction is carried out, the reaction temperature should not be too high, otherwise it is easy to cause MnOOH to be converted into manganese trioxide. If the temperature is low, the oxidation is not thorough and MnOOH residues will exist. In other words, the utility model converts the manganese element in the pyrolusite into manganese dioxide through the combined action of pyrolysis-hydrothermal reaction-oxidation reaction, thereby improving the efficiency and product quality of subsequent reduction to obtain manganese monoxide, and at the same time, it is helpful for the leaching and recovery of manganese element.

[0021] In the present utility model, the pyrolysis device for pyrolysis reaction is one of a pyrolysis furnace, a rotary kiln, and a pyrolysis furnace tube, and the hydrothermal reaction device for hydrothermal reaction and the oxidation reaction device for oxidation reaction are independently one of a reactor, a reaction tank, a reaction tower, and a reaction tube, wherein the pyrolysis device, the hydrothermal reaction device, and the oxidation reaction device can be independently arranged, or can be arranged in series as an integrated type, for example, a three-stage reaction furnace tube (including a pyrolysis section, a hydrothermal reaction section, and an oxidation reaction section) that are jointly formed in series in sequence (including a pyrolysis section, a hydrothermal reaction section, and an oxidation reaction section, each section independently inlet and outlet air and independently equipped with an electric heating device). In the present utility model, a preferred embodiment is that the reaction furnace tube jointly formed by the pyrolysis device, the hydrothermal reaction device, and the oxidation reaction device is spirally coiled from top to bottom and arranged on the outside of the side wall of the reduction reaction device, that is, the material after crushing and grinding passes through the pyrolysis section, the hydrothermal reaction section, and the oxidation reaction section of the reaction furnace tube in sequence and enters the reduction reaction device for reduction, and the whole process is continuous and uninterrupted, without intermediate transportation, which greatly improves production efficiency and saves equipment investment and site occupation.

[0022] In the present invention, the diameter of the three-stage reaction furnace tube composed of the pyrolysis device, the hydrothermal reaction device and the oxidation reaction device is 0.1-10m, preferably 0.2-8m, more preferably 0.3-6m. The inner diameter of the reducing gas generating device is 0.2-20m, preferably 0.3-15m, more preferably 0.5-12m.

[0023] Compared with the prior art, the beneficial technical effects of the utility model are as follows:

[0024] 1: The utility model converts manganese tetroxide and manganese trioxide contained in pyrolusite into manganese dioxide at low cost and high efficiency by pre-treating pyrolusite by pyrolysis, hydrothermal reaction and oxidation reaction, thereby improving the quality of manganese monoxide products in subsequent fluidized reduction and laying a foundation for subsequent efficient leaching of manganese.

[0025] 2: The utility model recycles the carbon dioxide released during the fluidized reduction of pyrolusite by means of electric heating, and further prepares CO that can be recycled for reduction, thereby maximizing the use of carbon resources, significantly reducing carbon emissions, and complying with the national industrial policy of low carbon and low energy consumption.

[0026] 3: The overall structure of the system of the utility model is simple, easy to operate, requires little equipment investment, and occupies little space. It has the advantage of large-scale promotion, good economic and environmental benefits, and is expected to open up a more stable and efficient way for the development and utilization of pyrolusite. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 It is a schematic diagram of the overall structure of the system of the utility model.

[0028] Figure 2 This is a structural schematic diagram of the utility model in which a pyrolysis device, a hydrothermal reaction device, and an oxidation reaction device are arranged in series on the outer side wall of a reduction reaction device.

[0029] Figure 3 The utility model is a structural schematic diagram of a spiral three-section reaction furnace tube formed by a pyrolysis device, a hydrothermal reaction device and an oxidation reaction device.

[0030] Figure numerals: 1: crushing and grinding device; 101: crusher; 102: grinding machine; 103: screening machine; 2: pyrolysis device; 3: hydrothermal reaction device; 4: oxidation reaction device; 5: reduction reaction device; 501: reduction feed port; 502: reduction gas inlet; 503: reduction discharge port; 6: material water cooling device; 7: reduction gas generating device; 701: carbon powder adding pipeline; 8: gas composition detector; 9: filter. DETAILED DESCRIPTION

[0031] The technical solution of the utility model is illustrated below, and the scope of protection requested for the utility model includes but is not limited to the following embodiments.

[0032] A system for preparing manganese monoxide using pyrolusite, the system comprising a crushing and grinding device 1, a pyrolysis device 2, a hydrothermal reaction device 3, an oxidation reaction device 4 and a reduction reaction device 5. The crushing and grinding device 1, the pyrolysis device 2, the hydrothermal reaction device 3, the oxidation reaction device 4 and the reduction reaction device 5 are sequentially arranged in series.

[0033] Preferably, the crushing and grinding device 1 comprises a crusher 101, a grinding machine 102 and a screening machine 103. The crusher 101, the grinding machine 102 and the screening machine 103 are sequentially arranged in series. The under-screen material outlet of the screening machine 103 is connected to the feed end of the pyrolysis device 2 through a feeding mechanism, and the over-screen material outlet of the screening machine 103 is connected to the feed end of the grinding machine 102 through a return mechanism.

[0034] Preferably, the sieve hole diameter of the screening machine 103 is not greater than 1 mm, preferably 0.5-1 mm.

[0035] Preferably, the pyrolysis device 2 is one of a pyrolysis furnace, a rotary kiln, and a pyrolysis furnace tube.

[0036] Preferably, the hydrothermal reaction device 3 and the oxidation reaction device 4 are independently one of a reaction kettle, a reaction tank, a reaction tower and a reaction tube.

[0037] Preferably, the reduction reaction device 5 is a vertical fluidized reduction furnace, a reduction feed port 501 connected to the discharge end of the oxidation reaction device 4 is arranged at the lower part of the side wall of the reduction furnace, a reduction gas inlet port 502 is arranged on the bottom wall of the reduction furnace, and a reduction discharge port 503 is arranged at the top of the reduction furnace.

[0038] Preferably, the pyrolysis device 2, the hydrothermal reaction device 3, and the oxidation reaction device 4 are arranged outside the side wall of the reduction reaction device 5 from top to bottom, and the pyrolysis device 2, the hydrothermal reaction device 3, and the oxidation reaction device 4 are sequentially connected in series to form a three-stage reaction furnace tube, a protective gas inlet and outlet are provided on the upper tube wall of the furnace tube corresponding to the pyrolysis, a water vapor inlet and outlet are provided on the middle tube wall of the furnace tube corresponding to the hydrothermal reaction, and an oxygen-containing gas inlet and outlet are provided on the lower tube wall of the furnace tube corresponding to the oxidation reaction. Preferably, the reaction furnace tube is spirally coiled from top to bottom and arranged outside the side wall of the reduction reaction device 5.

[0039] Preferably, the system further comprises a material water cooling device 6. The feed end of the material water cooling device 6 is connected to the reduction discharge port 503 through a discharge pipe.

[0040] Preferably, the system further comprises a reducing gas generating device 7, the air inlet of the reducing gas generating device 7 is connected to the upper chamber of the reducing reaction device 5 through an air extraction pipe, and the exhaust port of the reducing gas generating device 7 is connected to the reducing gas air inlet 502 through an exhaust pipe. A carbon powder adding pipeline 701 is also provided on the reducing gas generating device 7. Preferably, a gas composition detector 8 is also provided in the upper chamber of the reducing reaction device 5. A filter 9 is provided at the air inlet end of the air extraction pipe.

[0041] Example 1

[0042] like Figure 1-3 As shown, a system for preparing manganese monoxide using pyrolusite comprises a crushing and grinding device 1, a pyrolysis device 2, a hydrothermal reaction device 3, an oxidation reaction device 4 and a reduction reaction device 5. The crushing and grinding device 1, the pyrolysis device 2, the hydrothermal reaction device 3, the oxidation reaction device 4 and the reduction reaction device 5 are sequentially arranged in series.

[0043] Example 2

[0044] Example 1 is repeated, except that the crushing and grinding device 1 includes a crusher 101, a grinding machine 102 and a screening machine 103. The crusher 101, the grinding machine 102 and the screening machine 103 are sequentially arranged in series. The undersize material outlet of the screening machine 103 is connected to the feed end of the pyrolysis device 2 through a feeding mechanism, and the oversize material outlet of the screening machine 103 is connected to the feed end of the grinding machine 102 through a return mechanism.

[0045] Example 3

[0046] Example 2 was repeated except that the sieve hole diameter of the sieving machine 103 was 0.8 mm.

[0047] Example 4

[0048] Example 3 was repeated except that the sieve hole diameter of the sieving machine 103 was 1 mm.

[0049] Example 5

[0050] Example 4 is repeated, except that the pyrolysis device 2 is a pyrolysis furnace.

[0051] Example 6

[0052] Example 5 is repeated, except that the pyrolysis device 2 is a pyrolysis furnace tube.

[0053] Example 7

[0054] Example 6 is repeated, except that the hydrothermal reaction device 3 and the oxidation reaction device 4 are independent reaction tanks.

[0055] Example 8

[0056] Example 7 is repeated, except that the hydrothermal reaction device 3 and the oxidation reaction device 4 are independent reaction tubes.

[0057] Example 9

[0058] Example 8 is repeated, except that the reduction reaction device 5 is a vertical fluidized reduction furnace, a reduction feed port 501 connected to the discharge end of the oxidation reaction device 4 is provided at the lower part of the side wall of the reduction furnace, a reduction gas inlet port 502 is provided on the bottom wall of the reduction furnace, and a reduction discharge port 503 is provided at the top of the reduction furnace.

[0059] Example 10

[0060] Example 9 is repeated, except that the pyrolysis device 2, the hydrothermal reaction device 3, and the oxidation reaction device 4 are arranged outside the side wall of the reduction reaction device 5 from top to bottom, and the pyrolysis device 2, the hydrothermal reaction device 3, and the oxidation reaction device 4 are sequentially connected in series to form a three-stage reaction furnace tube, a protective gas inlet and an outlet are opened on the upper tube wall of the furnace tube corresponding to the pyrolysis, a water vapor inlet and an outlet are opened on the middle tube wall of the furnace tube corresponding to the hydrothermal reaction, and an oxygen-containing gas inlet and an outlet are opened on the lower tube wall of the furnace tube corresponding to the oxidation reaction.

[0061] Embodiment 11

[0062] Example 10 was repeated, except that the reaction furnace tube was spirally wound from top to bottom and arranged outside the side wall of the reduction reaction device 5.

[0063] Example 12

[0064] The embodiment 11 is repeated, except that the system further includes a material water cooling device 6. The feed end of the material water cooling device 6 is connected to the reduction discharge port 503 through a discharge pipe.

[0065] Embodiment 13

[0066] Example 12 is repeated, except that the system further includes a reducing gas generating device 7, the air inlet of the reducing gas generating device 7 is connected to the upper chamber of the reducing reaction device 5 through an air extraction pipe, and the exhaust port of the reducing gas generating device 7 is connected to the reducing gas inlet 502 through an exhaust pipe. A carbon powder adding pipeline 701 is also provided on the reducing gas generating device 7.

[0067] Embodiment 14

[0068] Example 13 was repeated except that a gas component detector 8 was further provided in the upper chamber of the reduction reaction device 5. A filter 9 was provided at the air inlet end of the air extraction pipe.

Claims

1. A system for preparing manganese monoxide using pyrolusite, characterized in that: The system comprises a crushing and grinding device (1), a pyrolysis device (2), a hydrothermal reaction device (3), an oxidation reaction device (4) and a reduction reaction device (5); the crushing and grinding device (1), the pyrolysis device (2), the hydrothermal reaction device (3), the oxidation reaction device (4) and the reduction reaction device (5) are sequentially arranged in series.

2. The system according to claim 1, characterized in that: The crushing and grinding device (1) comprises a crusher (101), a grinder (102) and a screen (103); the crusher (101), the grinder (102) and the screen (103) are arranged in series in sequence; the under-screen material outlet of the screen (103) is connected to the feed end of the pyrolysis device (2) via a feeding mechanism, and the over-screen material outlet of the screen (103) is connected to the feed end of the grinder (102) via a returning mechanism.

3. The system according to claim 2, characterized in that: The sieve hole diameter of the sieving machine (103) is not greater than 1 mm.

4. The system according to claim 3, characterized in that: The sieve hole diameter of the sieving machine (103) is 0.5-1 mm.

5. The system according to any one of claims 1 to 4, characterized in that: The pyrolysis device (2) is one of a pyrolysis furnace, a rotary kiln, and a pyrolysis furnace tube.

6. The system according to any one of claims 1 to 4, characterized in that: The hydrothermal reaction device (3) and the oxidation reaction device (4) are independently one of a reaction kettle, a reaction tank, a reaction tower, and a reaction tube.

7. The system according to any one of claims 1 to 4, characterized in that: The reduction reaction device (5) is a vertical fluidized reduction furnace, a reduction feed port (501) connected to the discharge end of the oxidation reaction device (4) is arranged at the lower part of the side wall of the vertical fluidized reduction furnace, a reduction gas inlet (502) is arranged on the bottom wall of the reduction furnace, and a reduction discharge port (503) is arranged on the top of the reduction furnace.

8. The system according to claim 7, characterized in that: The pyrolysis device (2), the hydrothermal reaction device (3), and the oxidation reaction device (4) are arranged outside the side wall of the reduction reaction device (5) from top to bottom, and the pyrolysis device (2), the hydrothermal reaction device (3), and the oxidation reaction device (4) are sequentially connected in series to form a three-stage reaction furnace tube, a protective gas inlet and an outlet are opened on the tube wall of the upper section of the furnace tube corresponding to the pyrolysis, a water vapor inlet and an outlet are opened on the tube wall of the middle section of the furnace tube corresponding to the hydrothermal reaction, and an oxygen-containing gas inlet and an outlet are opened on the tube wall of the lower section of the furnace tube corresponding to the oxidation reaction.

9. The system according to claim 8, characterized in that: The reaction furnace tube is spirally coiled from top to bottom and arranged outside the side wall of the reduction reaction device (5).

10. The system according to claim 8, characterized in that: The system also includes a material water cooling device (6); the feed end of the material water cooling device (6) is connected to the reduction discharge port (503) via a discharge pipe.

11. The system according to claim 10, characterized in that: The system also includes a reducing gas generating device (7), the air inlet of the reducing gas generating device (7) being connected to the upper chamber of the reducing reaction device (5) via an air extraction pipe, and the exhaust port of the reducing gas generating device (7) being connected to the reducing gas air inlet (502) via an exhaust pipe; and a carbon powder adding pipeline (701) is also provided on the reducing gas generating device (7).

12. The system according to claim 10 or 11, characterized in that: A gas component detector (8) is also provided in the upper chamber of the reduction reaction device (5); and a filter (9) is provided at the air inlet end of the air extraction pipe.

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