System for producing manganese sulfate

Abstract

The utility model relates to the technical field of chemical equipment, and provides a system for producing manganese sulfate, which comprises a forced circulation evaporator; the crystallization separator is provided with a first material inlet and a second material inlet, and the material outlet of the forced circulation evaporator is communicated with the second material inlet of the crystallization separator; the secondary separator is communicated with a steam outlet of the crystallization separator; one end of the centrifugal steam compressor is communicated with the secondary separator, and the other end of the centrifugal steam compressor is communicated with a steam inlet of the forced circulation evaporator. According to the technical scheme, the common problem of heat exchanger blockage caused by foaming, crystallization and caking in the traditional process in the prior art is solved.

Description

Technical Field

[0001] The utility model relates to the technical field of chemical equipment, and in particular to a system for producing manganese sulfate. Background Art

[0002] Manganese sulfate is an important chemical raw material that can be used to produce metallic manganese, other manganese salts and manganese oxides. It is widely used in energy, medicine, fertilizer, feed, food, papermaking, catalyst and other industries. Manganese sulfate has a wide range of applications in battery manufacturing and other fields. It is currently mainly used in positive electrode materials for new energy batteries. In positive electrode materials, manganese can stabilize the material structure, improve safety, and reduce battery costs.

[0003] There are many industrial production methods for manganese sulfate. The main process steps include acid leaching of manganese ore or acid leaching after roasting manganese ore, evaporation of manganese sulfate solution, and crystallization to obtain manganese sulfate. In the evaporation crystallizer, manganese sulfate can be separated and purified by evaporation and crystallization. The solubility of manganese sulfate decreases with increasing temperature within the evaporation temperature range. Based on this characteristic, the material will produce a certain degree of temperature increase due to heating during the circulation process in the heat exchange tube, so that the solubility begins to decrease in the heat exchange tube, and there is a tendency for solids to precipitate. Therefore, even if the solution does not boil and concentrate in the heat exchange tube, solids may precipitate and adhere to the heating surface, resulting in blockage of the heat exchange tube, significantly reducing the heat exchange efficiency of the evaporator, resulting in a sharp increase in the energy consumption cost of evaporation and reduced production efficiency. This situation is very likely to occur when the flow rate between the tubes is too low and the circulation volume of the axial flow pump is insufficient. Utility Model Content

[0004] The utility model provides a system for producing manganese sulfate, which solves the problem of heat exchanger blockage caused by foaming and crystal agglomeration commonly seen in traditional processes in the related art.

[0005] The technical solution of the utility model is as follows:

[0006] A system for producing manganese sulfate, comprising:

[0007] Forced circulation evaporator;

[0008] A crystal separator having a first material inlet and a second material inlet, wherein the material outlet of the forced circulation evaporator is connected to the second material inlet of the crystal separator;

[0009] a secondary separator, the secondary separator being in communication with a steam outlet of the crystallization separator;

[0010] A centrifugal steam compressor, one end of which is communicated with the secondary separator, and the other end of which is communicated with the steam inlet of the forced circulation evaporator.

[0011] Preferably, it also includes:

[0012] Condensate preheater;

[0013] A feed pump, the feed pump is connected to the material inlet of the condensate preheater;

[0014] A non-condensable gas preheater, wherein the material inlet of the non-condensable gas preheater is connected to the material outlet of the condensate preheater;

[0015] A raw steam preheater, wherein the material inlet of the raw steam preheater is connected to the material outlet of the non-condensable gas preheater, and the material outlet of the raw steam preheater is connected to the first material inlet of the crystallizer separator.

[0016] Preferably, it also includes:

[0017] A forced circulation pump is connected to the material outlet of the crystallizer separator, and the outlet of the forced circulation pump is connected to the material inlet of the forced circulation evaporator.

[0018] Preferably, it also includes:

[0019] a first pipeline, through which the material outlet of the forced circulation pump is connected to the forced circulation evaporator;

[0020] a discharge pump, wherein a material inlet of the discharge pump is connected to the first pipeline;

[0021] A thickener, wherein the material inlet of the thickener is communicated with the material outlet of the discharge pump.

[0022] Preferably, it also includes:

[0023] a centrifuge, the centrifuge being in communication with a material outlet of the thickener;

[0024] A storage tank, the centrifuge and the thickener are both connected to the storage tank, and the storage tank has a mother liquor discharge pipe.

[0025] Preferably, it also includes:

[0026] A condensed water tank, wherein the condensed water outlet of the forced circulation evaporator is communicated with the condensed water inlet of the condensed water tank, and the condensed water outlet of the condensed water tank is communicated with the condensed water inlet of the condensed water preheater.

[0027] Preferably, it also includes:

[0028] A liquid level meter is arranged on the crystal separator, and the liquid level meter is a double flange differential pressure transmitter.

[0029] Preferably, the condensate preheater, the non-condensable gas preheater and the live steam preheater are all plate heat exchangers.

[0030] The working principle and beneficial effects of the utility model are:

[0031] In the utility model, steam and solution are separated in the crystallization separator, and at the same time, part of manganese sulfate begins to crystallize out. The separated pure steam continues to go to the secondary separator for further processing, while the solution containing the incompletely crystallized substance is sent back to the evaporator for recycling. The secondary separator is used to further purify the steam from the crystallization separator and reduce the entrainment of mist in the steam. The problem of foaming and crystal agglomeration is effectively solved, thereby ensuring the service life and normal operation of the system. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] The preferred implementation modes will be described below in a clear and understandable manner with reference to the accompanying drawings to further illustrate the above-mentioned characteristics, technical features, advantages and implementation methods of the present utility model.

[0033] Figure 1 This is a schematic diagram of a system for producing manganese sulfate according to the utility model.

[0034] In the figure: 1. Condensate preheater; 2. Feed pump; 3. Non-condensable gas preheater; 4. Raw steam preheater; 5. Crystallizer separator; 501. First material inlet; 502. Second material inlet; 6. Forced circulation pump; 7. Forced circulation evaporator; 8. First pipeline; 9. Secondary separator; 10. Centrifugal steam compressor; 11. Discharge pump; 12. Thickener; 13. Centrifuge; 14. Condensate tank; 15. Second pipeline; 16. Mother liquor discharge pipe; 17. Storage tank. DETAILED DESCRIPTION

[0035] In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the specific implementation methods of the utility model will be described below with reference to the accompanying drawings. Obviously, the accompanying drawings described below are only some embodiments of the utility model. For ordinary technicians in this field, other drawings and other implementation methods can be obtained based on these drawings without creative work.

[0036] In order to simplify the drawings, only the parts related to the utility model are schematically shown in each figure, and they do not represent the actual structure of the product. In addition, in order to simplify the drawings and facilitate understanding, in some figures, only one of the parts with the same structure or function is schematically shown, or only one of them is marked. In this article, "one" not only means "only one", but also means "more than one", and "several" includes "two" and "more than two".

[0037] In this article, it should be noted that, unless otherwise clearly specified and limited, the terms "installed", "connected", and "connected" 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 it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in this utility model can be understood according to specific circumstances.

[0038] In addition, in the description of the present application, the terms "first", "second", etc. are only used to distinguish the description and cannot be understood as indicating or implying relative importance.

[0039] Reference Figure 1 , which is an embodiment of the utility model, proposes a system for producing manganese sulfate, including: a forced circulation evaporator 7; a crystal separator 5, having a first material inlet 501 and a second material inlet 502, the material outlet of the forced circulation evaporator 7 is connected to the second material inlet 502 of the crystal separator 5; a secondary separator 9, the secondary separator 9 is connected to the steam outlet of the crystal separator 5; a centrifugal steam compressor 10, one end of the centrifugal steam compressor 10 is connected to the secondary separator 9, and the other end of the centrifugal steam compressor 10 is connected to the steam inlet of the forced circulation evaporator 7.

[0040] In the above scheme, the evaporation and crystallization process is optimized to improve the production efficiency and product quality of manganese sulfate. The system components include a forced circulation evaporator 7, a crystal separator 5, a secondary separator 9 and a centrifugal steam compressor. The forced circulation evaporator 7 is used to heat the manganese sulfate solution, promote the evaporation of water, and maintain the circulation of the solution. The first material inlet 501 receives the manganese sulfate solution from the preheating treatment, and is driven by the built-in forced circulation pump 6 to flow at high speed in the heat exchange tube. The steam generated by evaporation and part of the unevaporated solution flow to the crystal separator 5 through the steam inlet, while the condensed water returns to the preheating link at the front end of the system through a specific pipeline to achieve energy recovery. The crystal separator 5 is located after the evaporator and has two key interfaces-the second material inlet 502 receives the mixed flow output by the evaporator, and the steam outlet is connected to the secondary separator 9. The steam and solution in the crystal separator 5 are separated, and at the same time, part of the manganese sulfate begins to crystallize. The separated pure steam continues to the secondary separator 9 for further processing, while the solution containing incompletely crystallized substances is sent back to the evaporator for recycling. The secondary separator 9 is used to further purify the steam from the crystal separator 5, reduce the entrainment of mist and foam in the steam, and prevent these droplets from causing damage to the subsequent compressor. The purified steam is transported to the centrifugal steam compressor, and the small amount of separated liquid may be recycled or processed. The centrifugal steam compressor is the energy boosting unit in the system. It receives the pure steam output from the secondary separator 9 and compresses it, increases the pressure and temperature of the steam, and then re-injects this part of high-energy steam into the forced circulation evaporator 7 as a heat source. This closed loop greatly improves the energy efficiency of the system and reduces the demand for external heat sources. Operation process: The manganese sulfate solution is first gradually heated in a series of preheaters, and then enters the forced circulation evaporator 7 to evaporate water under high-speed circulation. The generated steam and part of the solution mixture enter the crystal separator 5 to achieve the preliminary separation of steam and concentrated liquid. After the separated steam is finely treated by the secondary separator 9, it is input into the centrifugal steam compressor for compression to increase its energy level. The compressed high-temperature and high-pressure steam is sent back to the forced circulation evaporator 7, and continues to heat the newly flowing manganese sulfate solution as a heat source, forming a closed thermodynamic cycle.

[0041] Furthermore, it also includes: a condensate preheater 1; a feed pump 2, the feed pump 2 is connected to the material inlet of the condensate preheater 1; a non-condensable gas preheater 3, the material inlet of the non-condensable gas preheater 3 is connected to the material outlet of the condensate preheater 1; a raw steam preheater 4, the material inlet of the raw steam preheater 4 is connected to the material outlet of the non-condensable gas preheater 3, and the material outlet of the raw steam preheater 4 is connected to the first material inlet 501 of the crystallizer separator 5.

[0042] In the above scheme, the condensate preheater 1 is located at the front end of the system, and its main task is to use the condensate heat recovered from the evaporation process to preheat the manganese sulfate raw material solution. In this way, not only the energy that would otherwise be lost is recovered, but also the energy consumption of the subsequent heating process is effectively reduced. The feed pump 2 is installed in front of the first material inlet 501 of the condensate preheater 1, and its purpose is to extract the manganese sulfate raw material solution from the storage tank and send it into the condensate preheater 1 with sufficient pressure for preliminary heating. It ensures that the material can flow evenly and continuously during the preheating stage, laying a good foundation for the subsequent multi-stage preheating process. The non-condensable gas preheater 3 is immediately after the condensate preheater 1. The non-condensable gas preheater 3 uses the waste heat of the non-condensable gas (usually refers to a gas that cannot be condensed into a liquid, such as air) discharged from the system to further heat the material that has been preheated for the first time. This step not only recovers additional heat resources, but also avoids the energy waste caused by the direct discharge of non-condensable gas. The raw steam preheater 4 is located after the non-condensable gas preheater 3. Its main heat source is the raw steam provided by the outside of the system, or the circulating steam after the centrifugal steam compressor is pressurized. This equipment performs the final heating and lifting of the material to ensure that it reaches the ideal temperature state required for entering the crystallizer 5.

[0043] Furthermore, it also includes: a forced circulation pump 6 , the forced circulation pump 6 is connected to the material outlet of the crystallizer separator 5 , and the outlet of the forced circulation pump 6 is connected to the material inlet of the forced circulation evaporator 7 .

[0044] In the above scheme, after the crystallizer 5 completes the preliminary separation of steam and concentrated liquid, the power provided by the forced circulation pump 6 is used to send the incompletely crystallized concentrated liquid back to the evaporation environment again, so as to further concentrate and promote the crystallization process, ensure the efficient use of heat energy and increase the crystallization rate. The forced circulation pump 6 extracts the concentrated liquid output by the crystallizer 5 and sends it to the forced circulation evaporator 7 at a certain flow rate (for example, 2.0-2.2m / s). Such a flow rate helps to reduce the residence time of the material in the evaporation tube, avoid excessive crystallization or scaling problems caused by long-term high temperature, and ensure the effectiveness and stability of heat exchange in the evaporator. In this loop, with each cycle, the material is continuously evaporated and concentrated, and the uncrystallized solution continues to receive heat and circulates back to the crystallizer 5, promoting more water evaporation and crystal growth until the desired degree of crystallization is reached. The above scheme not only ensures the efficient conduction of the evaporation and crystallization process, but also significantly improves the energy efficiency and production capacity of the system by recycling heat energy and materials. At the same time, by precisely controlling the flow rate of the circulation pump and the operating parameters of the evaporator, the crystallization process can be flexibly adjusted to meet the production needs of manganese sulfate with different quality requirements, thus achieving refined management and optimization of the production process.

[0045] Furthermore, it also includes: a first pipeline 8, the material outlet of the forced circulation pump 6 is connected to the forced circulation evaporator 7 through the first pipeline 8; a discharge pump 11, the material inlet of the discharge pump 11 is connected to the first pipeline 8; a thickener 12, the material inlet of the thickener 12 is connected to the material outlet of the discharge pump 11.

[0046] In the above scheme, the outlet of the forced circulation pump 6 is directly connected to the forced circulation evaporator 7 through the first pipeline 8, ensuring that the concentrated liquid after pretreatment enters the evaporation environment smoothly. In addition, the discharge pump 11 is arranged on the first pipeline 8 and is connected thereto. The function of the discharge pump 11 is to extract the concentrated liquid that has reached a predetermined concentration from the circulation to prepare for the subsequent solid-liquid separation. The outlet of the discharge pump 11 is connected to the inlet of the thickener 12, so that the concentrated liquid extracted from the circulation can be introduced into the thickener 12. Inside the thickener 12, by controlling the appropriate temperature and stirring, the crystals in the solution are further grown (crystal growing process), and the viscosity of the solution is increased, creating favorable conditions for centrifugal separation.

[0047] Furthermore, it also includes: a centrifuge 13, which is connected to the material outlet of the thickener 12; a storage tank 17, and the centrifuge 13 and the thickener 12 are both connected to the storage tank 17, and the storage tank 17 has a mother liquor discharge pipe 18. The outlet of the thickener 12 is directly connected to the centrifuge 13, realizing a seamless transition from thickening treatment to final solid-liquid separation. The centrifuge 13 uses the centrifugal force generated by high-speed rotation to efficiently separate the mature manganese sulfate crystals from the mother liquor, ensuring the purity and dryness of the product, and also facilitating the collection and subsequent treatment of the crystals.

[0048] Furthermore, the condensed water tank 14 , the condensed water outlet of the forced circulation evaporator 7 is connected to the condensed water inlet of the condensed water tank 14 , and the condensed water outlet of the condensed water tank 14 is connected to the condensed water inlet of the condensed water preheater 1 .

[0049] In the above scheme, the condensed water generated during the evaporation process of the forced circulation evaporator 7 is collected. These condensed waters are by-products of the heat exchange process and contain a large amount of heat energy. The collected condensed water is introduced into the condensed water tank for temporary storage. The condensed water tank not only plays the role of buffer storage, but is also equipped with an outlet, which is directly connected to the inlet of the condensed water preheater 1. This means that the condensed water recovered from the evaporation process is reintroduced into the pretreatment stage of the system as one of the heat sources of the condensed water preheater 1. By returning the condensed water to the condensed water preheater 1, the system effectively recovers a large amount of heat energy released during the evaporation process, realizes the recycling of heat energy, greatly improves the energy efficiency ratio of the entire system, and reduces the consumption of external energy. The reuse of condensed water helps to maintain the preheating temperature of the material at the inlet of the condensed water preheater 1 at a relatively constant and appropriate level, which is conducive to the stable progress of the subsequent evaporation and crystallization process, and ensures product quality and production efficiency.

[0050] Furthermore, it also includes: a liquid level meter, which is arranged on the crystal separator 5, and the liquid level meter is a double-flange differential pressure transmitter, and the flange on the double-flange differential pressure transmitter is a wall-attached flange.

[0051] In the above scheme, the role of the liquid level gauge on the crystallizer separator 5 is to monitor the changes in the liquid level in the crystallization chamber in real time, which is crucial for controlling the evaporation rate, avoiding overflow and optimizing the crystallization conditions. The type of liquid level gauge is a double flange differential pressure transmitter. This type of transmitter calculates the liquid level by detecting the pressure difference between the two flanges. It has the characteristics of strong anti-interference and high measurement accuracy. It is suitable for measuring the liquid level of containers with complex working conditions such as crystallization, precipitation or foam. The wall-attached flange is directly installed on the wall of the crystallizer separator 5, which can reduce the possibility of crystallized material depositing near the flange, prevent blockage or affect the accuracy of measurement, and reduce the workload of cleaning and maintenance. By using a double flange differential pressure transmitter as a liquid level gauge, the system can more accurately control the liquid level in the crystallizer separator 5, ensure that the evaporation and crystallization processes are carried out under optimal conditions, and avoid the decline in production efficiency or product quality problems caused by improper liquid level control.

[0052] Furthermore, the condensate preheater 1, the non-condensable gas preheater 3 and the live steam preheater 4 are all plate heat exchangers.

[0053] The application aims to produce high-quality manganese sulfate products efficiently and energy-savingly, solve the common problems of foaming and crystal agglomeration leading to heat exchanger blockage in traditional processes, ensure the long-term stable operation of the system and optimize production costs.

[0054] Operation process:

[0055] 1. Initial material processing: First, the manganese sulfate raw material is fed into the condensate preheater 1 through the feed pump 2. At this stage, the material is preliminarily preheated and the temperature is raised by about 35°C to 40°C.

[0056] 2. Multi-stage preheating: The preheated material passes through the non-condensable gas preheater 3 and the live steam preheater 4 in sequence. After each stage of preheating, the material temperature rises further to ensure that the ideal evaporation conditions are achieved. This three-stage preheating design achieves uniform and efficient heating of the material.

[0057] 3. Crystallization and circulation: Subsequently, the material enters the crystallizer separator 5, which not only promotes the evaporation and crystallization of the material, but also has its steam outlet connected to the secondary separator 9, which effectively reduces the entrainment of mist and foam in the steam and protects the safety of the subsequent centrifugal steam compressor. At the same time, the incompletely crystallized material forms a closed-loop circulation with the forced circulation evaporator 7 through the forced circulation pump 6, and the circulation speed is controlled at 2.0-2.2m / s to shorten the residence time of the material and extend the effective working cycle of the system. The forced circulation evaporator 7 is designed with an upper and lower cone angle of 75°, which optimizes the internal fluid dynamics and improves the heat transfer efficiency.

[0058] 4. Condensate recovery and reuse: The condensed water produced by the forced circulation evaporator 7 is collected and sent back to the condensed water tank, and then introduced into the condensed water preheater 1 to participate in the material preheating process, forming a closed thermal energy circulation system and improving the overall energy utilization rate.

[0059] 5. Post-treatment and separation: The fully concentrated material is sent to the thickener 12 by the discharge pump 11 for crystal growth and thickening treatment, and finally the solid-liquid separation is achieved by the centrifuge 13 to obtain pure manganese sulfate crystals.

[0060] By applying the double flange differential pressure transmitter to the liquid level measurement of the crystallizer separator 5 and adopting the wall-attached flange design, the accumulation of crystals near the instrument is effectively avoided, the cleaning and maintenance requirements are reduced, and the accuracy of liquid level monitoring is maintained. As the core component of the condensate preheater 1, the non-condensable gas preheater 3 and the raw steam preheater 4, the plate heat exchanger improves the efficiency of the entire preheating process and the quality consistency of the final product through a single-flow design and uniform heating on the material side. Through the detailed description of the above embodiments, the present application provides a manganese sulfate production system that integrates MVR technology and evaporation crystallization technology, which not only solves the technical problems in traditional processes, but also significantly improves energy efficiency and reduces production costs.

[0061] It should be noted that the above embodiments are only used to illustrate the technical solution of the utility model rather than to limit it. Although the utility model has been described in detail with reference to the preferred embodiments, ordinary technicians in the field should understand that the technical solution of the utility model can be modified or replaced by equivalents without departing from the spirit and scope of the technical solution of the utility model, which should be included in the scope of the claims of the utility model.

Claims

1. A system for producing manganese sulfate, characterized in that: include: Forced circulation evaporator (7); A crystal separator (5) having a first material inlet (501) and a second material inlet (502), wherein the material outlet of the forced circulation evaporator (7) is connected to the second material inlet (502) of the crystal separator (5); a secondary separator (9), the secondary separator (9) being in communication with the steam outlet of the crystallization separator (5); A centrifugal steam compressor (10), one end of the centrifugal steam compressor (10) is connected to the secondary separator (9), and the other end of the centrifugal steam compressor (10) is connected to the steam inlet of the forced circulation evaporator (7).

2. A system for producing manganese sulfate according to claim 1, characterized in that: Also includes: Condensate preheater (1); A feed pump (2), the feed pump (2) being in communication with a material inlet of the condensate preheater (1); A non-condensable gas preheater (3), wherein a material inlet of the non-condensable gas preheater (3) is connected to a material outlet of the condensate preheater (1); A raw steam preheater (4), wherein the material inlet of the raw steam preheater (4) is connected to the material outlet of the non-condensable gas preheater (3), and the material outlet of the raw steam preheater (4) is connected to the first material inlet (501) of the crystallizer separator (5).

3. A system for producing manganese sulfate according to claim 2, characterized in that: Also includes: A forced circulation pump (6), wherein the forced circulation pump (6) is connected to the material outlet of the crystallizer separator (5), and the outlet of the forced circulation pump (6) is connected to the material inlet of the forced circulation evaporator (7).

4. A system for producing manganese sulfate according to claim 3, characterized in that: Also includes: A first pipeline (8), through which the material outlet of the forced circulation pump (6) is connected to the forced circulation evaporator (7); a discharge pump (11), wherein a material inlet of the discharge pump (11) is in communication with the first pipeline (8); A thickener (12), wherein the material inlet of the thickener (12) is connected to the material outlet of the discharge pump (11).

5. A system for producing manganese sulfate according to claim 2, characterized in that: Also includes: a centrifuge (13), wherein the centrifuge (13) is connected to a material outlet of the thickener (12); A storage tank (17), the centrifuge (13) and the thickener (12) are both connected to the storage tank (17), and the storage tank (17) has a mother liquor discharge pipe (16).

6. A system for producing manganese sulfate according to claim 2, characterized in that: Also includes: A condensate tank (14), wherein the condensate outlet of the forced circulation evaporator (7) is connected to the condensate inlet of the condensate tank (14), and the condensate outlet of the condensate tank (14) is connected to the condensate inlet of the condensate preheater (1).

7. A system for producing manganese sulfate according to claim 1, characterized in that: Also includes: A liquid level meter is arranged on the crystal separator (5), and the liquid level meter is a double flange differential pressure transmitter.

8. A system for producing manganese sulfate according to claim 2, characterized in that: The condensate preheater (1), the non-condensable gas preheater (3) and the live steam preheater (4) are all plate-type heat exchangers.

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