Carbon-reduction nickel sulfate extraction wastewater treatment system

Abstract

The utility model discloses a carbon reduction nickel sulfate extraction wastewater treatment system, which belongs to the technical field of wastewater treatment equipment, and comprises a heating device, a separation device and an extraction device, the output end of the heating device is provided with a vertical pipe section with an upward conveying direction, and the extraction device is provided with an extraction feeding pipeline. The extraction feeding pipeline is connected to the vertical pipe section, and an obtuse angle is formed between the conveying direction of the extraction feeding pipeline and the conveying direction of the vertical pipe section; a linkage valve assembly is arranged between the circulating pipeline and the extraction feeding pipeline, and the linkage valve assembly is used for controlling opening and closing of the extraction feeding pipeline according to the concentration of wastewater in the circulating pipeline. The nickel sulfate extraction wastewater treatment device can automatically feed nickel sulfate extraction wastewater into a crystallization separation extraction stage when the concentration of the nickel sulfate extraction wastewater reaches a set threshold value, and can prevent the extraction feeding pipeline from being blocked based on the arrangement of the extraction feeding pipeline and the circulating pipeline in combination with the working control of the linkage valve assembly.

Description

Technical Field

[0001] The utility model relates to wastewater treatment equipment, in particular to a carbon-reducing nickel sulfate extraction wastewater treatment system. Background Art

[0002] The extraction of nickel sulfate mainly adopts the solvent extraction method. Solvent extraction generally requires saponification, and the saponification methods usually include sodium soap and ammonia soap. Sodium soap is a widely used method for saponification of organic solvent extraction, mainly through the saponification reaction of liquid alkali and various extractants (organic fatty acids). After adjusting the pH to about 6, high-salt and high-oil wastewater containing sodium sulfate is generated in the lower phase, and the resource treatment of this kind of wastewater needs to be considered. In addition, how to reduce carbon emissions is also one of the means for enterprises to enhance their technological competitiveness. Therefore, how to reduce carbon emissions in the process of wastewater treatment is also one of the research directions of enterprises. Content of the Utility Model

[0003] The utility model aims to solve at least one of the technical problems existing in the prior art. For this purpose, the utility model provides a carbon-reducing nickel sulfate extraction wastewater treatment system, which can effectively carry out the resource treatment of nickel sulfate extraction wastewater.

[0004] The carbon-reducing nickel sulfate extraction wastewater treatment system according to the embodiment of the utility model includes:

[0005] A heating device for heating the wastewater;

[0006] A separation device for gas-liquid separation of the wastewater and sending the separated liquid phase into the heating device;

[0007] An extraction device for extracting sodium sulfate from the wastewater with a concentration reaching a set threshold;

[0008] Wherein, a circulation pipeline is arranged at the output end of the heating device, the circulation pipeline is connected to the input end of the separation device, the circulation pipeline has a vertical pipe section with an upward conveying direction, the extraction device is provided with an extraction feed pipeline, the extraction feed pipeline is connected to the vertical pipe section, and the conveying direction of the extraction feed pipeline is distributed at an obtuse angle with the conveying direction of the vertical pipe section; a linkage valve assembly is arranged between the circulation pipeline and the extraction feed pipeline, and the linkage valve assembly is used to control the opening and closing of the extraction feed pipeline according to the concentration of the wastewater in the circulation pipeline.

[0009] The carbon-reducing nickel sulfate extraction wastewater treatment system according to the embodiment of the utility model has at least the following beneficial effects:

[0010] The carbon reduction nickel sulfate extraction wastewater treatment system of the present utility model heats and evaporates the nickel sulfate extraction wastewater through a heating device, and uses a separation device for gas-liquid separation, which can effectively increase the wastewater concentration. Then, after the wastewater concentration reaches the set threshold, a linkage valve assembly is used to open the extraction feed pipeline, and the wastewater with the reached concentration is sent into the extraction device. Among them, the extraction feed pipeline is a connecting vertical pipe section, and the angle between the conveying direction of the extraction feed pipeline and the vertical pipe section is an obtuse angle, that is, the extraction feed pipeline is inclined downward. Therefore, when feeding, it relies on the gravity of sodium sulfate to enter the extraction feed pipeline, and the wastewater continues to be sent into the separation device. When the concentration drops, the extraction feed pipeline closes automatically again.

[0011] Therefore, the present utility model can automatically enter the crystallization separation and extraction stage when the nickel sulfate extraction wastewater concentration reaches the set threshold. At the same time, based on the settings of the extraction feed pipeline and the circulation pipeline, combined with the working control of the linkage valve assembly, it can avoid blockage of the extraction feed pipeline. The extraction of sodium sulfate by using the extraction device can achieve resource treatment.

[0012] According to some embodiments of the present utility model, the linkage valve assembly includes:

[0013] A densitometer, provided in the circulation pipeline, for monitoring the wastewater concentration in the circulation pipeline;

[0014] A switch valve, provided in the extraction feed pipeline, for opening and closing adjustment according to the monitoring result of the densitometer.

[0015] According to some embodiments of the present utility model, the separation device includes:

[0016] A primary separator, the primary separator includes a primary feed port and a primary discharge port provided at the bottom, and a primary gas phase outlet provided at the top. The primary feed port is connected to the circulation pipeline, and the primary discharge port is connected to the heating device;

[0017] A secondary separator, the secondary separator includes a secondary feed port, a secondary discharge port and a secondary gas phase outlet. The secondary feed port is connected to the primary gas phase outlet, and the secondary discharge port is located at the bottom of the secondary separator and is connected to the liquid phase region of the primary separator through a separation return pipe.

[0018] According to some embodiments of the present utility model, a primary wire mesh is arranged below the primary gas phase outlet of the primary separator, and a secondary wire mesh is arranged below the secondary gas phase outlet of the secondary separator.

[0019] According to some embodiments of the present utility model, the heating device includes:

[0020] A steam compressor, for providing hot steam;

[0021] A heat exchanger, in which a first heat exchange channel and a first working medium channel are arranged inside the heat exchanger;

[0022] A preheater, in which a second heat exchange channel and a second working medium channel are arranged inside the preheater;

[0023] Wherein, the input end and the output end of the first heat exchange channel are correspondingly connected to the liquid phase output end of the separation device and the circulation pipeline, the input end and the output end of the first working medium channel are correspondingly connected to the output end of the steam compressor and the input end of the second working medium channel, and the output end of the second working medium channel is connected to the factory water pipe; the input end and the output end of the second heat exchange channel are correspondingly connected to the factory raw liquid pipe and the separation device.

[0024] According to some embodiments of the present invention, the gas phase output end of the separation device is connected to the steam compressor.

[0025] According to some embodiments of the present invention, the extraction device includes:

[0026] A salt washing mechanism, connected to the output end of the extraction feed pipeline;

[0027] A thickening mechanism, connected to the output end of the salt washing mechanism;

[0028] A centrifugal separation mechanism, connected to the output end of the thickening mechanism;

[0029] A mother liquor supply mechanism, connected to the mother liquor outlet of the centrifugal separation mechanism, and a first supply pipeline is arranged at the output end of the mother liquor supply mechanism, and the first supply pipeline is connected to the salt washing mechanism.

[0030] According to some embodiments of the present invention, a second supply pipeline is further arranged at the output end of the mother liquor supply mechanism, and the second supply pipeline is connected to the liquid phase area of the separation device.

[0031] According to some embodiments of the present invention, a third supply pipeline is further arranged at the output end of the mother liquor supply mechanism, and the third supply pipeline is connected to the front-end use pipe of the factory area.

[0032] According to some embodiments of the present invention, the centrifugal separation mechanism is provided with a first output pipe and a second output pipe, the first output pipe is connected between the mother liquor outlet and the mother liquor supply mechanism, and the second output pipe is connected between the product outlet of the centrifugal separation mechanism and the sodium sulfate decahydrate pipe.

[0033] Some additional aspects and advantages of the present invention will be given in the following description, some additional aspects and advantages will become obvious from the following description, or be understood through the practice of the present invention. Description of the Drawings

[0034] The present utility model will be further described below in conjunction with the drawings and embodiments, where:

[0035] Figure 1 is a schematic diagram of the overall structure of the present utility model;

[0036] Figure 2 is a schematic diagram of the structural composition of the heating device and the separation device;

[0037] Figure 3 is a schematic diagram of the structural composition of the extraction device.

[0038] In the figure:

[0039] 100 - separation device, 101 - primary separator, 102 - secondary separator;

[0040] 1011 - primary feed inlet, 1012 - primary discharge outlet, 1013 - primary gas phase outlet, 1014 - primary wire mesh;

[0041] 1021 - secondary feed inlet, 1022 - secondary discharge outlet, 1023 - secondary gas phase outlet, 1024 - secondary wire mesh, 1025 - separation return pipe;

[0042] 200 - heating device, 201 - heat exchanger, 202 - steam compressor, 203 - preheater, 204 - circulation pipeline;

[0043] 2031 - plant water pipe, 2032 - plant raw liquid pipe;

[0044] 2041 - vertical pipe section;

[0045] 300 - extraction device, 301 - salt washing mechanism, 302 - thickening mechanism, 303 - centrifugal separation mechanism, 304 - mother liquor supply mechanism, 305 - extraction feed pipeline;

[0046] 3041 - first supply pipeline, 3042 - second supply pipeline, 3043 - third supply pipeline, 3044 - plant front - end use pipe, 3045 - sodium sulfate decahydrate pipe;

[0047] 401 - densitometer, 402 - on - off valve. Detailed Embodiments

[0048] Embodiments of the present utility model will be described in detail below. Examples of the embodiments are shown in the accompanying drawings, where the same or similar reference numerals denote the same or similar elements or elements having the same or similar functions throughout. The embodiments described below by referring to the accompanying drawings are exemplary and are only used to explain the present utility model, and should not be construed as a limitation to the present utility model.

[0049] In the description of the present utility model, it should be understood that the orientation or positional relationship indicated by terms such as up and down, etc., which relate to the orientation description, is based on the orientation or positional relationship shown in the accompanying drawings. It is only for the convenience of describing the present utility model and simplifying the description, rather than indicating or implying 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 construed as a limitation to the present utility model.

[0050] In the description of the present utility model, "a plurality" means more than two. If there is a description of first and second, it is only for the purpose of distinguishing technical features and should not be construed as indicating or implying relative importance or implicitly indicating the quantity of the indicated technical features or implicitly indicating the sequence relationship of the indicated technical features.

[0051] In the description of the present utility model, unless otherwise clearly defined, terms such as "arrangement", "installation", "connection", etc. should be understood in a broad sense. Those skilled in the relevant technical field can reasonably determine the specific meanings of the above terms in the present utility model in combination with the specific content of the technical solution.

[0052] The extraction of nickel sulfate mainly uses the solvent extraction method. The solvent extraction method generally requires saponification, and the saponification methods usually include sodium soap and ammonia soap. Sodium soap is a widely used method for saponification of organic solvent extraction at present, mainly through the saponification reaction of liquid alkali and various extractants (organic fatty acids). After adjusting the pH to about 6, high-salt and high-oil wastewater containing sodium sulfate is generated in the lower phase, and the resource treatment of such wastewater needs to be considered.

[0053] In addition, since the dual-carbon goal was put forward, how to reduce carbon emissions has also become one of the means for enterprises to enhance their technological competitiveness. Therefore, how to reduce carbon emissions during the wastewater treatment process has also become one of the research directions of enterprises.

[0054] For this reason, the present utility model proposes a carbon-reducing nickel sulfate extraction wastewater treatment system, which can effectively carry out the resource treatment of nickel sulfate extraction wastewater.

[0055] Refer to Figure 1, A carbon-reducing nickel sulfate extraction wastewater treatment system according to an embodiment of the present utility model mainly includes a heating device 200, a separation device 100, and an extraction device 300. Among them, the heating device 200 is used to heat the wastewater, and the separation device 100 is used to perform gas-liquid separation on the wastewater and send the separated liquid phase to the heating device 200. The heating device 200 and the separation device 100 can cooperate to achieve the purpose of circulating and evaporating the wastewater. The extraction device 300 is used to extract sodium sulfate from the wastewater whose concentration reaches a set threshold.

[0056] It can be understood that the wastewater can be regarded as a solution containing sodium sulfate solute. After being heated by the heating device 200, part of the solvent will evaporate to form steam, increasing the concentration of the solute in the solution. Each time after the separation device 100 cooperates to perform gas-liquid separation, the concentration of the solution will increase accordingly. The extraction device 300 receives the solution for sodium sulfate extraction after the concentration of the wastewater reaches the set threshold.

[0057] Among them, a circulation pipeline 204 is provided at the output end of the heating device 200 for outputting the heated solution through the circulation pipeline 204.

[0058] The circulation pipeline 204 is connected to the input end of the separation device 100 to transport the heated solution into the separation device 100 for separation.

[0059] The circulation pipeline 204 has a vertical pipe section 2041 with an upward conveying direction. It can be understood that the conveying direction of the solution in the vertical pipe section 2041 is opposite to the direction of gravity.

[0060] The extraction device 300 is provided with an extraction feed pipeline 305. The extraction feed pipeline 305 is connected to the vertical pipe section 2041 for raw material feeding from the vertical pipe section 2041. The conveying direction of the extraction feed pipeline 305 is distributed at an obtuse angle to the conveying direction of the vertical pipe section 2041. Since the conveying direction of the vertical pipe section 2041 is upward, the conveying direction of the extraction feed pipeline 305 is inclined downward, that is, the extraction feed pipeline 305 is connected to the vertical pipe section 2041 in an inclined downward state.

[0061] A linkage valve assembly is provided between the circulation pipeline 204 and the extraction feed pipeline 305. The linkage valve assembly is used to control the opening and closing of the extraction feed pipeline 305 according to the concentration of the wastewater in the circulation pipeline 204, specifically including: opening the extraction feed pipeline 305 when the concentration of the wastewater in the circulation pipeline 204 reaches the set threshold, and closing the extraction feed pipeline 305 when the concentration of the wastewater in the circulation pipeline 204 is lower than the set threshold.

[0062] It can be understood that for the carbon reduction nickel sulfate extraction wastewater treatment system of the present utility model, the nickel sulfate extraction wastewater is heated and evaporated by the heating device 200, and gas-liquid separation is carried out by the separation device 100, which can effectively increase the wastewater concentration. Then, after the wastewater concentration reaches the set threshold, the extraction feed pipeline 305 is opened by the linkage valve assembly, and the wastewater with the reached concentration is sent into the extraction device 300.

[0063] Among them, the extraction feed pipeline 305 is connected to the vertical pipe section 2041, and the conveying direction between the extraction feed pipeline 305 and the vertical pipe section 2041 is an obtuse angle, that is, the extraction feed pipeline 305 is inclined downward. Therefore, when feeding, it relies on the gravity of sodium sulfate to enter the extraction feed pipeline 305. At this time, the circulation pipeline 204 is not closed, and the wastewater continues to be sent into the separation device 100, which is beneficial to increasing the concentration of sodium sulfate when entering the extraction feed pipeline 305. When the concentration drops, the extraction feed pipeline 305 closes automatically again.

[0064] Therefore, the present utility model can automatically send the nickel sulfate extraction wastewater into the crystallization separation and extraction stage when the concentration reaches the set threshold. At the same time, based on the settings of the extraction feed pipeline 305 and the circulation pipeline 204, combined with the working control of the linkage valve assembly, the blockage of the extraction feed pipeline 305 can be avoided. By extracting sodium sulfate through the extraction device 300, the resource treatment of the nickel sulfate extraction wastewater can be realized. On this basis, it is beneficial to reduce carbon emissions.

[0065] Refer to Figure 1 and Figure 3 , in some embodiments of the present utility model, the linkage valve assembly includes a densitometer 401 and a switching valve 402.

[0066] The densitometer 401 is arranged on the circulation pipeline 204 for monitoring the wastewater concentration in the circulation pipeline 204. The switching valve 402 is arranged on the extraction feed pipeline 305 for controlling the opening and closing of the extraction feed pipeline 305. Among them, the feedback signal of the densitometer 401 is fed back to the switching valve 402, so that the switching valve 402 opens the extraction feed pipeline 305 when the wastewater concentration in the circulation pipeline 204 reaches the set threshold, and closes the extraction feed pipeline 305 when the wastewater concentration in the circulation pipeline 204 is lower than the set threshold.

[0067] With the structural setting of this embodiment, the densitometer 401 is used to monitor the concentration in the circulation pipeline 204 in real time. The monitoring result is reliable and timely, which can effectively ensure the smooth progress of the mechanism of "sending the wastewater with the reached concentration threshold into the extraction device 300".

[0068] Specifically, refer to Figure 3, taking the connection point of the extraction feed pipe 305 as the boundary, the vertical pipe section 2041 includes a first pipe section and a second pipe section distributed up and down. The densitometer 401 is arranged on the first pipe section, and an obtuse angle of 120° is formed between the extraction feed pipe 305 and the first pipe section. Moreover, the separation device 100 is directly connected to the upper end of the first pipe section.

[0069] With the structural arrangement of this embodiment, the monitoring point of the densitometer 401 is located behind the extraction feed pipe 305, and the monitoring result is more accurate, which can effectively avoid the influence of the pipe length on the concentration.

[0070] With the 120° angle arrangement, when sodium sulfate is conveyed upward with the solution to flow through the port of the extraction feed pipe 305, under the action of the negative pressure formed by the opening of the extraction feed pipe 305 and the gravity of sodium sulfate itself, the solution rich in sodium sulfate can quickly enter the extraction feed pipe 305 to avoid blockage.

[0071] Furthermore, the diameter of the extraction feed pipe 305 is smaller than that of the vertical pipe section 2041.

[0072] In some embodiments, the diameter of the vertical pipe section 2041 uses a DN800 pipe, and the extraction feed pipe 305 uses a DN40 pipe to ensure the feeding efficiency of the extraction feed pipe 305. When the extraction feed pipe 305 is opened, the solution will quickly enter the extraction feed pipe 305 under the action of the conveying pressure of the vertical pipe section 2041 combined with gravity, so that the wastewater with a concentration reaching the threshold value is quickly sent to the extraction device 300 for extraction. During this process, as the original solution of the wastewater is fed in, the concentration of the wastewater will decrease accordingly. When it drops below the set threshold value, the on-off valve 402 closes the extraction feed pipe 305 again.

[0073] In some embodiments of the present utility model, referring to Figure 2 , the separation device 100 includes a primary separator 101 and a secondary separator 102.

[0074] The primary separator 101 has a primary feed inlet 1011 and a primary discharge outlet 1012 provided at the bottom, and a primary gas phase outlet 1013 provided at the top. Specifically, the bottom of the primary separator 101 is conical. The primary feed inlet 1011 is arranged at the lower end of the primary separator 101 and is connected to the circulation pipe 204. The primary discharge outlet 1012 is arranged on the conical side wall and is connected to the heating device 200.

[0075] The secondary separator 102 has a secondary feed inlet 1021, a secondary discharge outlet 1022 and a secondary gas phase outlet 1023. The secondary feed inlet 1021 is connected to the primary gas phase outlet 1013. The secondary discharge outlet 1022 is located at the lower end of the secondary separator 102 and is connected to the liquid phase area of the primary separator 101 through a separation return pipe 1025.

[0076] During operation, the wastewater is first fed into the first-stage separator 101. After gas-liquid separation in the first-stage separator 101, the liquid phase is fed into the heating device 200 through the first-stage discharge port 1012 for reheating. The gas phase is fed into the second-stage separator 102 through the first-stage gas phase outlet 1013. After gas-liquid separation in the second-stage separator 102, the condensed liquid phase is sent back to the liquid phase area of the first-stage separator 101 through the second-stage discharge port 1022 and the separation return pipe 1025.

[0077] It can be understood that to send it back to the liquid phase area, it is only necessary to set the connection height of the separation return pipe 1025 to the first-stage separator 101 below the liquid level of the first-stage separator 101. Refer to Figure 2 , the installation height of the second-stage separator 102 is higher than that of the first-stage separator 101 to prevent the liquid phase in the first-stage separator 101 from flowing back into the second-stage separator 102.

[0078] Continue to refer to Figure 2 , in some embodiments of the present invention, a first-stage wire mesh 1014 is arranged below the first-stage gas phase outlet 1013 of the first-stage separator 101, and a second-stage wire mesh 1024 is arranged below the second-stage gas phase outlet 1023 of the second-stage separator 102 to prevent foam from entering the first-stage gas phase outlet 1013 and the second-stage gas phase outlet 1023.

[0079] Continue to refer to Figure 2 , in some embodiments of the present invention, the heating device 200 includes a steam compressor 202, a heat exchanger 201, and a preheater 203.

[0080] The steam compressor 202 is used to generate hot steam. A first heat exchange channel and a first working medium channel are arranged inside the heat exchanger 201, and a second heat exchange channel and a second working medium channel are arranged inside the preheater 203.

[0081] The input end of the first working medium channel is connected to the output end of the steam compressor 202 and is used to receive the hot steam sent by the steam compressor 202. The output end of the first working medium channel is connected to the input end of the second working medium channel and is used to send the steam and condensate after heat exchange with the heat exchanger 201 into the preheater 203. The output end of the second working medium channel is connected to the plant water pipe 2031 and is used to send the condensate back to the plant for reuse, which can effectively reduce carbon emissions. The input end of the first heat exchange channel is connected to the first-stage discharge port 1012 of the first-stage separator 101 and is used to receive the liquid phase after gas-liquid separation. The output end of the first heat exchange channel is connected to the circulation pipeline 204 and is used to send the heated wastewater into the first-stage separator 101 again through the circulation pipeline 204. The input end of the second heat exchange channel is connected to the plant raw liquid pipe 2032 and is used to send the raw wastewater. The output end of the second heat exchange channel is connected to the first-stage separator 101 and is used to send the preheated raw wastewater into the first-stage separator 101. In actual application, the second heat exchange channel can be directly connected to the circulation pipeline 204 or directly connected to the first-stage separator 101.

[0082] With the structural arrangement of this embodiment, the steam is utilized twice, making full use of the latent heat of the steam and having high energy efficiency. At the same time, there is no condensate that needs to be discharged for treatment, which can reduce carbon emissions.

[0083] In some embodiments of the present invention, the gas-phase output end of the separation device 100 is connected to the steam compressor 202 to realize the recycling of the gas phase and use it as one of the steam sources, which helps to reduce the steam consumption introduced into the entire system.

[0084] Refer to Figure 3 , in some embodiments of the present invention, the extraction device 300 includes a salt washing mechanism 301, a thickening mechanism 302, a centrifugal separation mechanism 303, and a mother liquor supply mechanism 304.

[0085] The salt washing mechanism 301 is connected to the output end of the extraction feed pipeline 305. Specifically, a salt washing tank is provided, and the height of the salt washing tank is lower than that of the extraction feed pipeline 305, so as to receive the wastewater sent from the extraction feed pipeline 305 and carry out a crystallization reaction. The thickening mechanism 302 is connected to the output end of the salt washing mechanism 301 and is used to receive the crystal slurry in the salt washing tank and thicken it. Specifically, a thickening tank is provided. The centrifugal separation mechanism 303 is connected to the output end of the thickening mechanism 302 and is used to extract sodium sulfate decahydrate, and at the same time send the separated mother liquor into the mother liquor supply mechanism 304. Specifically, the centrifugal separation mechanism 303 is provided with a mother liquor outlet and a product outlet. Among them, the product outlet is provided with a second output pipe, which is connected to the sodium sulfate decahydrate pipe 3045 through the second output pipe, and is directly discharged into the sodium sulfate decahydrate pipe 3045 when sodium sulfate decahydrate is separated. The mother liquor outlet is provided with a first output pipe, which is connected to the mother liquor supply mechanism 304 through the first output pipe and is used to directly send the separated mother liquor into the mother liquor supply mechanism 304. The mother liquor supply mechanism 304 is specifically provided with a mother liquor tank, and the output end of the mother liquor tank is provided with a first supply pipeline 3041, and the first supply pipeline 3041 is connected to the salt washing mechanism 301.

[0086] Continue to refer to Figure 3 , in some embodiments, a second supply pipeline 3042 is further provided at the output end of the mother liquor supply mechanism 304, and the second supply pipeline 3042 is connected to the liquid phase area of the separation device 100. It can be understood that the second supply pipeline 3042 is specifically connected to the liquid phase area of the primary separator 101.

[0087] Continue to refer to Figure 3 , in some embodiments, a third supply pipeline 3043 is further provided at the output end of the mother liquor supply mechanism 304, and the third supply pipeline 3043 is connected to the front-end use pipe 3044 of the plant area for front-end production use. Specifically, it includes sending the mother liquor into the extraction process of nickel sulfate for application.

[0088] In order to avoid blockage, in some embodiments of the present invention, the centrifugal separation mechanism 303 is arranged below the thickening mechanism 302, and the pipeline distance between the centrifugal separation mechanism 303 and the thickening mechanism 302 is less than or equal to 1 m to avoid blockage.

[0089] It should be noted that the transportation of relevant working fluids or solutions can be configured with a pump body for pumping, which will not be described in detail here, and relevant pipelines can be controlled for starting and stopping transportation by valves.

[0090] Refer to Figures 1 to 3 As shown, in some embodiments of the present invention, the carbon-reduced nickel sulfate extraction wastewater treatment system includes a heating device 200, a separation device 100, and an extraction device 300:

[0091] The separation device 100 includes a primary separator 101 and a secondary separator 102. The primary separator 101 has a primary feed inlet 1011 and a primary discharge outlet 1012 provided at the bottom, and a primary gas phase outlet 1013 provided at the top. Specifically, the bottom of the primary separator 101 is conical, the primary feed inlet 1011 is provided at the lower end of the primary separator 101, and the primary discharge outlet 1012 is provided on the conical side wall. The secondary separator 102 has a secondary feed inlet 1021, a secondary discharge outlet 1022, and a secondary gas phase outlet 1023. The secondary feed inlet 1021 is connected to the primary gas phase outlet 1013, the secondary discharge outlet 1022 is located at the lower end of the secondary separator 102, and is connected to the liquid phase region of the primary separator 101 through a separation reflux pipe 1025. The primary separator 101 is provided with a primary wire mesh 1014 below the primary gas phase outlet 1013, and the secondary separator 102 is provided with a secondary wire mesh 1024 below the secondary gas phase outlet 1023.

[0092] The heating device 200 includes a steam compressor 202, a heat exchanger 201, and a preheater 203. The steam compressor 202 is used to generate hot steam. The heat exchanger 201 defines a first heat exchange channel and a first working medium channel. The input end of the first working medium channel is connected to the output end of the steam compressor 202 and is used to receive the hot steam sent by the steam compressor 202. The output end of the first heat exchange channel is provided with a circulation pipeline 204, and the output end of the circulation pipeline 204 is connected to the primary feed inlet 1011 and is used to send the heated wastewater into the primary separator 101 through the circulation pipeline 204. The input end of the first heat exchange channel is connected to the primary discharge outlet 1012 of the primary separator 101. The preheater 203 defines a second heat exchange channel and a second working medium channel. The input end of the second working medium channel is connected to the output end of the first working medium channel, and the output end of the second working medium channel is connected to the plant water supply to recover and use the condensed water. The input end of the second heat exchange channel is for feeding the original wastewater, and the output end of the second heat exchange channel is connected to the primary separator 101 or the circulation pipeline 204 and is used to be sent back into the heating device 200 after separation. The secondary gas phase outlet 1023 is connected to the steam compressor 202.

[0093] The extraction device 300 includes a salt washing mechanism 301, a thickening mechanism 302, a centrifugal separation mechanism 303, and a mother liquor supply mechanism 304. The salt washing mechanism 301 is connected to the output end of the extraction feed pipeline 305, and is specifically provided with a salt washing tank. The height of the salt washing tank is lower than that of the extraction feed pipeline 305, and is used to receive the wastewater sent from the extraction feed pipeline 305 and carry out a crystallization reaction. The thickening mechanism 302 is connected to the output end of the salt washing mechanism 301, and is used to receive the crystal slurry in the salt washing tank and thicken it. Specifically, a thickening tank is provided. The centrifugal separation mechanism 303 is located below the thickening tank and is connected to the bottom of the thickening tank, and is used to extract sodium sulfate decahydrate and separate the mother liquor into the mother liquor supply mechanism 304. The pipeline distance between the centrifugal separation mechanism 303 and the thickening tank is less than or equal to 1 m to avoid material blockage as much as possible. The mother liquor supply mechanism 304 is specifically provided with a mother liquor tank, and the output end of the mother liquor tank is provided with a first supply pipeline 3041. The first supply pipeline 3041 is connected to the salt washing mechanism 301. The output end of the mother liquor supply mechanism 304 is also provided with a second supply pipeline 3042 and a third supply pipeline 3043. The second supply pipeline 3042 is connected to the liquid phase area of the first-stage separator 101, and the third supply pipeline 3043 is used to transport the mother liquor for front-end production use.

[0094] In summary, the carbon-reducing nickel sulfate extraction wastewater treatment system in the present utility model has the following advantages:

[0095] 1. This system can achieve automatic operation, and it is not easy to have pipeline blockage problems during the operation process.

[0096] 2. Zero discharge and resource utilization of nickel sulfate extraction wastewater can be achieved, effectively reducing carbon emissions. Through the implementation of this system, sodium sulfate with high purity can be obtained, which has good social and economic benefits.

[0097] 3. This system is provided with two-stage wire meshes, and the conductivity of the evaporated distilled water ≤ 100 μs / cm, meeting the plant reuse standard and reducing the external discharge of plant wastewater.

[0098] 4. By reasonably designing the automatic control points, this system has a high degree of automation and less human intervention.

[0099] 5. The operation difficulty for personnel is low, the equipment composition of the whole system is relatively streamlined, and the equipment investment is less.

[0100] The above has described the present utility model in detail in conjunction with the embodiments. However, the present utility model is not limited to the above embodiments. Within the scope of knowledge possessed by those of ordinary skill in the art, various changes can also be made without departing from the purpose of the present utility model.

Claims

1. A carbon-reducing nickel sulfate extraction wastewater treatment system, characterized in that: include: A heating device, used for heating the wastewater; A separation device, used for separating the wastewater into gas and liquid, and sending the separated liquid phase to the heating device; An extraction device for extracting sodium sulfate from wastewater having a concentration reaching a set threshold; Among them, a circulation pipeline is provided at the output end of the heating device, and the circulation pipeline is connected to the input end of the separation device. The circulation pipeline has a vertical pipe section with an upward conveying direction. The extraction device is provided with an extraction feed pipeline, and the extraction feed pipeline is connected to the vertical pipe section, and the conveying direction of the extraction feed pipeline is distributed at an obtuse angle to the conveying direction of the vertical pipe section; a linkage valve assembly is provided between the circulation pipeline and the extraction feed pipeline, and the linkage valve assembly is used to control the opening and closing of the extraction feed pipeline according to the wastewater concentration in the circulation pipeline.

2. The system for treating wastewater from the extraction of nickel sulfate with carbon reduction according to claim 1, characterized in that: The linkage valve assembly comprises: A densitometer, provided in the circulation pipeline, for monitoring the wastewater concentration in the circulation pipeline; The switch valve is arranged on the extraction feed pipeline and is used for opening and closing adjustment according to the monitoring result of the density meter.

3. The system for treating wastewater from nickel sulfate extraction with carbon reduction according to claim 1, characterized in that: The separation device comprises: A primary separator, the primary separator comprising a primary feed inlet and a primary discharge inlet provided at the bottom, and a primary gas phase outlet provided at the top, the primary feed inlet being connected to the circulation pipeline, and the primary discharge inlet being connected to the heating device; A secondary separator, the secondary separator comprises a secondary feed port, a secondary discharge port and a secondary gas phase outlet, the secondary feed port is connected to the primary gas phase outlet, the secondary discharge port is located at the bottom of the secondary separator and is connected to the liquid phase region of the primary separator through a separation reflux pipe.

4. The system for treating wastewater from nickel sulfate extraction with carbon reduction according to claim 3, characterized in that: The first-stage separator is provided with a first-stage wire mesh below the first-stage gas phase outlet, and the second-stage separator is provided with a second-stage wire mesh below the second-stage gas phase outlet.

5. The system for treating wastewater from nickel sulfate extraction with carbon reduction according to claim 1, characterized in that: The heating device comprises: Steam compressor, used to provide hot steam; A heat exchanger, wherein a first heat exchange channel and a first working medium channel are arranged inside the heat exchanger; A preheater, wherein a second heat exchange channel and a second working medium channel are arranged inside the preheater; Among them, the input end and output end of the first heat exchange channel are correspondingly connected to the liquid phase output end of the separation device and the circulation pipeline, the input end and output end of the first working fluid channel are correspondingly connected to the output end of the steam compressor and the input end of the second working fluid channel, and the output end of the second working fluid channel is connected to the plant water pipe; the input end and output end of the second heat exchange channel are correspondingly connected to the plant raw liquid pipe and the separation device.

6. The system for treating wastewater from nickel sulfate extraction with carbon reduction according to claim 5, characterized in that: The gas phase output end of the separation device is connected to the steam compressor.

7. The system for treating wastewater from nickel sulfate extraction with carbon reduction according to claim 1, characterized in that: The extraction device comprises: A salt washing mechanism connected to the output end of the extraction feed pipeline; A thickening mechanism connected to the output end of the salt washing mechanism; A centrifugal separation mechanism connected to the output end of the thickening mechanism; The mother liquid supply mechanism is connected to the mother liquid outlet of the centrifugal separation mechanism. The output end of the mother liquid supply mechanism is provided with a first supply pipeline, and the first supply pipeline is connected to the salt washing mechanism.

8. The system for treating wastewater from nickel sulfate extraction with carbon reduction according to claim 7, characterized in that: A second supply pipeline is also provided at the output end of the mother liquid supply mechanism, and the second supply pipeline is connected to the liquid phase region of the separation device.

9. The system for treating wastewater from nickel sulfate extraction with carbon reduction according to claim 7, characterized in that: A third supply pipeline is also arranged at the output end of the mother liquid supply mechanism, and the third supply pipeline is connected to the use pipe at the front end of the plant area.

10. The system for treating wastewater from nickel sulfate extraction with carbon reduction according to claim 7, characterized in that: The centrifugal separation mechanism is provided with a first output pipe and a second output pipe, wherein the first output pipe is connected between the mother liquor outlet and the mother liquor supply mechanism, and the second output pipe is connected between the product outlet of the centrifugal separation mechanism and a sodium sulfate decahydrate pipe.

Images