An MVR evaporation crystallizer

Abstract

The present invention discloses an MVR evaporation crystallizer, comprising a separator, the separator being provided with a separation inlet, a separation outlet, a circulation outlet, a circulation inlet, a secondary steam outlet, and a mother liquor reflux port; a spray pipe provided within the separator, the spray pipe being provided with a spray head; a heater provided with a raw steam inlet, a condensed water outlet, a heating inlet, and a heating outlet; a circulating pump; a compressor; and a slurry separation assembly for separating solids from the mother liquor discharged from the separation outlet and conveying the mother liquor from which the solids have been separated to the mother liquor reflux port. By providing the spray pipe and the spray head within the separator, the MVR evaporation crystallizer forms a spray mist of wastewater circulating into the separator, significantly increasing the surface area, facilitating evaporation, forming secondary steam, reducing concentration time, and lowering processing costs.

Description

Technical Field

[0001] The invention relates to the technical field of wastewater evaporation and concentration, in particular to an MVR evaporation crystallizer. Background Art

[0002] The MVR evaporator crystallizer is a common treatment device used for evaporation, concentration, and crystallization of industrial wastewater. Its principle is to use a high-efficiency steam compressor to compress the secondary steam produced by evaporation, raising its pressure and temperature. This steam, with its increased thermal energy, is then pumped into a heater to further heat the raw liquid, which then continues to evaporate and produce secondary steam, thus achieving a continuous evaporation state. The core of MVR technology is to use the heat of the secondary steam, increasing its temperature through compression, as a heat source to replace fresh steam. This involves adding some compressor work to achieve cyclic evaporation, eliminating the need for external fresh steam and relying on the evaporation system's self-circulation to achieve evaporation and concentration. This fully utilizes steam that would otherwise be discarded, recovering latent heat and improving thermal efficiency. Theoretically, using an MVR evaporator saves over 60%-80% of energy and over 90% of cooling water compared to conventional evaporators.

[0003] However, during the operation of the existing MVR evaporation crystallizer, industrial wastewater materials are deposited at the bottom of the evaporator, the heating area is small, the volatilization efficiency is low, and a large amount of steam is required; and when the secondary steam is formed, liquid droplets are mixed in the secondary steam and need to be separated by a gas-liquid separator. The additional gas-liquid separator increases the floor space and processing cost of the MVR evaporation crystallization device; in addition, the secondary steam outlet and the material turbid liquid outlet of the evaporator are usually arranged at the top and bottom of the evaporator respectively, with a large height difference, which makes assembly inconvenient; and when the compressor compresses the secondary steam, it usually works on the secondary steam to form superheated steam. Since superheated steam is not easy to condense, the heat exchange efficiency is low, the processing time is extended, and the processing cost is increased; and the clear liquid discharged from the clear liquid outlet of the evaporator is usually thickened by a thickener. During the processing process, the continuous discharge of the clear liquid causes large fluctuations in the liquid level inside the thickener, making it difficult to accurately measure the liquid level, resulting in an imbalance in the pressure inside the thickener, affecting the reflux of the mother liquor to the evaporator, further reducing the waste liquid treatment efficiency.

[0004] Therefore, it is necessary to improve the MVR evaporation crystallizer in the prior art. Summary of the Invention

[0005] The purpose of the present invention is to overcome the defects in the prior art and provide an MVR evaporation crystallizer which is easy to assemble, improves efficiency and reduces cost.

[0006] In order to achieve the above technical effects, the technical solution of the present invention is: an MVR evaporation crystallizer, comprising:

[0007] A separator, wherein the separator is provided with a separation inlet, a separation outlet, a circulation outlet, a circulation inlet, a secondary steam outlet and a mother liquor reflux port, a spray pipe connected to the circulation outlet is provided at the top of the separator, and a spray head is provided on the spray pipe;

[0008] A heater, wherein the heater is provided with a raw steam inlet, a condensed water outlet, a heating inlet and a heating outlet, and the heating outlet is connected to the circulation inlet;

[0009] a circulation pump, wherein the input end of the circulation pump is connected to the circulation outlet, and the output end of the circulation pump is connected to the heating input end;

[0010] a compressor, wherein the input end of the compressor is connected to the secondary steam outlet, and the output end of the compressor is connected to the raw steam inlet;

[0011] A slurry separation component is used to separate solids from the mother liquor discharged from the separation outlet, and to transport the mother liquor from which the solids are separated to the mother liquor reflux port.

[0012] When the MVR evaporation crystallizer of the above technical solution is used, industrial wastewater enters the interior of the separator through the separation inlet, and is evaporated and crystallized through heating, concentration, and during this process, the wastewater flows out through the circulation outlet, is pumped by the circulation pump, and transported to the heater. The raw steam enters the heater from the raw steam inlet, exchanges heat with the wastewater in the heater, and the raw steam cools down to form condensed water, which is discharged from the condensed water outlet. At the same time, the heated industrial wastewater is discharged from the heating outlet, enters the spray pipe in the separator through the circulation inlet, and is sprayed out from the spray head in the separator. Compared with the existing technology, the surface area of the wastewater is increased by evaporation, which is more conducive to removing moisture, shortening the evaporation time, and improving the wastewater treatment efficiency. During the wastewater concentration process, the wastewater is heated to generate steam, which is called secondary steam. The secondary steam is discharged through the secondary steam outlet and enters the compressor. After the compressor performs work on the secondary steam, the temperature rises, forming raw steam. It enters the heater through the raw steam inlet, continuously heating the industrial wastewater entering the heater through the heating inlet, thereby reducing the use of raw steam and saving energy. After being heated, the industrial wastewater in the heater enters the separation gas, where it is sprayed to increase the surface area, facilitate evaporation, and accelerate the concentration of the industrial wastewater. After the industrial wastewater is concentrated to a certain concentration, it is discharged through the separation outlet and enters the crystal slurry separation component, which separates the concentrated liquid into solids and liquids to separate the solids. The liquid with the separated solids, i.e., the mother liquor, is then transported to the separator through the mother liquor reflux port to achieve continuous evaporation and concentration of the mother liquor.

[0013] Preferably, it also includes a condensate tank, a condensate pump and a condensate preheater, the input end of the condensate pump is connected to the condensate outlet through the condensate tank, the heat medium inlet of the condensate preheater is connected to the output end of the condensate pump, the heat medium outlet is connected to the outside world, the feed port is used to input industrial waste water, and the discharge port is connected to the separation inlet; the output end of the condensate pump is also connected to the output end of the compressor.

[0014] By adopting the above technical solution, condensed water is formed after the raw steam exchanges heat with industrial wastewater in the heater. The condensed water is discharged from the condensed water outlet and enters the condensed water tank. The condensed water pump is started to pass the condensed water into the condensed water heat exchanger. The feed port of the condensed water heat exchanger is used to pass industrial wastewater. Since the temperature of industrial wastewater is generally lower than the condensed water formed after the raw steam is condensed, the condensed water can exchange heat with the industrial wastewater, thereby realizing preheating treatment of the industrial wastewater. The preheated industrial wastewater is then passed into the separator, and the temperature of the condensed water after heat transfer is reduced and can be discharged to the outside, thereby making full use of the heat of the condensed water, reducing the energy consumption of evaporation and concentration, and achieving energy saving.

[0015] Preferably, an isolation cylinder and a flushing pipe are provided in the separator, and the isolation cylinder and the separator are connected via a closed-loop wire mesh foam trap, the wire mesh foam trap is located below the secondary steam outlet, the spray head is provided on the inner side of the isolation cylinder, the flushing pipe is connected to a flushing head, the flushing head is located directly below and facing the wire mesh foam trap, the separator is provided with a condensate flushing port connected to the flushing pipe, and the condensate flushing port is connected to the output end of the condensate pump. In addition, the condensate pump can also transport condensate to the output end of the compressor, where the condensate contacts the superheated saturated steam at the output end of the compressor, thereby mixing to form saturated steam, so that the saturated steam can enter the heater, ensuring efficient heat exchange of the industrial wastewater flowing in the heater.

[0016] By adopting the above technical solution, the wire mesh foam catcher arranged in the separator can separate the droplets entrained by the secondary steam when it rises, so as to ensure that when the wastewater evaporates and concentrates, the wire mesh foam catcher captures the droplets, so that the adjacent secondary steam is passed into the compressor. In this way, there is no need to set up a gas-liquid separator outside the separator to separate the secondary steam and the droplets. On the one hand, it reduces the total cost of the equipment, and on the other hand, it makes the device structure more compact and reduces the occupied space. In addition, when the equipment is in long-term operation, the wire mesh foam catcher is prone to blockage. At this time, the condensate pump transports the condensate to the condensate flushing port, so that the condensate enters the flushing pipe and is sprayed out from the flushing head to clean the wire mesh foam catcher above the flushing head, so that the steam can be discharged smoothly through the secondary steam outlet.

[0017] Preferably, an isolation sleeve is further provided in the separator, and the isolation sleeve is located directly below the flushing pipe. The top circumferential outer edge of the isolation sleeve is fixedly connected to the circumferential inner wall of the separator, and there is a gap between the bottom of the isolation sleeve and the bottom of the separator. The circulation outlet and the secondary steam inlet are both arranged on the circumferential side wall of the separator, the circulation outlet is arranged adjacent to the top of the isolation sleeve, and the secondary steam outlet is arranged adjacent to the wire mesh foam catcher.

[0018] By adopting the above technical solution, the inner cavity of the separator is divided into two parts, the lower part, by using an isolation sleeve. The lower part is used to deposit industrial wastewater, which can be discharged from the circulation outlet, and the upper part is for the spray head to spray the heated wastewater downward, thereby increasing the surface area and facilitating evaporation to form secondary steam, which is then discharged from the secondary steam outlet. Since the circulation outlet is close to the top of the isolation sleeve, and the secondary steam outlet is close to the wire mesh foam catcher, the height difference between the circulation outlet and the secondary steam outlet is greatly reduced, making it convenient to connect the pipeline at the circulation outlet and the secondary steam outlet, thereby facilitating the assembly of the equipment.

[0019] Preferably, the isolation sleeve includes a partition and a connecting pipe, the partition is in a closed loop, the partition has a guide plate inclined downward, and the circumferential inner wall of the partition is fixedly connected to the top circumferential outer edge of the connecting pipe.

[0020] By adopting the above technical solution, the downward-inclined guide surface of the partition is utilized to facilitate the spray water sprayed from the sprinkler head to fall on the guide surface, flow downward, enter the connecting pipe, flow out from the bottom of the connecting pipe, and settle at the bottom of the separator. When the wastewater is deposited to a certain height, the wastewater flows out through the circulation outlet so that it can be heated and sprayed again, thereby realizing continuous heating, concentration, evaporation and crystallization of the wastewater.

[0021] Preferably, a waste steam preheater is further provided between the condensate preheater and the separator, a waste steam outlet is provided on the heater, the heat medium inlet of the waste steam preheater is connected to the waste steam outlet, the heat medium outlet is connected to the condensate tank, the feed port is connected to the discharge port of the condensate preheater, and the discharge port is connected to the separation inlet.

[0022] By adopting the above technical solution, when the raw steam heats the wastewater in the separator, part of it condenses to form condensed water, and part of it forms exhaust steam. The temperature of the exhaust steam is high enough for condensed water, so the exhaust steam is introduced into the exhaust steam preheater, and the industrial wastewater preheated by the condensed water preheater first enters the exhaust steam preheater before entering the separator. The industrial wastewater and the exhaust steam exchange heat, thereby realizing secondary preheating treatment of the industrial wastewater. After the secondary preheating treatment is completed, the industrial wastewater is introduced into the separator for evaporation, concentration and crystallization, and the temperature of the preheated exhaust steam drops to form condensed water, which is introduced into the condensate tank for extraction and use by the condensate pump. The industrial wastewater is preheated once or used to clean the wire mesh foam collector, saving water consumption and reducing treatment costs.

[0023] Preferably, the slurry separation component includes a discharge pump, a slurry tank, a centrifuge, a mother liquid tank and a mother liquid pump. The slurry tank has a slurry inlet, a sedimentation outlet and a clear liquid overflow port. The separation outlet is connected to the slurry inlet through the discharge pump, the sedimentation outlet is connected to the mother liquid tank through the centrifuge, the clear liquid overflow port is connected to the mother liquid tank, and the mother liquid tank is connected to the mother liquid reflux port through the mother liquid pump.

[0024] By adopting the above technical solution, after the wastewater is heated and evaporated, a thick slurry is formed. After being discharged from the separation outlet, the discharge pump is started, and the slurry enters the slurry tank through the slurry inlet for deposition. The crystal particles are deposited at the bottom of the slurry tank, while the clear liquid is located at the upper part and is discharged from the clear liquid overflow port into the mother liquid tank. The crystal particles carry part of the clear liquid into the centrifuge, and the centrifuge performs centrifugal treatment to separate the solid and the liquid. The separated liquid, that is, the mother liquor, enters the mother liquor tank again. The mother liquor tank is started and connected to the mother liquor reflux port, so that the mother liquor enters the separator again for further evaporation treatment.

[0025] Preferably, a spoiler is provided in the slurry tank, the circumferential outer edge of the spoiler is fixedly connected to the circumferential inner wall of the slurry tank, the inner side of the spoiler extends upward along the circumference of the slurry tank and the inner top of the spoiler is serrated, and the clear liquid overflow port is provided between the top and bottom ends of the spoiler.

[0026] By adopting the above technical solution, the serrated design of the inner top of the spoiler is used to interfere with the fluctuation of the liquid in the slurry tank, prevent the fluctuation of the liquid level in the slurry tank, facilitate the measurement of the liquid level, and maintain the pressure balance in the slurry tank. At the same time, the serrated design can intercept some of the solid particles entrained by the clear liquid, so that the solid particles settle to the bottom of the slurry tank, to ensure that the clarified mother liquor flows through the top of the serrated spoiler to the clear liquid overflow port, and enters the mother liquor tank through the clear liquid overflow port.

[0027] Preferably, the slurry inlet is arranged to be inclined downward and tangent to the circumferential inner wall of the slurry tank.

[0028] By adopting the above technical solution, the thick wastewater liquid entering the slurry tank has a certain initial velocity, and moves downward in a spiral along the tube wall of the slurry tank, depositing the solid shell at the bottom of the slurry tank. After the liquid flows to the bottom, it spirals upward again, causing the liquid level to rise, making it easier for the clarified liquid to be discharged through the clear liquid overflow port.

[0029] Preferably, a salt collecting tank is provided at the bottom of the separator, and the salt collecting tank is connected to the discharge pump.

[0030] By adopting the above technical solution, the salt collecting tank is used to conveniently deposit thick industrial wastewater. After opening the separation outlet, the discharge pump is started, and the wastewater carrying the crystal shell is sent into the slurry tank for solid-liquid separation.

[0031] In summary, compared with the prior art, the MVR evaporation crystallizer of the present invention provides a spray pipe and a spray head in the separator, so that the wastewater circulating into the separator is formed in the form of a spray mist, which greatly increases the surface area, facilitates evaporation, forms secondary steam, shortens the concentration time, and reduces the treatment cost. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] Figure 1 It is a structural schematic diagram of the MVR evaporation crystallizer of the present invention;

[0033] Figure 2 It is a structural schematic diagram of the separator of the present invention;

[0034] Figure 3 It is a structural schematic diagram of the heater of the present invention;

[0035] Figure 4 It is a structural schematic diagram of the slurry tank of the present invention;

[0036] Figure 5 It is a schematic diagram of the circulating heating and concentration of industrial wastewater of the present invention;

[0037] Figure 6 It is a schematic structural diagram of the slurry separation component of the present invention;

[0038] Figure 7 It is a schematic diagram of recycling secondary steam and condensed water according to the present invention;

[0039] Figure 8 is a schematic diagram of the present invention using steam and condensed water;

[0040] Figure 9 is a schematic diagram of the present invention using raw steam;

[0041] Figure 101 is a schematic diagram of a process using exhaust steam in the present invention;

[0042] In the figure: 100, separator; 101, separation inlet; 102, separation outlet; 103, circulation outlet; 104, circulation inlet; 105, secondary steam outlet; 106, mother liquor reflux port; 107, condensate flushing port; 200, spray pipe; 300, spray head; 400, heater; 401, raw steam inlet; 402, condensate outlet; 403, heating inlet; 404, heating outlet; 405, exhaust steam outlet; 500, circulation pump; 600, compressor; 700, condensate tank; 800, condensate pump; 900, condensate preheater; 110, isolation cylinder; 120, flushing pipe; 130, wire mesh foam catcher; 140, flushing head; 150, isolation sleeve; 151, partition; 152, connecting pipe; 160, exhaust steam preheater; 170, discharge pump; 180, slurry tank; 181, slurry inlet; 182, sedimentation outlet; 183, clear liquid overflow port; 190, centrifuge; 210, mother liquor tank; 220, mother liquor pump; 230, spoiler; 240, salt collecting tank. DETAILED DESCRIPTION

[0043] The following embodiments are further described in conjunction with the accompanying drawings and examples. The following embodiments are only used to more clearly illustrate the technical solutions of the present invention and are not intended to limit the scope of protection of the present invention.

[0044] like Figures 1-10 As shown, the MVR evaporation crystallizer of the present invention comprises:

[0045] The separator 100 is provided with a separation inlet 101, a separation outlet 102, a circulation outlet 103, a circulation inlet 104, a secondary steam outlet 105 and a mother liquor reflux port 106. The top of the separator 100 is provided with a spray pipe 200 connected to the circulation outlet 103, and the spray pipe 200 is provided with a spray head 300;

[0046] The heater 400 is provided with a raw steam inlet 401, a condensed water outlet 402, a heating inlet 403 and a heating outlet 404, and the heating outlet 404 is connected to the circulation inlet 104;

[0047] A circulation pump 500, wherein the input end of the circulation pump 500 is connected to the circulation outlet 103, and the output end of the circulation pump 500 is connected to the heating input end;

[0048] A compressor 600, wherein the input end of the compressor 600 is connected to the secondary steam outlet 105, and the output end of the compressor 600 is connected to the raw steam inlet 401;

[0049] The slurry separation component is used to separate solids from the mother liquor discharged from the separation outlet 102 and transport the mother liquor with the solids separated to the mother liquor reflux port 106 .

[0050] In the MVR evaporation crystallizer of the present invention, the separator 100 is arranged vertically, as shown in FIG. Figure 2 As shown, a separation inlet 101, a separation outlet 102, a circulation outlet 103, a circulation inlet 104, a secondary steam outlet 105 and a mother liquor reflux port 106 are provided on its outer surface, wherein the separation inlet 101 is used to introduce industrial wastewater with evaporation and concentration treatment, and the separation outlet 102 is used to discharge the wastewater after evaporation and concentration, which has a high concentration. After the liquid and solid are separated by the slurry separation component, the separated liquid, i.e., the mother liquor, is introduced into the separator 100 again from the mother liquor reflux port 106 to continue the evaporation and concentration treatment. The circulation outlet 103 and the circulation inlet 104 are used in conjunction with each other, so that during the evaporation and concentration process, the wastewater is discharged from the circulation outlet 103, and then enters the separator 100 through the circulation inlet 104 after passing through the circulation pump 500 and the heater 400, thereby forming a circulating flow and heating of the industrial wastewater. The secondary steam outlet 105 is used to discharge the secondary steam formed during the evaporation and concentration of the industrial wastewater.

[0051] According to the above description, if Figure 1 、 Figure 2 、 Figure 5 As shown, when the device evaporates and treats wastewater, the wastewater first enters the separator 100 through the separation inlet 101. During the evaporation process, part of the wastewater flows out through the circulation outlet 103, and the circulating pump 500 passes the outflowing wastewater into the heater 400. At the same time, the raw steam enters the heater 400 through the raw steam inlet 401. After the raw steam exchanges heat with the wastewater, the raw steam temperature drops and condenses to form condensed water, which is discharged from the condensed water outlet 402. After the wastewater is heated, the temperature rises and is discharged through the heating outlet 404. It then enters the spray pipe 200 inside the separator 100 through the circulation inlet 104, flows along the spray pipe 200, and is sprayed from the spray head 300. The spray head 300 is preferably an atomizing nozzle, so that the industrial wastewater flowing out of the spray head 300 has a mist structure, thereby greatly increasing the surface area of evaporation, which is conducive to the rapid evaporation of water in the wastewater, thereby more effectively removing water and shortening the evaporation time.

[0052] like Figure 7 and Figure 8As shown, after the wastewater evaporates, secondary steam is formed. After the secondary steam is discharged through the secondary steam outlet 105, it enters the compressor 600. The compressor 600 performs work on the secondary steam to increase its temperature to form raw steam. The formed raw steam enters the heater 400 through the raw steam inlet 401 of the heater 400, so that the raw steam exchanges heat with the industrial wastewater flowing in the heater 400, thereby achieving heating treatment of the industrial wastewater so that it can be evaporated and concentrated.

[0053] like Figure 1 and Figure 6 As shown, as the treatment time increases, the concentration of the wastewater gradually increases to form a thick liquid. The solids analyzed from the mixed part in the liquid are discharged through the separation outlet 102, and the wastewater liquid enters the slurry separation component. After the slurry separation component is used to separate the liquid (i.e., mother liquor) from the solid in the mixture, the liquid is passed through the mother liquor reflux port 106 into the separator 100 for evaporation and concentration treatment.

[0054] In a preferred embodiment, if Figure 1 、 Figure 3 、 Figure 7 and Figure 8 As shown, the MVR evaporation crystallizer of the present invention also includes a condensate tank 700, a condensate pump 800 and a condensate preheater 900. The input end of the condensate pump 800 is connected to the condensate outlet 402 through the condensate tank 700, the heat medium inlet of the condensate preheater 900 is connected to the output end of the condensate pump 800, the heat medium outlet is connected to the outside world, the feed port is used to input industrial wastewater, and the discharge port is connected to the separation inlet 101; the output end of the condensate pump 800 is also connected to the output end of the compressor 600.

[0055] After the raw steam exchanges heat with the industrial wastewater in the heater 400, the temperature drops to form condensed water, which is discharged into the condensed water tank 700 through the condensed water outlet 402. At this time, the temperature of the condensed water in the condensed water tank 700 is higher than that of the industrial wastewater in the wastewater source. Therefore, the industrial wastewater with higher temperature is passed into the condensed water preheater 900 through the condensed water pump 800. Before entering the separator 100, the industrial wastewater first passes through the condensed water preheater 900. The industrial wastewater and the condensed water exchange heat in the condensed water preheater 900, so that the temperature of the industrial wastewater increases. After the industrial wastewater is preheated, it is passed into the separator 100, which can effectively shorten the heating time of the industrial wastewater and make full use of the heat of the condensed water to achieve energy saving. After the condensed water is heat exchanged, the temperature drops and is discharged to the outside.

[0056] Not only that, the output end of the condensate pump 800 is also connected to the output end of the compressor 600. After adopting the above structure, the condensate pump 800 can also transport part of the condensate to the output end of the compressor 600. The output end of the compressor 600 outputs superheated steam. The superheated steam has the same temperature as the condensate. After the two come into contact, they mix to form saturated raw steam. Compared with superheated steam, saturated steam can be used as raw steam to achieve good heat exchange with industrial wastewater in the separator 100, so as to improve the heating effect of industrial wastewater, realize rapid boiling, evaporation and concentration of wastewater, improve treatment efficiency and save costs.

[0057] In a preferred embodiment, if Figure 1 、 Figure 2 and Figure 8 As shown, an isolation cylinder 110 and a flushing pipe 120 are provided in the separator 100. The isolation cylinder 110 and the separator 100 are connected via a closed-loop wire mesh foam catcher 130. The wire mesh foam catcher 130 is located below the secondary steam outlet 105. The spray head 300 is provided on the inner side of the isolation cylinder 110. The flushing pipe 120 is connected to a flushing head 140. The flushing head 140 is located directly below the wire mesh foam catcher 130 and faces the wire mesh foam catcher 130. The separator 100 is provided with a condensate flushing port 107 connected to the flushing pipe 120. The condensate flushing port 107 is connected to the output end of the condensate pump 800.

[0058] When industrial wastewater boils and evaporates in the separator 100 to form secondary steam that flows upward, the secondary steam will carry some droplets in the air and flow upward. The spray head 300 is set on the inner side of the isolation cylinder 110 to prevent the secondary steam from further contacting the droplets sprayed from the spray head 300. The wire mesh foam collector 130 can capture the droplets and foam in the secondary steam, thereby achieving a filtering effect on the secondary steam, so that the clean secondary steam is discharged through the secondary steam outlet 105 and is used by the compressor 600 to do work to form superheated steam.

[0059] After the condensate flushing port 107 is set on the separator 100, the condensate pump 800 transports part of the condensate through the condensate flushing port 107 to the flushing pipe 120 inside the separator 100. The condensate flows along the inside of the flushing pipe 120 and is sprayed out from the flushing head 140, flushing the wire mesh foam collector 130 upward to remove the liquid foam and droplets adsorbed by the wire mesh foam collector 130, so that the secondary steam formed after the wastewater evaporates can be discharged from the secondary steam outlet 105 through the wire mesh foam collector 130.

[0060] In a preferred embodiment, if Figure 1 and Figure 2As shown, an isolation sleeve 150 is also provided in the separator 100, and the isolation sleeve 150 is located directly below the flushing pipe 120. The top circumferential outer edge of the isolation sleeve 150 is fixedly connected to the circumferential inner wall of the separator 100, and there is a gap between the bottom of the isolation sleeve 150 and the bottom inside the separator 100. The circulation outlet 103 and the secondary steam inlet are both arranged on the circumferential side wall of the separator 100, the circulation outlet 103 is arranged adjacent to the top of the isolation sleeve 150, and the secondary steam outlet 105 is arranged adjacent to the wire mesh foam catcher 130; the isolation sleeve 150 includes a partition 151 and a connecting pipe 152, the partition 151 is closed-loop, the partition 151 has a guide plate inclined downward, and the circumferential inner wall of the partition 151 is fixedly connected to the top circumferential outer edge of the connecting pipe 152.

[0061] The isolation sleeve 150 formed by the fixed connection between the partition 151 and the connecting pipe 152 divides the inner cavity of the separator 100 into two parts, the upper part with a higher position is used for the spray pipe 200 and the spray head 300 to spray industrial wastewater and for discharging the secondary steam formed by the evaporation of industrial wastewater through the secondary steam outlet 105, while the lower part with a lower position is used to deposit liquid industrial wastewater. When the equipment is running, the industrial wastewater sprayed from the sprinkler head 300 falls on the guide plate of the partition 151, flows downward along the inclined guide plate and toward the inner side of the partition 151, and then deposits at the bottom of the separator 100 through the connecting pipe 152. When the deposited liquid level rises to a certain height, it is discharged through the circulation outlet 103. In the present invention, the circulation outlet 103 and the secondary steam inlet are both arranged on the circumferential side wall of the separator 100, the circulation outlet 103 is arranged close to the top of the isolation sleeve 150, and the secondary steam outlet 105 is arranged close to the wire mesh foam catcher 130. Compared with the prior art, the height difference between the circulation outlet 103 and the secondary steam outlet 105 is greatly shortened, which facilitates the docking of pipelines and makes the device easier to assemble.

[0062] In a preferred embodiment, if Figure 1 、 Figure 3 、 Figure 7 and Figure 10 As shown, an exhaust steam preheater 160 is further arranged between the condensate preheater 900 and the separator 100, and an exhaust steam outlet 405 is provided on the heater 400. The heat medium inlet of the exhaust steam preheater 160 is connected to the exhaust steam outlet 405, the heat medium outlet is connected to the condensate tank 700, the feed port is connected to the discharge port of the condensate preheater 900, and the discharge port is connected to the separation inlet 101.

[0063] After the live steam exchanges heat with the industrial wastewater in the heater 400, the live steam is divided into two parts. One part condenses to form condensed water and is discharged through the condensed water outlet 402, while the other part forms exhaust steam. The temperature of the exhaust steam is higher than that of the condensed water. Therefore, in order to make full use of the preheating of the exhaust steam, an exhaust steam preheater 160 is set between the condensed water preheater 900 and the separator 100, and the exhaust steam is introduced into the exhaust steam preheater 160. At the same time, after the industrial wastewater undergoes a first-level heat exchange with the condensed water in the condensed water preheater 900, the heated wastewater flowing out of the condensed water preheater 900 outlet enters the separator. Before 100, the industrial wastewater enters the exhaust steam preheater 160 through the feed port of the exhaust steam preheater 160. The heated industrial wastewater exchanges heat with the exhaust steam. Since the exhaust steam is higher than the heated industrial wastewater, the industrial wastewater is preheated again, increasing its temperature. The industrial wastewater is then discharged through the discharge port of the exhaust steam preheater 160 and enters the separator 100 through the separation inlet 101. The exhaust steam after heat exchange condenses to form condensed water, which is discharged from the heat medium outlet of the exhaust steam preheater 160 and enters the condensed water tank 700 for extraction and use by the condensed water pump 800. By adopting the above structure, the heat of the live steam is fully utilized to achieve secondary preheating of the industrial wastewater, which not only saves energy but also shortens the heating time of the industrial wastewater and improves efficiency.

[0064] In a preferred embodiment, if Figure 1 、 Figure 2 、 Figure 4 and Figure 6 As shown, a salt collecting tank 240 is provided at the bottom of the separator 100, and the salt collecting tank 240 is connected to the discharge pump 170; the slurry separation component includes a discharge pump 170, a slurry tank 180, a centrifuge 190, a mother liquid tank 210 and a mother liquid pump 220, the slurry tank 180 has a slurry inlet 181, a sedimentation outlet 182 and a clear liquid overflow port 183, the separation outlet 102 is connected to the slurry inlet 181 through the discharge pump 170, the sedimentation outlet 182 is connected to the mother liquid tank 210 through the centrifuge 190, the clear liquid overflow port 183 is connected to the mother liquid tank 210, and the mother liquid tank 210 is connected to the mother liquid reflux port 106 through the mother liquid pump 220.

[0065] After adopting the above structure, as the heating evaporation time increases, the concentration of the wastewater inside the separator 100 increases, some solids are precipitated to form a thick solid-liquid mixture, which settles in the salt collecting tank 240, and the separation outlet 102 is opened, and the discharge pump 170 is started. The discharge pump 170 extracts the solid-liquid mixture and transports it to the slurry tank 180 through the slurry inlet 181. Preliminary separation is carried out in the slurry tank 180. The solids are deposited at the bottom of the slurry tank 180, while the liquid is located at the top, flows out from the clear liquid overflow port 183, and enters the mother liquid tank 210; the solids deposited at the bottom carry part of the liquid and are discharged through the sedimentation outlet 182 and enter the centrifuge 190. The centrifugal separation treatment is carried out by the centrifuge 190 to separate the liquid and the solid. The liquid is the mother liquor, which is passed into the mother liquid tank 210. The mother liquid pump 220 is started to extract the liquid in the mother liquid tank 210 and transport it to the mother liquid reflux port 106 , so that the liquid continues to enter the separator 100 for evaporation and concentration.

[0066] In a preferred embodiment, the slurry tank 180 is cylindrical, and a spoiler 230 is provided in the slurry tank 180. The circumferential outer edge of the spoiler 230 is fixedly connected to the circumferential inner wall of the slurry tank 180. The inner side of the spoiler 230 extends upward along the circumference of the slurry tank 180 and the inner top of the spoiler 230 is serrated. The clear liquid overflow port 183 is provided between the top and bottom ends of the spoiler 230; the slurry inlet 181 is inclined downward and tangent to the circumferential inner wall of the slurry tank 180.

[0067] After adopting the above structure, when the discharge pump 170 pumps the solid-liquid mixture into the interior of the slurry tank 180 through the slurry inlet 181, the solid-liquid mixture first flows downward in a spiral along the inner wall of the slurry tank 180. After flowing to the bottom of the slurry tank 180, the solids in the solid-liquid mixture settle at the bottom of the slurry tank 180, and the liquid spirals up again. During the rising process of the liquid, some solid particles are driven to flow upward and encounter the serrated spoiler 230 with a serrated top. The spoiler 230 is used to disturb the flow of the liquid so that the liquid can pass through the gaps between the teeth in the serrated structure at the top of the spoiler 230, while the solids are intercepted by the teeth, thereby achieving good solid-liquid separation, so that the clarified liquid can be discharged through the clear liquid overflow port 183, and the solids are deposited at the bottom and discharged from the sedimentation outlet 182 to be subjected to solid-liquid separation again through the centrifuge 190.

[0068] The above is only a preferred embodiment of the present invention. It should be pointed out that for ordinary technicians in this technical field, several improvements and modifications can be made without departing from the technical principles of the present invention. These improvements and modifications should also be regarded as within the scope of protection of the present invention.

Claims

1. An MVR evaporation crystallizer, characterized in that: include: A separator (100), wherein the separator (100) is provided with a separation inlet (101), a separation outlet (102), a circulation outlet (103), a circulation inlet (104), a secondary steam outlet (105), and a mother liquor reflux port (106); a spray pipe (200) in communication with the circulation outlet (103) is provided at the top of the separator (100); and a spray head (300) is provided on the spray pipe (200); A heater (400), wherein the heater (400) is provided with a raw steam inlet (401), a condensed water outlet (402), a heating inlet (403), and a heating outlet (404), and the heating outlet (404) is in communication with the circulation inlet (104); a circulation pump (500), wherein the input end of the circulation pump (500) is in communication with the circulation outlet (103), and the output end of the circulation pump (500) is in communication with the heating input end; A compressor (600), wherein an input end of the compressor (600) is in communication with the secondary steam outlet (105), and an output end of the compressor (600) is in communication with the raw steam inlet (401); a slurry separation component, the slurry separation component being used to separate solids from the mother liquor discharged from the separation outlet (102) and to transport the mother liquor from which the solids have been separated to the mother liquor reflux port (106); The invention comprises a condensate tank (700), a condensate pump (800) and a condensate preheater (900), wherein the input end of the condensate pump (800) is connected to the condensate outlet (402) via the condensate tank (700), the heat medium inlet of the condensate preheater (900) is connected to the output end of the condensate pump (800), the heat medium outlet is connected to the outside, the feed port is used to input industrial wastewater, and the discharge port is connected to the separation inlet (101); the output end of the condensate pump (800) is also connected to the output end of the compressor (600); An isolation cylinder (110) and a flushing pipe (120) are provided in the separator (100), the isolation cylinder (110) and the separator (100) are connected via a closed-loop wire mesh foam trap (130), the wire mesh foam trap (130) is located below the secondary steam outlet (105), the spray head (300) is provided on the inner side of the isolation cylinder (110), the flushing pipe (120) is connected to a flushing head (140), the flushing head (140) is located directly below the wire mesh foam trap (130) and faces the wire mesh foam trap (130), the separator (100) is provided with a condensate flushing port (107) connected to the flushing pipe (120), and the condensate flushing port (107) is connected to the output end of the condensate pump (800); An isolation sleeve (150) is further provided in the separator (100), and the isolation sleeve (150) is located directly below the flushing pipe (120). The top circumferential outer edge of the isolation sleeve (150) is fixedly connected to the circumferential inner wall of the separator (100), and a gap exists between the bottom of the isolation sleeve (150) and the bottom of the separator (100). The circulation outlet (103) and the secondary steam inlet are both provided on the circumferential side wall of the separator (100), the circulation outlet (103) is provided adjacent to the top of the isolation sleeve (150), and the secondary steam outlet (105) is provided adjacent to the wire mesh foam catcher (130).

2. The MVR evaporation crystallizer according to claim 1, characterized in that: The isolation sleeve (150) comprises a partition (151) and a connecting pipe (152); the partition (151) is in a closed loop shape; the partition (151) has a guide plate inclined downward; and the circumferential inner wall of the partition (151) is fixedly connected to the top circumferential outer edge of the connecting pipe (152).

3. The MVR evaporation crystallizer according to claim 1, characterized in that: An exhaust steam preheater (160) is further provided between the condensate preheater (900) and the separator (100), and an exhaust steam outlet (405) is provided on the heater (400). The heat medium inlet of the exhaust steam preheater (160) is connected to the exhaust steam outlet (405), the heat medium outlet is connected to the condensate tank (700), the feed port is connected to the discharge port of the condensate preheater (900), and the discharge port is connected to the separation inlet (101).

4. The MVR evaporation crystallizer according to claim 1, characterized in that: The slurry separation component includes a discharge pump (170), a slurry tank (180), a centrifuge (190), a mother liquid tank (210) and a mother liquid pump (220), wherein the slurry tank (180) has a slurry inlet (181), a sedimentation outlet (182) and a clear liquid overflow port (183), the separation outlet (102) is connected to the slurry inlet (181) through the discharge pump (170), the sedimentation outlet (182) is connected to the mother liquid tank (210) through the centrifuge (190), the clear liquid overflow port (183) is connected to the mother liquid tank (210), and the mother liquid tank (210) is connected to the mother liquid reflux port (106) through the mother liquid pump (220).

5. The MVR evaporation crystallizer according to claim 4, characterized in that: A spoiler (230) is provided in the slurry tank (180), the circumferential outer edge of the spoiler (230) is fixedly connected to the circumferential inner wall of the slurry tank (180), the inner side of the spoiler (230) extends upward along the circumference of the slurry tank (180), and the inner top of the spoiler (230) is serrated, and the clear liquid overflow port (183) is provided between the top and bottom ends of the spoiler (230).

6. The MVR evaporation crystallizer according to claim 5, characterized in that: The slurry inlet (181) is arranged to be inclined downward and tangent to the circumferential inner side wall of the slurry tank (180).

7. The MVR evaporation crystallizer according to claim 4, characterized in that: A salt collecting tank (240) is provided at the bottom of the separator (100), and the salt collecting tank (240) is in communication with the discharge pump (170).

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