CN219409508U - High-salt film concentrated water treatment equipment - Google Patents
High-salt film concentrated water treatment equipment Download PDFInfo
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- CN219409508U CN219409508U CN202320710348.4U CN202320710348U CN219409508U CN 219409508 U CN219409508 U CN 219409508U CN 202320710348 U CN202320710348 U CN 202320710348U CN 219409508 U CN219409508 U CN 219409508U
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Abstract
The utility model provides high-salt membrane concentrated water treatment equipment, which relates to the technical field of wastewater treatment in the colored industry, and provides a high-salt membrane concentrated water treatment method, comprising the following steps: a first softening vessel, a second softening vessel, a first recycling device, a concentrating device, and a second recycling device; the first liquid outlet of the first softening treatment container is in fluid communication with the second softening treatment container, the second softening treatment container is internally filled with a decalcification adsorption medium, and the second liquid outlet of the second softening treatment container is in fluid communication with the first recycling device; a first bipolar membrane is installed inside the first recycling device, and a first low sodium sulfate outlet of the first recycling device is in fluid communication with the concentration treatment device; the concentrating processing means is in fluid communication with the second recycling means. The high-salt membrane concentrated water treatment equipment provided by the utility model can convert the high-salt membrane concentrated water into byproducts with high utilization value, and realizes the full resource treatment and high-value utilization of the high-salt membrane concentrated water.
Description
Technical Field
The utility model relates to the technical field of wastewater treatment in the colored industry, in particular to high-salt membrane concentrated water treatment equipment.
Background
When the nonferrous smelting enterprises treat industrial wastewater, the membrane separation technology is usually applied. But the membrane separation technology is adopted to treat industrial wastewater and recycle the industrial wastewater, and meanwhile, membrane concentrated water is also generated. Because the membrane concentrate contains a large amount of sodium, sulfate radical, chloride ions and the like, the composition components are greatly different, the treatment scheme is difficult to choose, and equipment is easy to corrode and scale. In addition, the quality and salt separation purification difficulty of the mixed salt in the membrane concentrated water is high, if the traditional thermal concentration salt steaming mode is adopted, only the industrial waste salt with the main components of sodium sulfate and sodium chloride can be obtained, the recycling is difficult, the treatment according to solid waste is needed, and the environmental protection cost burden of enterprises is further increased.
Disclosure of Invention
The utility model aims to provide high-salt membrane concentrated water treatment equipment so as to solve the technical problems that the high-salt membrane concentrated water treatment cost is high and the high-value reuse is difficult.
In a first aspect, the present utility model provides a high salt membrane concentrate water treatment apparatus comprising: a first softening vessel, a second softening vessel, a first recycling device, a concentrating device, and a second recycling device;
the first softening treatment container is provided with a softener input port, and a first liquid outlet of the first softening treatment container is in fluid communication with the second softening treatment container;
the second softening treatment container is internally filled with a decalcification adsorption medium, and a second liquid outlet of the second softening treatment container is in fluid communication with the first recycling device;
a first bipolar membrane is mounted within the first recycling device, and a first low sodium sulfate outlet of the first recycling device is in fluid communication with the concentrating treatment device;
the concentrating process device is in fluid communication with the second recycling device having a second bipolar membrane mounted therein.
With reference to the first aspect, the present utility model provides a first possible implementation of the first aspect, wherein the hydrochloric acid outlet of the first recycling means is in fluid communication with a first ammoniating means, which is in fluid communication with a first evaporation means.
With reference to the first aspect, the present utility model provides a second possible implementation of the first aspect, wherein the sulfuric acid outlet of the second recycling means is in fluid communication with a second ammoniating means, which is in fluid communication with a second evaporation means.
With reference to the first aspect, the present utility model provides a third possible implementation manner of the first aspect, wherein a liquid pump is installed between the second liquid outlet and the first recycling device.
With reference to the first aspect, the present utility model provides a fourth possible implementation manner of the first aspect, wherein one end of the first recycling device is provided with a third liquid inlet, and the other end of the first recycling device is provided with the first low sodium sulfate outlet, the first sodium hydroxide outlet and the hydrochloric acid outlet, and the first low sodium sulfate outlet, the first sodium hydroxide outlet and the hydrochloric acid outlet are sequentially arranged at intervals from top to bottom.
With reference to the fourth possible implementation manner of the first aspect, the present utility model provides a fifth possible implementation manner of the first aspect, wherein a first polar water inlet and a first polar water outlet are provided at a bottom of the first recycling device, the first polar water inlet is located at a liquid inlet end of the first recycling device, and the first polar water outlet is located at a liquid outlet end of the first recycling device.
With reference to the first aspect, the present utility model provides a sixth possible implementation manner of the first aspect, wherein the concentration processing device is provided with a fourth liquid inlet, a pure water outlet and a concentrated water outlet;
reverse osmosis membrane or electrodialysis membrane is installed to the inner chamber of concentration processing device, pure water export with the dense water export is located the offside of fourth inlet, pure water export intercommunication in the top of concentration processing device inner chamber liquid phase district, dense water export intercommunication in the bottom of concentration processing device inner chamber liquid phase district.
With reference to the first aspect, the present utility model provides a seventh possible implementation manner of the first aspect, wherein the second recycling device is provided with a hydrochloric acid outlet, a second sodium hydroxide outlet, a second low sodium sulfate outlet and a fifth liquid inlet;
the sulfuric acid outlet, the second sodium hydroxide outlet and the second sodium hyposulfite outlet are all positioned on the opposite sides of the fifth liquid inlet, the fifth liquid inlet is in fluid communication with the concentration treatment device, and the sulfuric acid outlet, the second sodium hydroxide outlet and the second sodium hyposulfite outlet are sequentially arranged at intervals from top to bottom.
With reference to the seventh possible implementation manner of the first aspect, the present utility model provides an eighth possible implementation manner of the first aspect, wherein a second water inlet and a second water outlet are further provided at a bottom of the second recycling device, the second water inlet is located at a liquid inlet end of the second recycling device, and the second water outlet is located at a liquid outlet end of the second recycling device.
With reference to the first aspect, the present utility model provides a ninth possible implementation manner of the first aspect, where the second softening treatment container is provided with a second liquid inlet that communicates with the first softening treatment container, and the second softening treatment container is further provided with a second liquid outlet that communicates with the first recycling device;
the second liquid inlet is communicated with the top of the liquid phase zone of the inner cavity of the second softening treatment container, and the second liquid outlet is communicated with the bottom of the liquid phase zone of the inner cavity of the second softening treatment container.
The embodiment of the utility model has the following beneficial effects: the softener is added into the first softening treatment container through the softener feeding port, so that the high-salt membrane concentrated water can be primarily softened, the high-salt membrane concentrated water in the second softening treatment container is treated by a decalcification adsorption medium to realize deep softening, the deeply softened high-salt membrane concentrated water is treated by a bipolar membrane electrodialysis method in the first recycling device to obtain hydrochloric acid, sodium hydroxide and brine containing sodium sulfate, the brine is concentrated by the concentrating treatment device, sulfuric acid and sodium hydroxide are obtained by the bipolar membrane treatment of the second recycling device after concentration, the high-salt membrane concentrated water can be converted into byproducts with high utilization values such as sodium hydroxide, ammonium chloride and ammonium sulfate, and the full resource treatment and high-value utilization of the high-salt membrane concentrated water are realized.
In order to make the above objects, features and advantages of the present utility model more comprehensible, preferred embodiments accompanied with figures are described in detail below.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the related art, the drawings that are required to be used in the description of the embodiments or the related art will be briefly described, and it is apparent that the drawings in the description below are some embodiments of the present utility model, and other drawings may be obtained according to the drawings without inventive effort for those skilled in the art.
FIG. 1 is a schematic diagram of a high-salt membrane concentrate treatment process according to an embodiment of the present utility model;
fig. 2 is a schematic diagram of a high-salt membrane concentrated water treatment device according to an embodiment of the present utility model.
Icon: 001-a first softening treatment vessel; 101-a softener inlet; 102-a first liquid inlet; 103-a first liquid outlet; 104-a calcium slag external discharge port; 002-a second softening treatment vessel; 201-decalcification adsorption medium; 202-a second liquid inlet; 203-a second outlet; 003-first recycling device; 301-a first bipolar membrane; 302-a first sodium hyposulfite outlet; 303-hydrochloric acid outlet; 304-a first sodium hydroxide outlet; 305-a third liquid inlet; 306-a first polar water inlet; 307-a first pole water outlet; 004-concentrating the treatment device; 401-fourth liquid inlet; 402-pure water outlet; 403-concentrated water outlet; 005-a second recycling device; 501-a second bipolar membrane; 502-sulfuric acid outlet; 503-a second sodium hydroxide outlet; 504-a second sodium hyposulfate outlet; 505-fifth liquid inlet; 506-second water inlet; 507-second water outlet; 006-a first ammoniated device; 601-a first ammoniation inlet; 602-a first ammoniation outlet; 603-a first dosing port; 007-a first evaporation device; 701-ammonium chloride liquid inlet; 702-a first crystallization discharge port; 008-a second ammoniated device; 801-a second ammoniation inlet; 802-a second ammoniation outlet; 803-a second dosing port; 009-a second evaporation device; 901-ammonium sulfate liquid inlet; 902-a crystallization discharge port; 010-liquid pump.
Detailed Description
The following description of the embodiments of the present utility model will be made apparent and fully in view of the accompanying drawings, in which some, but not all embodiments of the utility model are shown. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
In the description of the present utility model, it should be noted that the directions or positional relationships indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, are merely for convenience of describing the present utility model and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present utility model. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance. Physical quantities in the formulas, unless otherwise noted, are understood to be basic quantities of basic units of the international system of units, or derived quantities derived from the basic quantities by mathematical operations such as multiplication, division, differentiation, or integration.
In the description of the present utility model, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present utility model will be understood in specific cases by those of ordinary skill in the art.
As shown in fig. 1, the high-salt membrane concentrated water treatment apparatus provided by the embodiment of the utility model includes: a first softening process vessel 001, a second softening process vessel 002, a first recycling device 003, a concentration process device 004, and a second recycling device 005;
the first softening treatment container 001 is provided with a softener inlet 101, and a first liquid outlet 103 of the first softening treatment container 001 is in fluid communication with the second softening treatment container 002;
the second softening treatment vessel 002 is filled with a decalcification adsorption medium 201, and the second liquid outlet 203 of the second softening treatment vessel 002 is in fluid communication with the first recycling device 003;
the first bipolar membrane 301 is mounted within the first recycling device 003, and the first low sodium sulfate outlet 302 of the first recycling device 003 is in fluid communication with the concentration process device 004;
the concentration treatment device 004 is in fluid communication with a second recycling device 005, the second recycling device 005 having a second bipolar membrane 501 mounted therein.
Specifically, the high-salt film concentrated water is input through the first liquid inlet 102 of the first softening vessel 001, sodium carbonate or carbon dioxide is added into the first softening vessel 001 through the softener input port 101, the first liquid inlet 102 and the first liquid outlet 103 are respectively communicated to the top of the liquid phase zone of the first softening vessel 001, and the precipitate formed in the first softening vessel 001 can be discharged through the calcium slag external discharge port 104 at the bottom. The decalcification adsorption medium 201 can adopt D001X 4 resin, and can effectively deeply adsorb calcium in wastewater. The first liquid outlet 103 is communicated with the second liquid inlet 202 of the second softening treatment container 002, brine subjected to deep softening treatment in the second softening treatment container 002 is discharged through the second liquid outlet 203, the second liquid inlet 202 is communicated with the top of the liquid phase zone in the inner cavity of the second softening treatment container 002, and the second liquid outlet 203 is communicated with the bottom of the liquid phase zone in the inner cavity of the second softening treatment container 002, so that the brine flowing through the second softening treatment container 002 can be fully contacted with the decalcification adsorption medium 201, further deep softening is realized, and the concentration of calcium ions can be less than 1mg/L.
In the embodiment of the present utility model, the third liquid inlet 305 of the first recycling device 003 is in fluid communication with the second liquid outlet 203, and a liquid pump 010 is installed between the third liquid inlet 305 and the second liquid outlet 203, and the liquid pump 010 can pressurize and drain the liquid, so that the highly softened high-salt film concentrated water is introduced into the first recycling device 003. One end of the first recycling device 003, which is away from the third liquid inlet 305, is provided with a first low sodium sulfate outlet 302, a first sodium hydroxide outlet 304 and a hydrochloric acid outlet 303, and the first low sodium sulfate outlet 302, the first sodium hydroxide outlet 304 and the hydrochloric acid outlet 303 are sequentially arranged at intervals from top to bottom. In addition, the liquid inlet end of the first recycling device 003 is provided with a first polar water inlet 306, the liquid outlet end is provided with a first polar water outlet 307, the first polar water inlet 306 and the first polar water outlet 307 are both arranged at the bottom of the first recycling device 003, and a plurality of first bipolar membranes 301 are arranged in the inner cavity of the first recycling device 003 at intervals from the liquid inlet end to the liquid outlet end.
Further, the hydrochloric acid outlet 303 of the first recycling device 003 is in fluid communication with the first ammoniated device 006, and the first ammoniated device 006 is in fluid communication with the first evaporation device 007.
Specifically, the first ammoniation device 006 is provided with a first ammoniation inlet 601, a first ammoniation outlet 602 and a first dosing port 603, the hydrochloric acid outlet 303 is communicated with the first ammoniation inlet 601, ammonia water or ammonium chloride can be added into the first ammoniation device 006 through the first dosing port 603, an ammonium chloride solution can enter the first evaporation device 007 through the first ammoniation outlet 602 and the ammonium chloride liquid inlet 701, and ammonium chloride crystals can be discharged through a first crystal discharge port 702 at the bottom of the first evaporation device 007.
Further, the sulfuric acid outlet 502 of the second recycling device 005 is in fluid communication with the second ammoniated device 008, and the second ammoniated device 008 is in fluid communication with the second evaporation device 009.
Specifically, the concentration treatment device 004 is provided with a fourth liquid inlet 401, a pure water outlet 402 and a concentrated water outlet 403, the pure water outlet 402 and the concentrated water outlet 403 are both positioned on opposite sides of the fourth liquid inlet 401, the pure water outlet 402 is communicated with the top of the liquid phase zone in the inner cavity of the concentration treatment device 004, and the concentrated water outlet 403 is communicated with the bottom of the liquid phase zone in the inner cavity of the concentration treatment device 004. The first low sodium sulfate outlet 302 is communicated with the fourth liquid inlet 401, and the pure water outlet 402 discharges pure water for realizing the reuse of the pure water; the concentrate outlet 403 communicates with the fifth inlet 505 of the second recycling device 005. The second recycling device 005 is further provided with a second sodium hydroxide outlet 503 and a second sodium hyposulfite outlet 504, and the sulfuric acid outlet 502, the second sodium hydroxide outlet 503 and the second sodium hyposulfite outlet 504 are sequentially arranged at intervals from top to bottom. The bottom of the second recycling device 005 is also provided with a second water inlet 506 and a second water outlet 507, and the second water inlet 506 is used for introducing the polar water into the second recycling device 005, and the polar water after reaction is discharged through the second water outlet 507. The sulfuric acid outlet 502 is communicated with a second ammoniation inlet 801 of the second ammoniation device 008, the second ammoniation inlet 801 and the second ammoniation outlet 802 are respectively communicated with the top of the liquid phase area of the inner cavity of the second ammoniation device 008, the second ammoniation device 008 is provided with a second dosing port 803, and ammonia water or ammonium chloride can be added into the second ammoniation device 008 through the second dosing port 803. The second evaporation device 009 is provided with an ammonium sulfate inlet 901 and a crystallization outlet 902, the second ammoniation outlet 802 is communicated with the ammonium sulfate inlet 901, the ammonium sulfate solution is evaporated in the second evaporation device 009 to form ammonium sulfate crystals, and the ammonium sulfate crystals can be discharged through the crystallization outlet 902 at the bottom of the second evaporation device 009.
By adopting the high-salt membrane concentrated water treatment equipment disclosed by the embodiment, the high-salt membrane concentrated water can be treated, the generated sodium hydroxide can be reused for nonferrous metal smelting, the ammonium chloride and the ammonium sulfate can be respectively formed after the ammoniation treatment of the hydrochloric acid and the sulfuric acid, and the ammonium chloride and the ammonium sulfate are formed after the evaporation crystallization and serve as agricultural fertilizers or industrial byproducts, so that the high-value byproducts are extracted from the high-salt membrane concentrated water, and the full-resource treatment and the high-value utilization are realized.
As shown in fig. 1 and 2, in the high-salt membrane concentrate treatment method using the above-described high-salt membrane concentrate treatment apparatus, the method comprises the steps of: adding a softener into the high-salt film concentrated water in the first softening treatment container 001 to primarily soften the high-salt film concentrated water; the ion exchange method is adopted in the second softening treatment container 002 to deeply soften the primarily softened high-salt film concentrated water; treating the deeply softened high-salt membrane concentrated water in the first recycling device 003 by adopting a bipolar membrane electrodialysis method to obtain hydrochloric acid, sodium hydroxide and brine containing sodium sulfate; concentrating the brine in a concentration processing device 004; the concentrated brine is treated with bipolar membranes in a second recycling device 005 to obtain sulfuric acid and sodium hydroxide.
In the method for treating high-salt-concentration-film-concentrated water according to the present embodiment, a softener is used to chemically react with calcium ions in high-salt-concentration-film-concentrated water to form a deposited chemical substance, so that the concentration of calcium ions in high-salt-concentration-film-concentrated water can be initially reduced. And then, deeply softening the high-salt membrane concentrated water by adopting an ion exchange method, and further reducing the concentration of calcium ions in the high-salt membrane concentrated water. And (3) after deep softening, carrying out I-level recycling treatment on the high-salt membrane concentrated water by adopting a bipolar membrane electrodialysis method, so that hydrochloric acid, sodium hydroxide and brine containing sodium sulfate can be obtained. And concentrating the brine after the I-level recycling treatment, recycling fresh water generated in the concentration process or returning the concentrated brine to a raw water tank, and treating the concentrated brine by adopting a bipolar membrane to realize the II-level recycling treatment, so that sulfuric acid and sodium hydroxide can be obtained. The sodium hydroxide can be recycled for nonferrous smelting production, and the sulfuric acid and the hydrochloric acid can respectively pass through ammonification reaction, so that ammonium sulfate and ammonium chloride are formed, the ammonium sulfate and the ammonium chloride can be used as agricultural fertilizers or industrial byproducts, the utilization value of the byproducts is high, and the full resource treatment and high-value utilization of high-salt membrane concentrated water are realized.
In the embodiment of the utility model, in the step of adding the softener into the high-salt film concentrated water:
the softening agent adopts sodium carbonate or carbon dioxide; the softener was added in an amount to satisfy a molar ratio of carbon to calcium of 1.2:1 to 1.5:1. the carbon dioxide ions in the sodium carbonate or the carbon dioxide are combined with the calcium ions to form calcium carbonate precipitates, so that the concentration of the calcium ions in the high-salt membrane concentrated water can be reduced. Before the softener is added, the concentration of calcium ions in the high-salt film concentrated water can be detected, so that the mole number of the calcium ions in the high-salt film concentrated water is estimated, and the mole ratio of carbon to calcium is 1.2:1 to 1.5:1 adding a softening agent, thereby ensuring that the primary softening can achieve the expected effect.
Further, the step of preliminary softening includes:
detecting the content of calcium ions in the high-salt film concentrated water;
if the concentration of the calcium ions is more than or equal to 10mg/L, continuously adding a softener into the high-salt membrane concentrated water;
if the concentration of the calcium ions is less than 10mg/L, the softener is stopped.
The high-salt film concentrated water should be stirred along with the addition of the softener, so that the softener and calcium ions in the high-salt film concentrated water fully react, the softening efficiency is improved, and the preliminary softening is finished when the concentration of the calcium ions is less than 10 mg/L.
Further, the deep softening step comprises:
detecting the content of calcium ions in the high-salt film concentrated water;
if the concentration of the calcium ions is more than or equal to 1mg/L, continuing to adsorb the calcium ions in the high-salt membrane concentrated water;
and if the concentration of the calcium ions is less than 1mg/L, introducing softened high-salt membrane concentrated water into the next working procedure.
After the preliminary softening is finished, the high-salt membrane concentrated water is deeply softened by an ion exchange method until the concentration of calcium ions is less than 1mg/L, so that the influence of the calcium ions in the high-salt membrane concentrated water on the subsequent recycling treatment can be avoided.
Further, the high-salt membrane concentrated water treatment method further comprises the following steps: the hydrochloric acid is subjected to ammoniation reaction, and ammonium chloride crystals are obtained through evaporation and crystallization, so that the recycling of chloride ions in the high-salt membrane concentrated water can be realized.
Further, the high-salt membrane concentrated water treatment method further comprises the following steps: the sulfuric acid is subjected to ammonification reaction, and ammonium sulfate crystals are obtained through evaporation and crystallization, so that the resource utilization of sulfate ions in the high-salt membrane concentrated water can be realized.
In the step of treating the deeply softened high-salt membrane concentrated water by adopting a bipolar membrane electrodialysis method and the step of treating the concentrated brine by adopting a bipolar membrane: and 2% sodium hydroxide solution is circularly introduced into the brine container, the sodium hydroxide solution is used as polar water, the bipolar membrane is used for preparing acid and alkali from the brine, and the purity of the generated hydrochloric acid is over 99% due to the effect of the anion nanofiltration membrane.
In the embodiment of the comprehensive treatment of the lead-zinc smelting plant sewage, the salt content of the sewage is 8.6%, the concentration of calcium ions is 167mg/L, the concentration of chloride ions is 2.3%, the concentration of sulfate ions is 3.6%, and the concentration of sodium ions is 2.6%. In the primary softening correction: adding sodium carbonate for chemical softening reaction, wherein the adding amount of the sodium carbonate is 368mg/L, and the molar ratio of carbon to calcium is 1.2:1, the concentration of calcium ions after softening was detected to be 8.5mg/L. In the deep softening step, the D001X 4 resin is adsorbed at an adsorption filtration rate of 5BV/h, and BV is the bed volume, i.e., the resin loading. And then, carrying out I-level recycling treatment on the softened membrane concentrated water, initially adding deionized water into an acid tank and an alkali tank, preparing acid and alkali from brine by using 2% sodium hydroxide and using a bipolar membrane, wherein the purity of the generated hydrochloric acid is over 99% due to the effect of an anion nanofiltration membrane, when the concentration of the sodium hydroxide and the hydrochloric acid generated by the alkali tank and the acid tank is 5%, opening a way, the sodium hydroxide with the concentration reaching the standard can be recycled for production, adding 5% ammonium bicarbonate after the hydrochloric acid is collected, and carrying out evaporation crystallization after ammonium chloride is generated. When the concentration of the brine in the salt tank is 3.5%, the brine with the concentration reaching the standard enters an electrodialysis concentration system, fresh water returns to a raw water tank, when the concentration of the concentrated water is 8%, grade II recycling treatment is carried out, deionized water is initially added into an acid tank and an alkali tank, 2% sodium hydroxide is adopted as polar water, the brine is utilized to prepare acid and alkali, when the concentration of sodium hydroxide and sulfuric acid generated by the alkali tank and the acid tank is 5%, the brine is opened, the sodium hydroxide can be recycled for production, 5% ammonium bicarbonate is added after sulfuric acid is collected, and the ammonium sulfate is produced and is used for evaporative crystallization.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present utility model, and not for limiting the same; although the utility model has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the utility model.
Claims (10)
1. A high salt film concentrate water treatment apparatus, comprising: a first softening treatment vessel (001), a second softening treatment vessel (002), a first recycling device (003), a concentration treatment device (004) and a second recycling device (005);
the first softening treatment container (001) is provided with a softener input port (101), and a first liquid outlet (103) of the first softening treatment container (001) is in fluid communication with the second softening treatment container (002);
the second softening treatment vessel (002) is internally filled with a decalcification adsorption medium (201), and a second liquid outlet (203) of the second softening treatment vessel (002) is in fluid communication with the first recycling device (003);
a first bipolar membrane (301) is mounted inside the first recycling means (003), and a first low sodium sulfate outlet (302) of the first recycling means (003) is in fluid communication with the concentration processing means (004);
the concentrating treatment device (004) is in fluid communication with the second recycling device (005), and a second bipolar membrane (501) is mounted inside the second recycling device (005).
2. The high salt membrane concentrate water treatment device of claim 1, wherein the hydrochloric acid outlet (303) of the first recycling means (003) is in fluid communication with a first ammoniated means (006), the first ammoniated means (006) being in fluid communication with a first evaporation means (007).
3. The high salt membrane concentrate water treatment apparatus of claim 1, wherein the sulfuric acid outlet (502) of the second recycling means (005) is in fluid communication with a second ammoniation means (008), the second ammoniation means (008) being in fluid communication with a second evaporation means (009).
4. The high-salt membrane concentrated water treatment apparatus according to claim 1, wherein a liquid pump (010) is installed between the second liquid outlet (203) and the first recycling device (003).
5. The high-salt membrane concentrated water treatment device according to claim 1 or 2, wherein one end of the first recycling device (003) is provided with a third liquid inlet (305), and the other end of the first recycling device is provided with the first low sodium sulfate outlet (302), the first sodium hydroxide outlet (304) and the hydrochloric acid outlet (303), and the first low sodium sulfate outlet (302), the first sodium hydroxide outlet (304) and the hydrochloric acid outlet (303) are sequentially arranged at intervals from top to bottom.
6. The high-salt membrane concentrated water treatment device according to claim 5, wherein a first polar water inlet (306) and a first polar water outlet (307) are arranged at the bottom of the first recycling device (003), the first polar water inlet (306) is located at the liquid inlet end of the first recycling device (003), and the first polar water outlet (307) is located at the liquid outlet end of the first recycling device (003).
7. The high-salt membrane concentrate treatment apparatus according to claim 1, wherein the concentrate treatment device (004) is provided with a fourth liquid inlet (401), a pure water outlet (402) and a concentrate outlet (403);
reverse osmosis membrane or electrodialysis membrane is installed to the inner chamber of concentrated processing device (004), pure water export (402) with dense water export (403) all are located the offside of fourth inlet (401), pure water export (402) communicate in the top of concentrated processing device (004) inner chamber liquid phase district, dense water export (403) communicate in the bottom of concentrated processing device (004) inner chamber liquid phase district.
8. The high-salt membrane concentrated water treatment apparatus according to claim 1, wherein the second recycling device (005) is provided with a sulfuric acid outlet (502), a second sodium hydroxide outlet (503), a second low sodium sulfate outlet (504), and a fifth liquid inlet (505);
the sulfuric acid outlet (502), the second sodium hydroxide outlet (503) and the second sodium hyposulfite outlet (504) are all located at opposite sides of the fifth liquid inlet (505), the fifth liquid inlet (505) is in fluid communication with the concentrating device (004), and the sulfuric acid outlet (502), the second sodium hydroxide outlet (503) and the second sodium hyposulfite outlet (504) are sequentially arranged at intervals from top to bottom.
9. The high-salt membrane dense water treatment apparatus according to claim 8, wherein the bottom of the second recycling device (005) is further provided with a second water inlet (506) and a second water outlet (507), the second water inlet (506) is located at a liquid inlet end of the second recycling device (005), and the second water outlet (507) is located at a liquid outlet end of the second recycling device (005).
10. The high-salt membrane concentrated water treatment apparatus according to claim 1, wherein the second softening treatment container (002) is provided with a second liquid inlet (202) communicating with the first softening treatment container (001), and the second softening treatment container (002) is further provided with a second liquid outlet (203) communicating with the first recycling device (003);
the second liquid inlet (202) is communicated with the top of the liquid phase zone of the inner cavity of the second softening treatment container (002), and the second liquid outlet (203) is communicated with the bottom of the liquid phase zone of the inner cavity of the second softening treatment container (002).
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| CN202320710348.4U CN219409508U (en) | 2023-04-03 | 2023-04-03 | High-salt film concentrated water treatment equipment |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116282733A (en) * | 2023-04-03 | 2023-06-23 | 矿冶科技集团有限公司 | High-salt membrane concentrated water treatment method and high-salt membrane concentrated water treatment equipment |
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2023
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116282733A (en) * | 2023-04-03 | 2023-06-23 | 矿冶科技集团有限公司 | High-salt membrane concentrated water treatment method and high-salt membrane concentrated water treatment equipment |
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