CN210122533U - Processing system who contains salt waste water - Google Patents
Processing system who contains salt waste water Download PDFInfo
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- CN210122533U CN210122533U CN201920356932.8U CN201920356932U CN210122533U CN 210122533 U CN210122533 U CN 210122533U CN 201920356932 U CN201920356932 U CN 201920356932U CN 210122533 U CN210122533 U CN 210122533U
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Abstract
The utility model provides a processing system (10) that contains salt waste water, include: the device comprises an organic matter removing unit (100), a nanofiltration membrane unit (200) and a sodium chloride electrolysis unit (300) which are sequentially connected along the flow direction of the salt-containing wastewater; an electrically-driven ion separation membrane unit (400), a resin softening unit (500) and a bipolar membrane unit (600) which are connected in sequence along the flow direction of the salt-containing wastewater; wherein the electrically driven ion separation membrane unit (400) is connected with the nanofiltration membrane unit (200), and the electrically driven ion separation membrane unit (400) is arranged at the downstream of the nanofiltration membrane unit (200) along the flow direction of the saline wastewater. The utility model aims to at least realize the self-sufficiency of medicament of water treatment.
Description
Technical Field
The utility model relates to a water treatment field, more specifically relates to a processing system who contains salt waste water.
Background
The high-salt water of the water treatment industry mainly comes from concentrated solution generated in the desalination process and the water recycling treatment process. The high-salt water mainly comes from desulfurization waste water of a power plant, landfill leachate, reverse osmosis concentrated water in the petrochemical industry, mine water and coal chemical industry. The high-salt water has large discharge amount, small water quality change, stable and generally higher salt content, and the composition form mainly comprises organic matters and inorganic matters. The Chemical Oxygen Demand (COD) is generally 200-600mg/L, the Total Dissolved Solids (TDS) is 10000-80000mg/L, the calcium/magnesium content is high, and the scale-prone ions such as sulfate radicals are contained. The direct discharge of the high-salinity wastewater not only can cause soil hardening, salinization, crop damage and ecological environment deterioration in a discharge area, but also can cause waste of water resources. Therefore, the realization of the recycling of the saline wastewater in the coal chemical industry is one of the problems to be solved urgently at present.
The near zero emission is an effective way for recycling the salt-containing wastewater. Currently, the "near zero emission" process includes softening pretreatment, membrane concentration and evaporative crystallization as the major components. The softening adopts double alkali chemical precipitation, the medicament consumption is large, and the cost is high. The membrane concentration method comprises high-pressure flat membrane, electrodialysis, vibration membrane and forward osmosis membrane. The evaporative crystallization has mechanical compression evaporation and multiple-effect evaporation, and is the link which consumes the most energy in the near zero emission process. Because of the limitation of industrial layout, the export of qualified crystallization industrial salt is limited, so the current 'zero emission' process and 'quality-divided crystallization' process do not realize the resource utilization in the real sense.
In the high-salt water zero-discharge process, a plurality of pretreatment processes are required, the high-salt water needs to be softened and de-hardened before being re-concentrated, a large amount of soda ash, lime or liquid alkali, coagulant and coagulant aid are consumed, and the treatment cost is high; or a large amount of sludge is generated and needs to be disposed, and the resource utilization is not realized; investment and operating costs increase and the reuse of the produced crystalline salts is limited.
SUMMERY OF THE UTILITY MODEL
To the problems in the related art, the present invention is directed to a salt-containing wastewater treatment system to at least achieve drug self-sufficiency in water treatment.
In order to achieve the above object, the utility model provides a processing system who contains salt waste water, include: the organic matter removing unit, the nanofiltration membrane unit and the sodium chloride electrolysis unit are sequentially connected along the flow direction of the salt-containing wastewater; the electric-driven ion separation membrane unit, the resin softening unit and the bipolar membrane unit are sequentially connected along the flow direction of the salt-containing wastewater; wherein, electrically driven ion separation membrane unit connects the nanofiltration membrane unit to, along the flow direction that contains salt waste water, electrically driven ion separation membrane unit sets up the low reaches at the nanofiltration membrane unit.
According to the utility model discloses an embodiment, the unit is got rid of to organic matter includes electrochemical oxidation reactor, and electrochemical oxidation reactor includes the cavity and sets up the filler in the cavity, is provided with interconnect's first positive pole and first negative pole in the filler, and wherein, the entry linkage of cavity contains the conveying line of salt waste water.
According to the utility model discloses an embodiment, receive filter membrane unit and include along the flow direction cartridge filter, force (forcing) pump and the membrane module that connect gradually of containing salt waste water, cartridge filter's entry linkage cavity's export.
According to an embodiment of the utility model, the sodium chloride electrolysis unit includes the electrolysis trough and sets up second positive pole and second negative pole in the electrolysis trough, and the second positive pole passes through DC power supply and connects the second negative pole, and wherein, the export of the entry linkage membrane module of electrolysis trough, the first branch road of the outside that extends to processing system is connected to the export of electrolysis trough.
According to the utility model discloses an embodiment, electrically driven ion separation membrane unit includes dense room, the first room and the second that fade that link to each other with dense room and the first anode chamber and the first cathode chamber that link to each other with the first room and the second that fade respectively, and the membrane module is connected to the first room and the second that fade.
According to an embodiment of the present invention, the electrically driven ion separation membrane unit further includes: the inlet of the fade chamber circulation box is connected with the outlets of the first fade chamber and the second fade chamber, and the outlet of the fade chamber circulation box is connected with the inlets of the first fade chamber, the second fade chamber and the resin softening unit; the inlet of the calcium chloride/magnesium circulation box is connected with the outlet of the concentration chamber, the outlet of the calcium chloride/magnesium circulation box is connected with the inlet of the heat exchange device, and the outlet of the heat exchange device is connected with the inlet of the concentration chamber and a second branch extending to the outside of the treatment system; an inlet of the anode effusion circulation box is connected with an outlet of the first anode chamber, and an outlet of the anode effusion circulation box is connected with an inlet of the first anode chamber; the inlet of the cathode effusion circulation box is connected with the outlet of the first cathode chamber, and the outlet of the cathode effusion circulation box is connected with the inlet of the first cathode chamber.
According to an embodiment of the present invention, a bipolar membrane unit includes: an acid chamber and a base chamber connected to the acid chamber; a first salt chamber and a second salt chamber respectively connected with the acid chamber and the alkali chamber; and a second anode chamber and a second cathode chamber connected to the first salt chamber and the second salt chamber, respectively.
According to an embodiment of the invention, the outlet of the resin softening unit is connected to the inlets of the first and second salt chambers.
According to an embodiment of the present invention, the bipolar membrane unit further comprises: the inlet of the salt chamber circulation box is connected with the outlets of the first salt chamber and the second salt chamber, and the outlet of the salt chamber circulation box is connected with the inlets of the first salt chamber and the second salt chamber and a third branch extending to the outside of the treatment system; the inlet of the acid chamber circulation box is connected with the outlet of the acid chamber, the outlet of the acid chamber circulation box is connected with the inlet of the acid chamber, and a fourth branch extending to the outside of the treatment system is connected; the inlet of the alkali chamber circulation box is connected with the outlet of the alkali chamber, and the outlet of the alkali chamber circulation box is connected with the inlet of the alkali chamber and a fifth branch extending to the outside of the treatment system; the inlet of the second anode effusion circulating box is connected with the outlet of the second anode chamber, and the outlet of the second anode effusion circulating box is connected with the inlet of the second anode chamber; and an inlet of the second cathode effusion circulation box is connected with an outlet of the second cathode chamber, and an outlet of the second cathode effusion circulation box is connected with an inlet of the second cathode chamber.
According to one embodiment of the present invention, a bipolar membrane is disposed between the acid chamber and the alkali chamber, and the bipolar membrane is connected to the water supply branch.
The utility model has the advantages of:
1. the salt water softening pretreatment unit is reduced, the chemical agent cost is low, the sludge production and disposal cost are reduced, the hardness ions are recycled, and the investment cost is saved;
2. the water treatment agent for wastewater treatment is self-sufficient, sodium chloride is prepared into a sodium hypochlorite disinfectant or bactericide, and sodium sulfate is prepared into sulfuric acid and sodium hydroxide;
3. an evaporation crystallization unit of the traditional zero-discharge process is omitted, the energy consumption is greatly reduced, and the operating cost is reduced.
Drawings
Fig. 1 is a schematic structural view of a treatment system for salt-containing wastewater according to an embodiment of the present invention.
Detailed Description
The technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. Based on the embodiments in the present invention, other embodiments obtained by the ordinary person in the art without creative work all belong to the protection scope of the present invention.
Fig. 1 shows a system 10 for treating salt-containing wastewater according to an embodiment of the present invention, including: the organic matter removing unit 100, the nanofiltration membrane unit 200 and the sodium chloride electrolysis unit 300 are sequentially connected along the flow direction of the salt-containing wastewater; an electrically-driven ion separation membrane unit 400, a resin softening unit 500 and a bipolar membrane unit 600 which are connected in sequence in the flow direction of the salt-containing wastewater; wherein, the electrically driven ion separation membrane unit 400 is connected with the nanofiltration membrane unit 200, and the electrically driven ion separation membrane unit 400 is arranged at the downstream of the nanofiltration membrane unit 200 along the flow direction of the saline wastewater. In other words, the nanofiltration membrane unit 200 connects the sodium chloride electrolysis unit 300 and the electrically driven ion separation membrane unit 400.
According to an embodiment of the present invention, the organic matter removing unit 100 comprises an electrochemical oxidation reactor 101, the electrochemical oxidation reactor 101 comprises a cavity 102 and a filler 103 disposed in the cavity 102, the filler 103 is provided with a first anode 104 and a first cathode 105 which are connected with each other, wherein an inlet of the cavity 102 is connected to a conveying pipeline 106 for salt-containing wastewater.
In one embodiment, electrochemical oxidation reactor 101 is a multi-interface electrochemical oxidation reactor. The filler 103 is a multi-interface high-conductivity filler, which refers to carbon particles subjected to chemical oxidation treatment. The material of the first cathode 105 and the first anode 104 is titanium ruthenium mesh electrode or diamond doped electrode. The organic matter removing unit 100 may also be other processing units for achieving the same technical effect, such as one or a combination of coagulation, resin, adsorption, ozone catalytic oxidation, photocatalytic oxidation, and fenton technology.
According to an embodiment of the present invention, the nanofiltration membrane unit 200 comprises a cartridge filter 201, a pressure pump 202 and a membrane module 203 connected in sequence along the flow direction of the salt-containing wastewater, wherein the inlet of the cartridge filter 201 is connected with the outlet of the cavity 102. In other words, the salt-containing wastewater enters the nanofiltration membrane unit 200 after being treated by the organic matter removal unit 100.
According to one embodiment of the present invention, the sodium chloride electrolysis unit 300 comprises an electrolysis cell 302 and a second anode 303 and a second cathode 304 arranged within the electrolysis cell 302. The second anode 303 is connected to the second cathode 304 via a dc power supply 301. Wherein the inlet of the electrolytic cell 302 is connected to the outlet of the membrane module 203 and the outlet of the electrolytic cell 302 is connected to a first branch 305 extending to the outside of the treatment system 10. The first branch 305 carries a sodium hypochlorite (NaCLO) solution. In other words, the salt-containing wastewater enters the sodium chloride electrolysis unit 300 after being treated by the organic matter removal unit 100 and the nanofiltration membrane unit 200.
In one embodiment, the second anode 303 is a titanium ruthenium mesh electrode, the second cathode 304 is hastelloy, and the electrolytic cell 302 is made of polyvinyl chloride (PVC). The positive electrode of the direct current power supply 301 is connected with the second anode 303; the negative pole of the dc power supply 301 is connected to the second cathode 304.
According to an embodiment of the present invention, the electrically-driven ion separation membrane unit 400 includes a concentration chamber 402, a first diluting chamber 401 and a second diluting chamber 421 connected to the concentration chamber 402, and a first anode chamber 403 and a first cathode chamber 423 connected to the first diluting chamber 401 and the second diluting chamber 421, respectively, and the membrane module 203 is connected to the first diluting chamber 401 and the second diluting chamber 421. In other words, the membrane module 203 is connected with the first dilute chamber 401, the second dilute chamber 421 and the electrolytic bath 302, and the nanofiltration membrane unit 200 produces concentrated water to enter the electrically driven ion separation membrane unit 400.
In one embodiment, the concentration chamber 402 is a calcium chloride/magnesium concentration chamber, the concentration chamber 402 being located between an anion selective membrane and a cation exchange membrane; the first and second diluting chambers 401 and 421 are sodium sulfate solution chambers; the anode and cathode plates of the first anode chamber 403 and the first cathode chamber 423 are made of titanium ruthenium. In other words, a cation exchange membrane is disposed between the first fade chamber 401 and the rich chamber 402, and an anion selective membrane is disposed between the rich chamber 402 and the second fade chamber 421.
According to an embodiment of the present invention, the electrically driven ion separation membrane unit 400 further includes: a fresh chamber circulation tank 405, a calcium/magnesium chloride circulation tank 406, an anolyte circulation tank 408, and a catholyte circulation tank 409.
In one embodiment, the inlet of the fade chamber circulation box 405 is connected to the outlets of the first fade chamber 401 and the second fade chamber 421, and the outlet of the fade chamber circulation box 405 is connected to the inlets of the first fade chamber 401, the second fade chamber 421, and the resin softening unit 500. In other words, the circulation feed liquid inlet of the fresh water circulation tank 405 is connected with the circulation outlet of the first fade chamber 401 and the second fade chamber 421 through a pipeline; the circulating feed liquid outlet of the fresh water circulating tank 405 is connected with the circulating inlets of the first fade chamber 401 and the second fade chamber 421 through pipelines.
In one embodiment, the inlet of the calcium chloride/magnesium recycle tank 406 is connected to the outlet of the concentration chamber 402, the outlet of the calcium chloride/magnesium recycle tank 406 is connected to the inlet of the heat exchange device 407, the outlet of the heat exchange device 407 is connected to the inlet of the concentration chamber 402, and to the second branch 410 which extends to the outside of the treatment system 10. In other words, the circulating feed liquid inlet of the calcium chloride/magnesium circulating box 406 is connected with the circulating outlet of the concentrating chamber 402 through a pipeline, and the circulating feed liquid outlet of the calcium chloride/magnesium circulating box 406 is connected with the circulating inlet of the concentrating chamber 402 through a pipeline. The calcium chloride/magnesium concentrate produced by the concentrating chamber 402 is circulated between the calcium chloride/magnesium circulation tank 406 and the concentrating chamber 402 until the calcium chloride/magnesium concentrate meets the target level and is discharged to the storage tank through the second branch 410. The calcium chloride/magnesium concentrated solution generated by the concentrated chamber 402 is provided with a heat exchange device 407 on an outlet connecting pipeline of the calcium chloride/magnesium concentrated solution circulating box 406 for cooling.
In one embodiment, an inlet of anolyte circulation tank 408 is connected to an outlet of first anode chamber 403 and an outlet of anolyte circulation tank 408 is connected to an inlet of first anode chamber 403. An inlet of the catholyte circulation tank 409 is connected to an outlet of the first cathode chamber 423, and an outlet of the catholyte circulation tank 409 is connected to an inlet of the first cathode chamber 423.
In one embodiment, the first and second diluting chambers 401 and 421 of the electrically driven ion separation membrane unit 400 discharge water into the resin softening unit 500, and the resin softening unit 500 uses a commercial sodium type resin or a weakly acidic resin. And the water from the resin softening unit 500 enters the bipolar membrane unit 600, the bipolar membrane unit 600 being a bipolar electrolysis unit.
According to an embodiment of the present invention, the bipolar membrane unit 600 includes: an acid chamber 602 and a base chamber 603 connected to the acid chamber; a first salt chamber 604 and a second salt chamber 624 connected to the acid chamber 602 and the base chamber 603, respectively; and a second anode chamber 601 and a second cathode chamber 621 connected to the first salt chamber 604 and the second salt chamber 624, respectively.
In one embodiment, bipolar membrane unit 600 further comprises a number of pairs of male membranes, a number of pairs of female membranes, and a number of bipolar membranes. Acid compartment 602 is between bipolar membrane 613 and the anion exchange membrane, base compartment 603 is between the bipolar membrane and the cation exchange membrane, and first salt compartment 604 and second salt compartment 624 are between the anion exchange membrane and the cation exchange membrane. The cathode and anode plates of the second anode chamber 601 and the second cathode chamber 621 are made of titanium ruthenium. In other words, a bipolar membrane 613 is disposed between the acid chamber 602 and the alkali chamber 603, an anion exchange membrane is disposed between the acid chamber 602 and the first salt chamber 604, a cation exchange membrane is disposed between the alkali chamber 603 and the second salt chamber 624, and the bipolar membrane 613 is connected to the water supply branch 614. The water supply branch 614 delivers water.
According to an embodiment of the present invention, the outlet of the resin softening unit 500 is connected to the inlets of the first salt chamber 604 and the second salt chamber 624. In other words, the salt-containing wastewater is treated by the organic matter removing unit 100, the nanofiltration membrane unit 200, the electrically-driven ion separation membrane unit 400, and the resin softening unit 500 into the bipolar membrane unit 600, and further, into the first salt chamber 604 and the second salt chamber 624.
According to an embodiment of the present invention, the bipolar membrane unit 600 further includes: a salt chamber circulation tank 605, an acid chamber circulation tank 606, a base chamber circulation tank 607, a second anolyte circulation tank 608, and a second catholyte circulation tank 609.
In one embodiment, the inlet of the salt chamber circulation tank 605 is connected to the outlets of the first and second salt chambers 604, 624, and the outlet of the salt chamber circulation tank 605 is connected to the inlets of the first and second salt chambers 604, 624 and to a third branch 610 that extends outside of the processing system 10. The third branch 610 conveys a sodium sulfate solution. In other words, the circulating feed liquid inlet of the salt chamber circulation tank 605 is connected to the circulating outlets of the first and second salt chambers 604 and 624 by piping, and the circulating feed liquid outlet of the salt chamber circulation tank 605 is connected to the circulating inlets of the first and second salt chambers 604 and 624 by piping.
In one embodiment, the inlet of the acid chamber circulation tank 606 is connected to the outlet of the acid chamber 602, the outlet of the acid chamber circulation tank 606 is connected to the inlet of the acid chamber 602, and to a fourth branch 611 extending to the exterior of the treatment system 10. In other words, the circulating feed liquid inlet of the acid chamber circulation tank 606 is connected to the circulating outlet of the acid 602 chamber by a pipe, and the circulating feed liquid outlet of the acid chamber circulation tank 606 is connected to the circulating inlet of the acid chamber 602 by a pipe. The acid concentrate produced by the acid chamber 602 is circulated between the acid chamber circulation tank 605 and the acid chamber 602 until the acid concentration satisfies the target level and then discharged to the storage tank through the fourth branch 611. The fourth branch 611 carries a sulfuric acid solution.
In one embodiment, the inlet of the base chamber circulation tank 607 is connected to the outlet of the base chamber 603, and the outlet of the base chamber circulation tank 607 is connected to the inlet of the base chamber 603 and to a fifth branch 612 extending to the exterior of the treatment system 10. The fifth branch 612 carries the sodium hydroxide solution. In other words, the circulation feed liquid inlet of the alkali chamber circulation tank 607 is connected to the circulation outlet of the alkali chamber 603 through a pipe, and the circulation feed liquid outlet of the alkali chamber circulation tank 607 is connected to the circulation inlet of the alkali chamber 603 through a pipe. The alkali concentrate produced in the alkali chamber 603 is circulated between the alkali chamber circulation tank 606 and the alkali chamber 603 until the alkali concentration satisfies the target content and is discharged to the storage tank through the fifth branch 612.
In one embodiment, an inlet of second anolyte circulation tank 608 is connected to an outlet of second anode chamber 601 and an outlet of second anolyte circulation tank 608 is connected to an inlet of second anode chamber 601. The inlet of the second catholyte circulation tank 609 is connected to the outlet of the second cathode chamber 621, and the outlet of the second catholyte circulation tank 609 is connected to the inlet of the second cathode chamber 621.
In one embodiment, the hardness of the secondary reverse osmosis concentrated water of the desalting process of the saline water in a certain coal chemical industry park is 300mg/L, COD to be 300mg/L, TDS to be 17000 and 20000mg/L, and the electric conductivity is 24000 and 30000 us/cm.
The low-consumption high-salt water recycling process is applied to the salt-containing wastewater treatment system and comprises the following steps:
step 1, treating industrial salt-containing wastewater by an organic matter removal unit for 100 to reduce COD to be within 80 mg/L;
step 2, the effluent of the organic matter removal unit 100 passes through a cartridge filter 201 and then enters a nanofiltration membrane unit 200, wherein the hardness is 300mg/L, COD and is 60mg/L, TDS and is 17000 and 20000mg/L, and the conductivity is 24000 and 30000 us/cm; the cartridge filter further removes colloid or particles;
step 3, the water produced by the nanofiltration membrane unit 200 enters a sodium hypochlorite solution produced by a sodium chloride electrolysis device 300, and a water treatment agent is supplied externally, wherein the concentration of sodium chloride in the water produced by the nanofiltration membrane unit 200 is 1.5-3.0%, the COD (chemical oxygen demand) is 20mg/L, and the hardness is lower than 10 mg/L;
step 4, enabling concentrated water of the nanofiltration membrane unit 200 to enter an electrically-driven ion separation membrane unit 400, wherein the hardness is 300mg/L, COD and is 60mg/L, and the salt content is 4-8%;
step 5, the concentrated solution of the electrically driven ion separation membrane unit 400 is divided into two streams, namely a calcium chloride/magnesium solution and a sodium sulfate solution, wherein the calcium chloride/magnesium concentration is 6-10%, and the sodium sulfate concentration is 2-5%;
step 6, electrically driving a fresh chamber of the ion separation membrane unit 400 to generate sodium sulfate solution, allowing the sodium sulfate solution to enter the resin softening unit 500, and reducing the hardness of the resin softening unit 500 to be within 10 mg/L;
and 7, enabling the outlet water of the resin softening unit 500 to enter a bipolar membrane unit 600, wherein the hardness of the inlet water is 5mg/L, the concentration of sodium sulfate is 2-5%, and the bipolar membrane unit 600 generates sulfuric acid and sodium hydroxide solution with the concentration of 0.5-1.0 mol/L.
Through the treatment system 10 for the salt-containing wastewater, provided by the utility model, the salt water softening pretreatment unit is reduced, the chemical agent cost is low, the sludge production and disposal cost are also reduced, the hardness ions are recycled, and the investment cost is saved; the water treatment agent for wastewater treatment is self-sufficient, sodium chloride is prepared into a sodium hypochlorite disinfectant or bactericide, and sodium sulfate is prepared into sulfuric acid and sodium hydroxide; an evaporation crystallization unit of the traditional zero-discharge process is omitted, the energy consumption is greatly reduced, and the operating cost is reduced.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A system (10) for treating salt-containing wastewater, comprising:
the organic matter removing unit (100), the nanofiltration membrane unit (200) and the sodium chloride electrolysis unit (300) are sequentially connected along the flow direction of the salt-containing wastewater;
an electrically-driven ion separation membrane unit (400), a resin softening unit (500) and a bipolar membrane unit (600) which are connected in sequence along the flow direction of the salt-containing wastewater;
wherein the electrically driven ion separation membrane unit (400) is connected with the nanofiltration membrane unit (200), and the electrically driven ion separation membrane unit (400) is arranged at the downstream of the nanofiltration membrane unit (200) along the flow direction of the salt-containing wastewater.
2. The treatment system (10) according to claim 1, wherein the organic matter removal unit (100) comprises an electrochemical oxidation reactor (101), the electrochemical oxidation reactor (101) comprising a cavity (102) and a packing (103) arranged in the cavity (102), the packing (103) being provided with a first anode (104) and a first cathode (105) connected to each other, wherein an inlet of the cavity (102) is connected to the transport pipe (106) of the salt-containing wastewater.
3. The treatment system (10) according to claim 2, wherein the nanofiltration membrane unit (200) comprises a cartridge filter (201), a pressure pump (202) and a membrane module (203) which are connected in sequence along the flow direction of the saline wastewater, and an inlet of the cartridge filter (201) is connected with an outlet of the cavity (102).
4. The treatment system (10) according to claim 3, wherein the sodium chloride electrolysis unit (300) comprises an electrolysis cell (302) and a second anode (303) and a second cathode (304) arranged within the electrolysis cell (302), the second anode (303) being connected to the second cathode (304) by a direct current power supply (301),
wherein an inlet of the electrolysis cell (302) is connected to an outlet of the membrane module (203), and an outlet of the electrolysis cell (302) is connected to a first branch (305) extending to the outside of the treatment system (10).
5. The processing system (10) of claim 3, wherein the electrically driven ion separation membrane unit (400) comprises a dense chamber (402), a first and a second dense chamber (401, 421) connected to the dense chamber (402), and a first anode chamber (403) and a first cathode chamber (423) connected to the first and the second dense chamber (401, 421), respectively, the first and the second dense chamber (401, 421) being connected to the membrane module (203).
6. The processing system (10) of claim 5, wherein the electrically driven ion separation membrane unit (400) further comprises:
a fade chamber circulation tank (405), an inlet of the fade chamber circulation tank (405) being connected to outlets of the first fade chamber (401) and the second fade chamber (421), an outlet of the fade chamber circulation tank (405) being connected to inlets of the first fade chamber (401), the second fade chamber (421), and the resin softening unit (500);
a calcium chloride/magnesium circulation box (406), wherein the inlet of the calcium chloride/magnesium circulation box (406) is connected with the outlet of the concentration chamber (402), the outlet of the calcium chloride/magnesium circulation box (406) is connected with the inlet of a heat exchange device (407), the outlet of the heat exchange device (407) is connected with the inlet of the concentration chamber (402), and a second branch (410) extending to the outside of the treatment system (10) is connected;
an inlet of the anode effusion circulation tank (408) is connected with an outlet of the first anode chamber (403), and an outlet of the anode effusion circulation tank (408) is connected with an inlet of the first anode chamber (403);
a catholyte circulation tank (409), an inlet of the catholyte circulation tank (409) being connected to an outlet of the first cathode chamber (423), an outlet of the catholyte circulation tank (409) being connected to an inlet of the first cathode chamber (423).
7. The treatment system (10) according to claim 1, wherein the bipolar membrane unit (600) comprises:
an acid chamber (602) and a base chamber (603) connected to the acid chamber;
a first salt compartment (604) and a second salt compartment (624) connected to the acid compartment (602) and the base compartment (603), respectively; and
a second anode compartment (601) and a second cathode compartment (621) connected to the first salt compartment (604) and the second salt compartment (624), respectively.
8. The treatment system (10) of claim 7, wherein an outlet of the resin softening unit (500) connects inlets of the first salt chamber (604) and the second salt chamber (624).
9. The treatment system (10) according to claim 7, wherein the bipolar membrane unit (600) further comprises:
a salt chamber circulation tank (605), an inlet of the salt chamber circulation tank (605) being connected to outlets of the first salt chamber (604) and the second salt chamber (624), an outlet of the salt chamber circulation tank (605) being connected to inlets of the first salt chamber (604) and the second salt chamber (624), and a third branch (610) extending to the outside of the treatment system (10);
an acid chamber circulation tank (606), an inlet of the acid chamber circulation tank (606) being connected to an outlet of the acid chamber (602), an outlet of the acid chamber circulation tank (606) being connected to an inlet of the acid chamber (602) and to a fourth branch (611) extending to the outside of the treatment system (10);
an alkali chamber circulation tank (607), an inlet of the alkali chamber circulation tank (607) being connected to an outlet of the alkali chamber (603), an outlet of the alkali chamber circulation tank (607) being connected to an inlet of the alkali chamber (603) and to a fifth branch (612) extending to the outside of the treatment system (10);
a second anolyte circulation tank (608), an inlet of the second anolyte circulation tank (608) being connected to an outlet of the second anode chamber (601), an outlet of the second anolyte circulation tank (608) being connected to an inlet of the second anode chamber (601);
a second catholyte circulation tank (609), an inlet of the second catholyte circulation tank (609) being connected to an outlet of the second cathode chamber (621), an outlet of the second catholyte circulation tank (609) being connected to an inlet of the second cathode chamber (621).
10. The treatment system (10) according to claim 7, wherein a bipolar membrane (613) is arranged between the acid chamber (602) and the base chamber (603), and the bipolar membrane (613) is connected to a water supply branch (614).
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| CN201920356932.8U CN210122533U (en) | 2019-03-20 | 2019-03-20 | Processing system who contains salt waste water |
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| CN201920356932.8U CN210122533U (en) | 2019-03-20 | 2019-03-20 | Processing system who contains salt waste water |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115259484A (en) * | 2022-03-25 | 2022-11-01 | 中国科学院城市环境研究所 | Landfill leachate membrane concentrate inorganic salt recovery and synchronous resource system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115259484A (en) * | 2022-03-25 | 2022-11-01 | 中国科学院城市环境研究所 | Landfill leachate membrane concentrate inorganic salt recovery and synchronous resource system |
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