CN106865865A - Membrane separation process concentrates the processing unit and method of brackish water - Google Patents
Membrane separation process concentrates the processing unit and method of brackish water Download PDFInfo
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- CN106865865A CN106865865A CN201710234910.XA CN201710234910A CN106865865A CN 106865865 A CN106865865 A CN 106865865A CN 201710234910 A CN201710234910 A CN 201710234910A CN 106865865 A CN106865865 A CN 106865865A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 247
- 239000012528 membrane Substances 0.000 title claims abstract description 46
- 238000000926 separation method Methods 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 27
- 239000012141 concentrate Substances 0.000 title claims abstract description 22
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 239
- 239000011780 sodium chloride Substances 0.000 claims abstract description 121
- 238000000909 electrodialysis Methods 0.000 claims abstract description 46
- 229910052925 anhydrite Inorganic materials 0.000 claims abstract description 39
- 229910052602 gypsum Inorganic materials 0.000 claims abstract description 27
- 239000010440 gypsum Substances 0.000 claims abstract description 27
- 238000002425 crystallisation Methods 0.000 claims abstract description 17
- 230000008025 crystallization Effects 0.000 claims abstract description 17
- 238000003672 processing method Methods 0.000 claims abstract description 16
- 230000008569 process Effects 0.000 claims abstract description 15
- 150000003839 salts Chemical class 0.000 claims abstract description 7
- 239000013078 crystal Substances 0.000 claims abstract description 6
- 239000013505 freshwater Substances 0.000 claims abstract description 3
- 238000001223 reverse osmosis Methods 0.000 claims description 36
- 239000003643 water by type Substances 0.000 claims description 32
- 239000004571 lime Substances 0.000 claims description 19
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 16
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 14
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 238000001764 infiltration Methods 0.000 claims description 10
- 238000005341 cation exchange Methods 0.000 claims description 8
- 150000002500 ions Chemical class 0.000 claims description 5
- 238000005370 electroosmosis Methods 0.000 claims description 4
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 3
- 239000008213 purified water Substances 0.000 claims description 3
- 239000000725 suspension Substances 0.000 claims description 3
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 abstract description 6
- 239000012267 brine Substances 0.000 abstract description 3
- 239000010842 industrial wastewater Substances 0.000 abstract description 3
- 239000013535 sea water Substances 0.000 abstract description 2
- 238000001704 evaporation Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000003014 ion exchange membrane Substances 0.000 description 3
- 229910001415 sodium ion Inorganic materials 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000012266 salt solution Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000031018 biological processes and functions Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 229910001410 inorganic ion Inorganic materials 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
- 239000002453 shampoo Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/06—Preparation by working up brines; seawater or spent lyes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/46—Sulfates
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
- C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/101—Sulfur compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Materials Engineering (AREA)
- Geology (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses processing unit and method that a kind of membrane separation process concentrates brackish water, processing unit includes：Brackish water raw water box；Electrodialysis plant, connects with brackish water raw water box；CaSO4Water tank is produced, is connected with electrodialysis plant freshwater room, for receiving the CaSO in electrodialysis plant4Produce water；NaCl produces water tank, is connected with electrodialysis plant concentrated water room；Evaporated crystallization device, produces water tank and connects, for obtaining NaCl crystal salts with NaCl；Gypsum cyclone, with CaSO4Water tank connection is produced, for gypsum primary dewatering；Vacuum belt dewaterer, connects with gypsum cyclone underflow outlet, is further dehydrated for gypsum, obtains gypsum.Membrane separation process of the invention concentrates the processing unit simple structure of brackish water, and processing method simple operation can be used for containing Na+,Ca2+‑Cl‑,SO4 2‑The concentration decrement process of the industrial wastewater/seawater/subsurface brine/salt lake saline of system, while being recycled to the component in water.
Description
Technical field
The present invention relates to water treatment field, espespecially a kind of membrane separation process concentrates the processing unit and method of brackish water.
Background technology
In recent years, the demand with people for water resource constantly increases with the sharp increase of the size of population, shortage of water resources
Phenomenon is increasingly aggravated.And the fast development of social economy, certainly will be along with substantial amounts of life and the generation of industrial wastewater.Wherein
Contain a certain amount of dissolubility inorganic ion (such as Na+,Ca2+-Cl-,SO4 2-System) waste water be brine waste, when salinity >=
When 1%, we can be referred to as high-salt wastewater.Any discharge of brine waste, can not only influence people's Drinking Water quality,
Industrial and agricultural production can be also endangered, difficulty of Organic Wastewater Treatment by Biological Process etc. is increased.
UF membrane refers to that in the presence of outside energy or chemical potential difference, the selection using film to different material passes through energy
The property that power has differences reaches the method to material separating-purifying.The purification side that membrane separation technique is got up as latest developments
Method and isolation technics, compared with traditional lock out operation, have the advantages that energy-conservation, efficient, simple to operate, low cost and cleaning.
In addition, membrane separation technique and other technologies be combined with there is extraordinary effect in terms of wastewater treatment, can be very good
Solve a series of relevant issues of wastewater treatment.
Therefore, the applicant is devoted to providing processing unit and method that a kind of new membrane separation process concentrates brackish water.
The content of the invention
It is an object of the invention to provide processing unit and method that a kind of membrane separation process concentrates brackish water, apparatus structure letter
Single, processing method simple operation can be used for containing Na+,Ca2+-Cl-,SO4 2-Industrial wastewater/seawater/subsurface brine/the salt of system
The concentration decrement process of lake water, while being recycled to the component in water.
In order to solve the above technical problems, the invention provides the processing unit that a kind of membrane separation process concentrates brackish water, including：
Brackish water raw water box, for storing brackish water；Electrodialysis plant, connects, for the saliferous with the brackish water raw water box
Water carries out electrodialysis process；Saliferous water pump, connects with the brackish water raw water box, for by containing in the brackish water raw water box
Salt solution is delivered in the electrodialysis plant；NaCl produces water tank, is connected with the concentrated water room of the electrodialysis plant, for receiving
The NaCl stated in electrodialysis plant produces water；CaSO4Water tank is produced, the freshwater room with the electrodialysis plant is connected, for receiving
State the CaSO in electrodialysis plant4Produce water；Evaporated crystallization device, produces water tank and connects with the NaCl, enters for producing water to NaCl
Row evaporative crystallization；Gypsum cyclone, with the CaSO4Water tank connection is produced, for gypsum primary dewatering；Vacuum belt dewaterer,
Underflow outlet with the gypsum cyclone is connected, and is further dehydrated for gypsum；The cation exchange of the electrodialysis plant
Film uses Monovalent selectivity cation-exchange membrane.
Preferably, the electrodialysis plant used frequently pole-reversing electroosmosis device, every 15-20 minutes conversion dc source
Positive and negative electrode polarity, is reversed ion flow.
Preferably, the processing unit of the membrane separation process concentration brackish water also includes：Reverse osmosis unit, produces with the NaCl
Water tank is connected, and reverse-osmosis treated is carried out for producing water to the NaCl；High-pressure pump, produces water tank and counter-infiltration with the NaCl respectively
Device is connected, and the NaCl for producing the NaCl in water tank produces water and is delivered in the reverse osmosis unit；NaCl condensed water water
Case, connects with the reverse osmosis unit, for receiving the NaCl condensed waters in the reverse osmosis unit.
Preferably, the processing unit of the membrane separation process concentration brackish water also includes：Plate type heat exchanger, is arranged on described
NaCl is produced between water tank and NaCl concentration water tanks, and its water inlet end and the NaCl concentration water tank are connected, its water side and institute
State NaCl and produce water tank connection, for being lowered the temperature to the NaCl condensed waters and be delivered to the NaCl condensed waters after cooling described
NaCl is produced in water tank；Circulating pump, is arranged on the plate type heat exchanger and the NaCl and produces between water tank, for board-like being changed described
NaCl condensed waters after lowering the temperature in hot device are back in the NaCl products water tank.
Preferably, the processing unit of the membrane separation process concentration brackish water also includes：Lime dosing tank, the lime dosing
The outlet of case and the CaSO4Water tank connection is produced, for the CaSO4Producing water tank dispensing lime makes lime and CaSO4Produce water tank
In unnecessary SO4 2-Reaction, generates CaSO4。
The invention also discloses the processing method that a kind of membrane separation process concentrates brackish water, including step：
S10：First brackish water is pre-processed, the suspension in brackish water is reduced, electrodialysis plant flow condition is reached；
S20：Electrodialysis process is carried out to pretreated brackish water and obtains NaCl products water and CaSO4Produce water；
S30：Water is produced to NaCl and is evaporated crystallization treatment, obtain the NaCl crystal salts of high-purity；
S40：To CaSO4Producing water carries out two-stage dewater treatment, obtains gypsum of the moisture content less than 10%.
Preferably, in the step S20, pretreated brackish water is entered by Monovalent selectivity cation-exchange membrane
Row electrodialysis process.
Preferably, the processing method of the membrane separation process concentration brackish water also includes step：
S50：Reverse-osmosis treated is carried out to NaCl product water and is purified water and NaCl condensed waters；
Preferably, the processing method of the membrane separation process concentration brackish water also includes step：
S60：Cooling treatment is carried out to the NaCl condensed waters；
S70：NaCl condensed waters after cooling is processed are produced after water mixes with the NaCl and carry out reverse-osmosis treated again, so that
Form the interior circulation counter-infiltration that NaCl produces water.
Preferably, the processing method of the membrane separation process concentration brackish water also includes step：
S80：To the CaSO4Lime, the lime and CaSO are added in product water4Produce the unnecessary SO in water4 2-Reaction, improves
CaSO4Produce water concentration.
The processing unit and method of membrane separation process concentration brackish water of the invention can realize following any one beneficial effect
Really.
1st, the processing unit of membrane separation process concentration brackish water of the invention is by using Monovalent selectivity cation-exchange membrane
Electrodialysis plant treatment brackish water obtain CaSO4Produce water and NaCl and produce water, thus calcium in effective recycling brackish water from
Son and sodium ion, water evaporation crystallization, CaSO are produced by follow-up NaCl4The process steps such as product water second dehydration can obtain NaCl and consolidate
Body and gypsum, processing unit simple structure, low cost, process method step are few, easy to operate, and the concentration for realizing brackish water subtracts
Amount.
2nd, the present invention passed through to use frequently pole-reversing electroosmosis device, every 15-20 minutes conversion dc source positive and negative electrode
Polarity, is reversed ion flow, can automatically clean the dirt that electrodialysis plant amberplex and electrode surface are formed, with
Ensure that the long-time stability and device of ion exchange membrane efficiency produce the water quality and quantity of water.
3rd, when the NaCl product water concentrations obtained after being processed by electrodialysis plant are relatively low, first NaCl product water is first sent into instead
Evaporation and crystallization system is entered back into after permeability apparatus concentration decrement, the evaporated water of subsequent evaporation crystalline element is reduced, evaporation is reduced
Crystalline element energy consumption and investment；And the NaCl condensed waters after counter-infiltration flow back according to a certain percentage, form interior circulation counter-infiltration
Unit, improves the deposit that membrane component surface transverse flow speed comes flushing membrane surface, prevents the film surface in reverse osmosis process from producing
Scale formation.
4th, in NaCl condensed water interior circulation reverse osmosis units, NaCl condensed waters are first made to reduce water by heat exchanger cooling
Temperature, it is to avoid NaCl condensed waters are excessive due to cycle-index, be heated by high-pressure pump extruding cause temperature rise it is too fast and to equipment
Cause to damage；The useless heat energy that cooling water is produced after being exchanged heat through heat exchanger in recyclable concentration water cycle process, can be used to evaporate
The primary heating process of crystalline element thermal source, it can also be used to other heating workshop sections, realizes the cascade utilization of the energy and recycles.
5th, the CaSO for being obtained after being processed by electrodialysis plant4Produce water concentration relatively low, and SO4 2-When ion concentration is higher,
Can be in CaSO4Produce addition lime and SO in water4 2-Reaction, improves CaSO4Water concentration is produced, increases the rate of recovery of gypsum.
Brief description of the drawings
The present invention is described in further detail with reference to the accompanying drawings and detailed description：
Fig. 1 is a kind of structural representation of specific embodiment of the processing unit of membrane separation process concentration brackish water of the invention
Figure；
Fig. 2, Fig. 3, Fig. 4 are another three kinds of specific embodiments of the processing unit of membrane separation process concentration brackish water of the invention
Structural representation.
Drawing reference numeral explanation：
Brackish water raw water box 1, saliferous water pump 2, electrodialysis plant 3, NaCl produces water tank 4, CaSO4Produce water tank 5, evaporative crystallization
Device 6, NaCl crystal salts 7, gypsum cyclone 8, vacuum belt dewaterer 9, gypsum 10, high-pressure pump 11, reverse osmosis unit 12,
NaCl concentrates water tank 13, heat exchanger 14, circulating pump 15, lime dosing tank 16.
Specific embodiment
In order to illustrate more clearly about the embodiment of the present invention or technical scheme of the prior art, below will be to embodiment or existing
The accompanying drawing to be used needed for having technology description is briefly described, it should be apparent that, drawings in the following description are only this
Some embodiments of invention, for those of ordinary skill in the art, on the premise of not paying creative work, can be with
Other accompanying drawings are obtained according to these accompanying drawings.
Embodiment one
Present embodiment discloses a kind of processing unit of reverse osmosis concentration brackish water, as shown in figure 1, anti-in the present embodiment
The processing unit of osmosis concentration brackish water includes：Brackish water raw water box 1, for storing brackish water；Electrodialysis plant 3, with saliferous
Water raw water box 1 is connected, for carrying out electrodialysis process to brackish water；CaSO4Water tank 5 is produced, is connected with electrodialysis plant 3, be used for
Receive the CaSO in electrodialysis plant 34Produce water；NaCl produces water tank 4, is connected with electrodialysis plant 3, for receiving electrodialysis plant
NaCl in 3 produces water；Evaporated crystallization device 6, produces water tank 4 and connects with NaCl, and crystallization is evaporated for producing water to NaCl；Gypsum
Cyclone 8, with CaSO4Produce water tank 5 to connect, for gypsum primary dewatering；Vacuum belt dewaterer 9, with the underflow of gypsum cyclone 8
Outlet, is further dehydrated for gypsum.
Specifically, electrodialysis plant 3 is provided with homogeneous monovalention exchange membrane, homogeneous monovalention exchange membrane contains for treatment
Brackish water in salt solution raw water box simultaneously forms NaCl and produces water and CaSO4Produce water.
Specifically, electrodialysis plant 3 uses frequently pole-reversing electroosmosis device, every 15-20 minutes conversion dc source just
Negative electrode polarity, is reversed ion flow, the dirt that automatic cleaning electrodialysis plant amberplex and electrode surface are formed
Dirt, it is ensured that the long-time stability and device of ion exchange membrane efficiency produce the water quality and quantity of water.
In addition, CaSO4Produce the CaSO in water tank4Produce water follow-up by the secondary of gypsum cyclone and vacuum belt dewaterer
Dewater treatment obtains gypsum 10, and the NaCl that NaCl is produced in water tank produces water and can obtain NaCl crystallizations by evaporative crystallization cell processing
Salt 7, gypsum 10 and NaCl crystal salts 7 can be reused, it is achieved thereby that the secondary utilization to saliferous water component, section
The about energy.
Embodiment two
As shown in Fig. 2 another specific implementation of the processing unit present embodiment discloses reverse osmosis concentration brackish water
Example, its structure is essentially identical with embodiment one, and difference is that in the present embodiment, increased the counter-infiltration that NaCl produces water
Upgrading unit, including：Reverse osmosis unit 12, produces water tank 4 and connects with NaCl, is carried out at counter-infiltration for producing water to the NaCl
Reason；High-pressure pump 11, produces water tank 4 and reverse osmosis unit connects 12, for the NaCl to be produced the NaCl in water tank 4 with NaCl respectively
Water is produced to be delivered in the reverse osmosis unit 12；NaCl concentrates water tank 13, is connected with reverse osmosis unit 12, for receiving reverse osmosis
NaCl condensed waters in saturating device 12.
Embodiment three
As shown in figure 3, another specific implementation of the processing unit present embodiment discloses reverse osmosis concentration brackish water
Example, its structure is essentially identical with embodiment two, and difference is that in the present embodiment, increased and followed in NaCl condensed waters
Ring reverse osmosis units, including heat exchanger 14, heat exchanger 14 are arranged between NaCl concentration water tanks 13 and NaCl product water tanks 4, and
Its water inlet is connected with NaCl concentration water tanks 13, and delivery port produces water tank 4 and connects with NaCl, for being dropped to NaCl condensed waters
Simultaneously be delivered to the NaCl condensed waters after cooling in NaCl product water tanks 4 by temperature.In the present embodiment, heat exchanger 10 by cooling water with
NaCl condensed waters carry out heat exchange, so as to realize the cooling of NaCl condensed waters.
Specifically, the processing unit of reverse osmosis concentration brackish water also includes circulating pump 15, circulating pump 15 is arranged on heat exchanger
14 and NaCl produce water tank 4 between, for by heat exchanger 14 lower the temperature after NaCl condensed waters deliver to NaCl produce water tank 4 in.
The processing unit of the reverse osmosis concentration brackish water in the present embodiment (is pressed according to a certain percentage by by NaCl condensed waters
According to the facts border it needs to be determined that) backflow, concentration is circulated in reverse osmosis unit, such that it is able to reduce subsequent evaporation crystalline element steaming
Shampoo amount, reduces evaporative crystallization unit energy consumption and investment, by setting heat exchanger it is possible to prevente effectively from NaCl condensed waters are due to following
Ring number of times is excessive, and is heated by high-pressure pump extruding and causes temperature to rise too fast and equipment is caused to damage；Cooling water is through changing
The useless heat energy produced in recyclable concentration water cycle process after hot device heat exchange, the primary that can be used for evaporative crystallization unit thermal source adds
Thermal process, it can also be used to other heating workshop sections, realizes the cascade utilization of the energy and recycles.
Of course, in other specific embodiments, electrodialysis plant of the invention can also use other kinds of ion
Exchange membrane；The species model of reverse osmosis unit can be selected according to actual needs；Saliferous water pump, high-pressure pump and circulating pump
Can be selected as needed；NaCl condensed waters after cooling can be filled by being directly inputted into counter-infiltration after heat exchanger
In putting；Additionally, NaCl condensed waters can not be directly inputted in NaCl product water tanks or reverse osmosis unit by heat exchanger, also
It is to say that heat exchanger can selectively be set, heat exchange side's examination of heat exchanger can also be adjusted according to actual needs, herein no longer
Repeat.
Example IV
As shown in figure 4, another specific implementation of the processing unit present embodiment discloses reverse osmosis concentration brackish water
Example, its structure is essentially identical with embodiment one, and difference is that in the present embodiment, increased CaSO4The lime for producing water adds
Prescription unit, including：Lime dosing tank 16, outlet and CaSO4Produce water tank 5 to connect, for CaSO4Lime is added in product water tank 5,
Make lime and CaSO4Produce the unnecessary SO in water tank 54 2-Reaction, generates CaSO4。
Embodiment five
The invention also discloses a kind of processing method of reverse osmosis concentration brackish water, including step：
S10：First brackish water is pre-processed, the suspension in brackish water is reduced, electrodialysis plant flow condition is reached；
S20：Electrodialysis process is carried out to pretreated brackish water and obtains NaCl products water and CaSO4Produce water；S30：Water is produced to NaCl to enter
The treatment of row evaporative crystallization, obtains the NaCl crystal salts of high-purity；S40：To CaSO4Producing water carries out two-stage dewater treatment, is contained
Gypsum of the water rate less than 10%.
Specifically, in the step S20, being entered to pretreated brackish water by Monovalent selectivity cation-exchange membrane
Row electrodialysis process.
Specifically, the processing method of the membrane separation process concentration brackish water also includes step：S50：Water is produced to the NaCl
Carry out reverse-osmosis treated and be purified water and NaCl condensed waters；
Specifically, the processing method of the membrane separation process concentration brackish water also includes step：S60：The NaCl is concentrated
Water carries out cooling treatment；S70：NaCl condensed waters after cooling is processed are produced after water mixes with the NaCl and carried out at counter-infiltration again
Reason, so as to form the interior circulation counter-infiltration that NaCl produces water.
Specifically, the processing method of the membrane separation process concentration brackish water also includes step：S80：To the CaSO4Produce water
Middle addition lime, with CaSO4Produce the unnecessary SO in water tank4 2-Reaction, improves CaSO4Produce water concentration.
Of course, in other specific embodiments, the processing method of reverse osmosis concentration brackish water of the invention can also be adopted
Cooling treatment is carried out to NaCl condensed waters with the type of cooling of other forms；NaCl condensed waters after cooling can not be produced with NaCl
Water mixes, but is directly evaporated concentration；Additionally, this method is also applied for Li+,Mg2+-Cl-,SO4 2-Etc. system
First, the separation method of bivalent metal ion.
The above is only the preferred embodiment of the present invention, it is noted that for the ordinary skill people of the art
For member, under the premise without departing from the principles of the invention, some improvements and modifications can also be made, these improvements and modifications also should
It is considered as protection scope of the present invention.
Claims (10)
1. a kind of membrane separation process concentrates the processing unit of brackish water, it is characterised in that including：
Brackish water raw water box, for storing brackish water；
Electrodialysis plant, connects with the brackish water raw water box, for carrying out electrodialysis process to the brackish water；
Saliferous water pump, connects with the brackish water raw water box, for the brackish water in the brackish water raw water box to be delivered into institute
In stating electrodialysis plant；NaCl produces water tank, is connected with the concentrated water room of the electrodialysis plant, for receiving the electrodialysis plant
In NaCl produce water；
CaSO4Water tank is produced, the freshwater room with the electrodialysis plant is connected, for receiving the CaSO in the electrodialysis plant4Produce
Water；
Evaporated crystallization device, produces water tank and connects with the NaCl, and crystallization is evaporated for producing water to NaCl；
Gypsum cyclone, with the CaSO4Water tank connection is produced, for gypsum primary dewatering；
Vacuum belt dewaterer, the underflow outlet with the gypsum cyclone is connected, and is further dehydrated for gypsum；
The cation-exchange membrane of the electrodialysis plant uses Monovalent selectivity cation-exchange membrane.
2. membrane separation process as claimed in claim 1 concentrates the processing unit of brackish water, it is characterised in that：
The electrodialysis plant used frequently pole-reversing electroosmosis device, every 15-20 minutes conversion dc source positive and negative electrode pole
Property, it is reversed ion flow.
3. the membrane separation process as any one of claim 1-2 concentrates the processing unit of brackish water, it is characterised in that also wrap
Include：
Reverse osmosis unit, produces water tank and connects with the NaCl, and reverse-osmosis treated is carried out for producing water to the NaCl；
High-pressure pump, produces water tank and reverse osmosis unit is connected, for the NaCl to be produced the NaCl in water tank with the NaCl respectively
Water is produced to be delivered in the reverse osmosis unit；
NaCl concentrates water tank, is connected with the reverse osmosis unit, for receiving the NaCl condensed waters in the reverse osmosis unit.
4. membrane separation process as claimed in claim 3 concentrates the processing unit of brackish water, it is characterised in that also include：
Plate type heat exchanger, is arranged on the NaCl and produces between water tank and NaCl concentration water tanks, and its water inlet end is dense with the NaCl
Shrink water tank is connected, and its water side and the NaCl produce water tank and connect, for being lowered the temperature to the NaCl condensed waters and will be dropped
NaCl condensed waters after temperature are delivered in the NaCl products water tank；
Circulating pump, is arranged between the plate type heat exchanger and NaCl product water tanks, for that will be dropped in the plate type heat exchanger
NaCl condensed waters after temperature are back in the NaCl products water tank.
5. membrane separation process as claimed in claim 1 concentrates the processing unit of brackish water, it is characterised in that also include：
Lime dosing tank, outlet and the CaSO of the lime dosing tank4Water tank connection is produced, for the CaSO4Produce water tank
Delivering lime makes lime and CaSO4Produce the unnecessary SO in water tank4 2-Reaction, generates CaSO4。
6. a kind of membrane separation process concentrates the processing method of brackish water, it is characterised in that including step：
S10：First brackish water is pre-processed, the suspension in brackish water is reduced, electrodialysis plant flow condition is reached；
S20：Electrodialysis process is carried out to pretreated brackish water and obtains NaCl products water and CaSO4Produce water；
S30：Water is produced to NaCl and is evaporated crystallization treatment, obtain the NaCl crystal salts of high-purity；
S40：To CaSO4Producing water carries out two-stage dewater treatment, obtains gypsum of the moisture content less than 10%.
7. membrane separation process as claimed in claim 6 concentrates the processing method of brackish water, it is characterised in that：
In the step S20, pretreated brackish water is carried out at electrodialysis by Monovalent selectivity cation-exchange membrane
Reason.
8. membrane separation process as claimed in claim 6 concentrates the processing method of brackish water, it is characterised in that also including step：
S50：Reverse-osmosis treated is carried out to NaCl product water and is purified water and NaCl condensed waters.
9. membrane separation process as claimed in claim 8 concentrates the processing method of brackish water, it is characterised in that also including step：
S60：Cooling treatment is carried out to the NaCl condensed waters；
S70：NaCl condensed waters after cooling is processed are produced after water mixes with the NaCl and carry out reverse-osmosis treated again, so as to be formed
NaCl produces the interior circulation counter-infiltration of water.
10. membrane separation process as claimed in claim 6 concentrates the processing method of brackish water, it is characterised in that also including step：
S80：To the CaSO4Lime, the lime and CaSO are added in product water4Produce the unnecessary SO in water4 2-Reaction, improves
CaSO4Produce water concentration.
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