CN108558099A - A kind of zero-discharge treatment system of high slat-containing wastewater - Google Patents
A kind of zero-discharge treatment system of high slat-containing wastewater Download PDFInfo
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- CN108558099A CN108558099A CN201810004576.3A CN201810004576A CN108558099A CN 108558099 A CN108558099 A CN 108558099A CN 201810004576 A CN201810004576 A CN 201810004576A CN 108558099 A CN108558099 A CN 108558099A
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- 238000011282 treatment Methods 0.000 title claims description 19
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- 238000001223 reverse osmosis Methods 0.000 claims abstract description 81
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 61
- 239000012267 brine Substances 0.000 claims abstract description 54
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 53
- 239000002699 waste material Substances 0.000 claims abstract description 40
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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
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
-
- 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
- C02F1/46—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
- C02F1/4698—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electro-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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
- C02F5/06—Softening water by precipitation of the hardness using calcium compounds
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention relates to a kind of processing systems of brine waste, including recycling pretreatment unit, recycle minimizing unit and zero-emission unit, it is characterized in that, production water after cycle pretreatment unit is used to react high slat-containing wastewater with pre-treatment medicaments passes through dispatch after the filtering of tubular type microstrainer to cycle minimizing unit, it recycles minimizing unit and preliminary minimizing processing is carried out to the production water of cycle pretreatment unit processing by reverse osmosis unit, and the multistage electrically-driven ion film device by being made of at least one electrically-driven ion film device carries out depth concentration with the moisture in further minimizing separation high slat-containing wastewater to fresh water tanks reuse, the concentration mixing saline solution dispatch that depth is concentrated to give is to zero-emission unit, zero-emission unit passes through to concentration mixing saline solution heating, evaporation, crystallization is to recycle salt made from earth containing a comparatively high percentage of sodium chloride and sodium salt in concentration mixing saline solution.The present invention detaches final mixed salt and accounts for total salt amount 5% hereinafter, all recyclings of production water, reach wastewater zero discharge.
Description
The present invention is that original applying number is 201510981321.9, and the applying date is on December 23rd, 2015, original name is：
A kind of divisional application of the zero-discharge treatment system of high slat-containing wastewater.
Technical field
At the zero discharge treatment field of high slat-containing wastewater more particularly to a kind of zero-emission of high slat-containing wastewater
Reason system.
Background technology
In recent years, it with the fast development of the industries such as petrochemical industry, electric power, metallurgy, coal chemical industry, is generated in industrial processes
The sewage quantities containing complicated component such as reverse osmosis concentrated water, trade effluent, circulating sewage and some processes draining increase year by year, these
The sewage of complicated component how widely paid attention to by final disposal and Utilizing question.
Currently, for the processing method of the complicated waste water containing hardly degraded organic substance with high salt, it is mainly the following scheme：
First, (mainly there are ozone, hydrogen peroxide using oxidizing species to the hardly degraded organic substance substance in waste water
Deng) carry out catalysis oxidation, so that hardly degraded organic substance substance in waste water is effectively degraded, it is oxidation-treated after waste water again into
Enter biochemical unit to be removed the organic matter in sewage, by precipitating and direct emission after filter element；
Second, by calcic magnesium hardness waste water by softening after, then decrement treatment carried out into one by secondary reverse osmosis unit
Walk recovery section water, the concentrated water direct emission generated after minimizing；
Third, high-salt concentrated water zero-emission disposition after minimizing by concentrated water with high salt using more evaporations at crystalline element
Reason forms mixed salt class, realizes the zero-emission of water.
Comprehensive analysis three of the above scheme, the first scheme are effectively treated digestion just for the organic matter in waste water,
General sewage disposal is all by longer biochemical treatment flow, and remainder biodegradability of organic matter is very poor in waste water, very
Extremely cannot be biochemical, therefore, it is limited to the removal effect of the part to depend merely on chemical catalytic oxidation, most importantly to waste water
Inorganic salts ingredients are acted on without removal substantially；Second scheme to raw water from technique although carry out certain decrement treatment, however, instead
It has been that raw water has been carried out the high-salt wastewater after at least 4 times concentrations, all calcium ions, magnesium ion, a huge sum of money to permeate concentrated water to be
Category ion, silicon ion etc., and the pollutant concentrations such as not biochemical organic matter are very high, therefore, common reverse osmosis membrane
The rate of recovery to the waste water, which is not high or even sea water desalination membrane, can only also accomplish 50% or so, although generated concentrated water carries out
Decrement but the concentrated water water or bigger generated, still have the relatively strong brine for accounting for total 10% or more water of processing to produce environment
Raw very big influence；The third scheme handles more thoroughly to high-salt wastewater after concentration, and relative skill is ripe, only processing cost
It is too high, it needs to consume a large amount of steam in the process, according to the final general cost of water treatment of concentrated water salt concentration at 50 yuan/ton or more,
General only to detach a kind of salt or directly form mixed salt, which needs progress specially treated as dangerous waste object, and cost is very high, the method
Big yield haline water is carried out handling its investment cost and operating cost is all very high, enterprise is unacceptable.
Chinese patent (103482810 B of CN) provides a kind of zero discharge treatment of novel high-salinity heavy metal wastewater
System, including waste water adjusts and oxidation pond, waste water lifting pump, filter, spray cooler, the waste water adjusts and oxidation pond
On have waterwater entrance, air intake and a wastewater outlet, spray cooler is equipped with high-temperature flue gas entry, low-temperature flue gas outlet, useless
Water inlet, the waste water adjust and oxidation pond on wastewater outlet be connected with the entrance of waste water lifting pump, the filter enters
Mouth is connected with the outlet of waste water lifting pump, and filter outlet is connected with the waterwater entrance of spray cooler, the spray cooler
It is interior to be equipped with atomizer.Although the patented technology realizes zero discharge treatment to high-salinity heavy metal wastewater, the patent
Using the third scheme, processing cost is higher, needs to consume a large amount of steam in processing procedure, and only isolates a kind of salt or straight
It connects to form mixed salt.The mixed salt needs to carry out specially treated as dangerous waste object, further increases cost.The patented technology is to big yield
Haline water carries out handling its investment cost and operating cost is all very high, and enterprise is beyond affordability and uses.
Therefore, in the market there is an urgent need for a kind of zero-discharge treatment system of low cost, treated salt can classify place
Economic value is managed and generated, not only environmental protection but also be enterprise through low cost, creates economic value.
Invention content
For the deficiency of the prior art, the present invention provides a kind of zero-discharge treatment system of high slat-containing wastewater, including cycle
Pretreatment unit, cycle minimizing unit and zero-emission unit, which is characterized in that
Production water after the cycle pretreatment unit is used to react high slat-containing wastewater with pre-treatment medicaments is micro- by tubular type
Dispatch is to the cycle minimizing unit after filter filtering,
The cycle minimizing unit carries out just the production water of the cycle pretreatment unit processing by reverse osmosis unit
Minimizing processing is walked, and the multistage electrically-driven ion film device by being made of at least one electrically-driven ion film device carries out
Depth concentration detaches the moisture in high slat-containing wastewater to fresh water tanks reuse with further minimizing, what depth was concentrated to give
Concentration mixing saline solution dispatch to the zero-emission unit,
The zero-emission unit is mixed by mixing saline solution heating, evaporation to the concentration, crystallizing with recycling the concentration
Salt made from earth containing a comparatively high percentage of sodium chloride in saline solution and sodium salt.
According to a preferred embodiment, the cycle pretreatment unit includes at least regulating reservoir, highly dense pond, tubular type micro-filtration
Device and sludge-tank,
The highly dense pond generates after mixing the brine waste for measuring adjusting by the regulating reservoir homogeneous and pre-treatment medicaments
Sludge according to the sludge-tank for draining into its underpart under gravity, by pre-treatment medicaments treated the production water in the highly dense pond
Enter cycle minimizing unit after handling via the tubular type microstrainer micro-filtration to be handled；
Wherein, the sludge in the sludge-tank carried out in the form of press filtration by sludge dehydrating and drying device mud-water separation and
The water of separation abjection is vented back to the regulating reservoir or the highly dense pond carries out cycle pretreatment again.
According to a preferred embodiment, the cycle minimizing unit is filled including at least at least one electrically-driven ion film
Set, middle pressure reverse osmosis unit, high pressure reverse osmosis unit, active carbon filter, the second tubular type microstrainer, second level reverse osmosis apparatus and
Fresh water tanks,
The high pressure reverse osmosis unit will be concentrated by medium pressure reverse osmosis unit in a manner of middle pressure osmosis filtration described
The concentrated water that the production water of cycle pretreatment unit discharge obtains obtains after being concentrated into horizontal high voltage osmosis filtration, to be carried out to production water
Preliminary minimizing processing；
The fresh water that medium pressure reverse osmosis unit and the high pressure reverse osmosis unit generate is filled via the two-pass reverse osmosis
Reuse is set after being purified in a manner of reverse osmosis and ultraviolet-sterilization to the fresh water tanks；
The active carbon filter and the second tubular type microstrainer is filtered successively to the counter-infiltration dope and calcium
Dispatch to the multistage electrically-driven ion film device carries out depth minus quantification treatment after magnesium ion softening；
The multistage electrically-driven ion film device includes that the first electrically-driven ion film device and the second electrically-driven ion film fill
Set, the second electrically-driven ion film device by the TDS of the first electrically-driven ion film device thickening filtration be 1.2 ×
105The concentrated water of mg/l carries out secondary concentration and TDS is obtained by filtration to be 2 × 105The concentration mixing salt solution of mg/l, wherein
The isolated desalted water of the second electrically-driven ion film device be vented back to medium pressure reverse osmosis unit with into
The cycle minimizing processing of row primary minimizing and depth concentration.
According to a preferred embodiment, the zero-emission unit includes at least feedstock preheater, nitre evaporative crystallization
Device, nitre thickener, nitre circulating pump, the first vapour compression machine, at least one drying equipment, cooling water system, salt evaporative crystallization
Device,
The cycle minimizing unit preheated by the feedstock preheater is discharged the nitre evaporated crystallization device
Concentration mixing salt solution the nitre evaporated crystallization device be vented back to after nitre circulating pump, primary heater successively recycled
Heating is concentrated and separated out salt made from earth containing a comparatively high percentage of sodium chloride and feed liquid with evaporative crystallization,
The feed liquid enters whizzer by the nitre thickener is dried with the salt made from earth containing a comparatively high percentage of sodium chloride that will be centrifuged out through first
It is packaged as commodity salt made from earth containing a comparatively high percentage of sodium chloride after equipment drying,
The nitre mother liquor freezing that the whizzer is isolated enters freezing nitre crystallizing tank after being spent up to -5 and by freezing nitre
Isolated ten water nitre is recycled to the circulation crystallization separation that the feedstock preheater carries out salt made from earth containing a comparatively high percentage of sodium chloride by whizzer,
The supersaturated feed liquid dispatch of the freezing nitre whizzer separation is to the salt evaporated crystallization device to centrifuge point
From obtaining commodity salt.
According to a preferred embodiment, the nitre crystallizing evaporator steams under negative pressure/or slight positive pressure state by first
The low temperature secondary dead steam that vapour compressor generates evaporation is compressed to improve steam exhaust temperature, so that the nitre circulating pump, first
The circulating heater that heater and the nitre crystallizing evaporator are formed has continual and steady thermal energy,
The nitre evaporated crystallization device utilizes reference under conditions of extracting and compressing indirect steam of the first vapour compression machine
Nitre crystallization required temperature is freezed to connect cooling water system by first vapour compression machine and utilize cooler and/or refrigeration station
Keep required temperature inside the freezing nitre crystallization apparatus.
According to a preferred embodiment, the nitre mother liquor that the whizzer is isolated enters nitre mother liquor tank, and through nitre
Mother liquor pump enters the freezing nitre crystallization apparatus and carries out decrease temperature crystalline, and the nitre mother liquor carries out in the freezing nitre crystallization apparatus
It is adjusted after being emitted into the first thickener after crystallization, the freezing nitre crystallization apparatus connects cooler and passes through cold nitre circulating pump
The freezing nitre crystallization apparatus is set to be maintained at -6~-5 DEG C, the freezing nitre mother liquor enters preheater by freezing nitre mother liquor pump
It is heated, is evaporated subsequently into the salt evaporated crystallization device and under negative pressure crystallization；
The salt evaporated crystallization device connects secondary heater by circulating pump and adds to the salt evaporated crystallization device
Heat, the indirect steam that the salt evaporated crystallization device generates are extracted by second vapour compression machine and are heated through described second
The heating of the preheater internal liquid is used for after device raising temperature,
After the product after salt evaporative crystallization enters the separation of salt whizzer by the second thickener, then by crystal
Commodity sodium salt is obtained after the drying of the second drying equipment.
According to a preferred embodiment, spiral-flow type electrocoagulation dress is connected between the regulating reservoir and the highly dense pond
It sets, the Spiral-flow type electrocoagulation device includes cathode, anode, water inlet, and water outlet is reacted by what is formed between cathode and anode
Room, insulate fixing seal lid and insulated enclosure support plate, and insulation fixing seal lid is set to cathode top, is formed by cylindrical rod
Anode is fixed using the center of cathode as axis by the fixing seal lid that insulate, and insulated enclosure support plate is set to the lower part of cathode, into
The mouth of a river is set to the side shell lower end of cathode, and water outlet is set to the upper end of cathode other side shell, inlet and outlet
It is set to the shell section tangential direction of cathode in the same direction；
The brine waste that the electro-coagulation equipment makes the regulating reservoir homogeneous measure adjusting enters in secant-shaped from water inlet
Reative cell simultaneously flows in reative cell in spiral-flow type, and electrochemistry occurs under the action of the direct current that brine waste applies on the electrode
Reaction, so that flocculation occurs for brine waste impurities particle.
According to a preferred embodiment, the first electrically-driven ion film device and the second electrically-driven ion film device are equal
Including a spaced anode and a cathode, between the anode and cathode including aligned transfer it is at least one by anode membrane,
The film pair that cavity block and baffle combination are constituted, anode membrane and cavity block are that low film hinders high performance homogeneous membrane, the uniform partition board setting of fluidised form
At power supply is that positive-negative polarity automatically switches high-frequency direct-current power supply, and module utilizes Digital Program Control electricity between anode membrane and cavity block
It is broken using the adjustable clearance high frequency oscillation output high frequency current hogging of falling polarity DC in the polarization layer of film surface easily formed in source
Calcium and magnesium cation under high concentration multiple in the polarization layer that ring is formed due to film surface, destroys crystallization process and causes its molecule discrimination
Change, play physical scale inhibition, optimizes hydrodynamic condition, effectively reduce the 30-50% of power consumption,
Pretreatment unit discharge saline solns enter in the compartment of depth concentration electrically-driven ion film device, electrically-driven ion
Film causes to flow through under the action of applying direct current electric field the anions and canons directed movement in the saline solns of compartment, anion to
Anode direction moves, and cation is moved to cathode direction, to make in the Ion transfer to concentrated water compartment in fresh water compartment solution,
The ion in saline solns is set to be detached from saline solns, the concentrated water to be concentrated and desalination fresh water.
According to a preferred embodiment, the electrically-driven ion film device is at least by membrane stack, locking frame, into material frame, the moon
Ionic membrane, cationic membrane, partition board, cloth sink, filter, electrode and pole room, press composition, the membrane stack is by least one by sun
For the film that film, cavity block and baffle combination are constituted to being alternately arranged composition, the anionic membrane, cationic membrane and partition board composition are dense
The fixation cation exchange groups of contracting room and/or desalting chamber, the cation-exchange membrane with selective penetrated property are negatively charged to allow water
It is middle cation by and stop anion；The fixation cation exchange groups of anion-exchange membrane with selective penetrated property are positively charged,
To allow in water anion by and stop cation, cause in the Ion transfer to concentrated water compartment in fresh water compartment, institute
The thickness of partition board is stated in 0.5-2.0mm.
According to a preferred embodiment, the cycle pretreatment unit include regulating reservoir, highly dense pond, tubular type microstrainer,
At least one intermediate pool and sludge-tank,
The regulating reservoir is connect by elevator pump with the highly dense pond for being connected at least one chemicals dosing plant so that uniformly
Brine waste carries out coagulation, softening precipitation after being reacted with drug, the highly dense pond passes through the first booster pump and the tubular type micro-filtration
Device connection with will treated production water dispatch to first intermediate pool, and the highly dense pond connect with the sludge-tank with
The sludge of precipitation is carried out dehydrating, the sludge-tank connect with the regulating reservoir with by the production water dispatch after dehydration extremely
The regulating reservoir carries out cycle pretreatment；
The cycle pretreatment unit further includes candle filter, and the candle filter is connected to the tubular type microstrainer
Between first intermediate pool, the sludge-tank is connected with the sludge dehydrating and drying for carrying out dehydration and drying to sludge and fills
It sets；
The cycle minimizing unit includes at least one intermediate pool, at least one electrically-driven ion film device, middle pressure
Reverse osmosis unit, high pressure reverse osmosis unit, active carbon filter, the second tubular type microstrainer, second level reverse osmosis apparatus and/or fresh water
Water tank,
First intermediate pool is connect by middle pressure reverse osmosis unit with the high pressure reverse osmosis unit, and the high pressure is anti-
By treated, production water removes hard reactor and activated carbon filtering to permeability apparatus by reverse osmosis concentrated pond dispatch to connected to it
Device and tubular type micro-filtration filter, the active carbon filter pass through the second tubular type micro-filtration filter and the first electrically-driven ion
Film device connects, and the first electrically-driven ion film device is connect with the second electrically-driven ion film device so as to produce water by cycle
Dispatch is to the second strong brine case after desalination, the first electrically-driven ion film device and the second strong brine case and the two level reverse osmosis
Saturating device connects jointly, and the second level reverse osmosis apparatus is connect with first intermediate pool and the fresh water tanks；
The zero-emission unit includes feedstock preheater, nitre evaporated crystallization device, nitre thickener, nitre circulating pump, steams
Vapour compressor, at least one drying equipment, cooling water system, salt evaporated crystallization device,
The second strong brine case is connect by the 5th booster pump with the feedstock preheater, and the feedstock is pre-
Hot device passes sequentially through the nitre evaporated crystallization device, the nitre thickener, whizzer, nitre mother liquor tank, nitre mother liquor pump with it is cold
Freeze the connection of nitre crystallizing tank, the freezing nitre crystallizing tank passes sequentially through the first thickener, freezing nitre whizzer, freezing nitre mother liquor
Slot, freezing nitre mother liquor pump, preheater connect with the salt evaporated crystallization device, the salt evaporated crystallization device respectively with cycle
Pump, secondary heater and the second thickener connection, the secondary heater respectively with the second vapour compression machine and initial steam device
Connection, second thickener passes sequentially through salt whizzer, the second drying equipment is connect with the second metering packing device, institute
It states nitre evaporated crystallization device to be separately connected with vacuum system, nitre circulating pump, primary heater and the first vapour compression machine respectively, institute
It states primary heater to be separately connected with the nitre circulating pump, the initial steam device and the first vapour compression machine, described first steams
Vapour compressor passes sequentially through cooling water system and refrigeration station is connect with cooler, the cooler and the freezing nitre crystallizing tank it
Between connect cold nitre circulating pump；
The first drying equipment, the freezing nitre centrifugation are connected between the whizzer and the first metering packing device
Separator is connect with the nitre thickener, and the preheater is connect with secondary heater and reclamation set respectively, the nitre evaporation
Crystallization apparatus connect antifoaming agent dosing system jointly with the salt evaporated crystallization device；
First intermediate pool passes sequentially through in the filter device connection being made of booster pump, cartridge filter and presses reverse osmosis
Saturating device, the filter device and institute that middle pressure reverse osmosis unit is formed by the second intermediate pool and by booster pump, cartridge filter
The connection of high pressure reverse osmosis unit is stated, by the between the first electrically-driven ion film device and the second electrically-driven ion film device
One strong brine case and the connection of the 4th booster pump.
The advantageous effects of the present invention：
Present invention process have technology maturation, construction investment is low, operating cost is low, operational administrative is simple, system operation is steady
The features such as fixed reliable, small accommodation area.It recycles product water and condensed water water quality is excellent, can be used for circulating water system or desalted water
Supplement of standing water.96% or more the simple substance salt sodium sulphate of separation, 98% or more sodium chloride, final mixed salt account for 5% or less total salt amount.Production
Water all recycles, and non-wastewater discharge reaches wastewater zero discharge.
Description of the drawings
Fig. 1 is the technological process rough schematic view of the present invention；
Fig. 2 is the process flow diagram of the present invention；
Fig. 3 is the structural schematic diagram of the Spiral-flow type electrocoagulation device of the present invention；With
Fig. 4 is the overlooking structure diagram of the Spiral-flow type electrocoagulation device of the present invention.
Reference numerals list
1：Brine waste 2：Regulating reservoir 3：Elevator pump
4：Highly dense pond 5：First booster pump 6：Tubular type microstrainer
7：Candle filter 8：First intermediate pool 9：Second booster pump
10：First cartridge filter 11：Middle pressure reverse osmosis unit 12：Second intermediate pool
13：Third booster pump 14：Second cartridge filter 15：High pressure reverse osmosis unit
16：Reverse osmosis concentrated pond 17：Booster water pump 18：Active carbon filter
19：Second tubular type microstrainer 20：Intermediate water tank 21：Booster water pump
22：Third cartridge filter 23：First electrically-driven ion film device 24.：First strong brine case
25：4th booster pump 26：Second electrically-driven ion film device 27：Second strong brine case
28：5th booster pump 29：Feedstock preheater 30：Nitre evaporated crystallization device
31：Primary heater 32：Initial steam device 33：Nitre circulating pump
34：Vacuum system 35：First vapour compression machine 36：Nitre thickener
37：Whizzer 38：First drying equipment 39：Nitre mother liquor tank
40：First metering packing device 41：Nitre mother liquor pump 42：Freeze nitre crystallizing tank
43：Cooling water system 44：Refrigeration station 45：Cooler
46：Freeze nitre circulating pump 47：First thickener 48：Freeze nitre whizzer
49：Freeze nitre mother liquor tank 50：Freeze nitre mother liquor pump 51：Preheater
52：Salt evaporated crystallization device 53：Circulating pump 54：Secondary heater
55：Second vapour compression machine 56：Second thickener 57：Salt whizzer
58：Second drying equipment 59：Second metering packing device 60：Sludge-tank
61：Sludge dehydrating and drying device 62：Second level reverse osmosis apparatus 63：Fresh water tanks
64：Reclamation set 65：First chemicals dosing plant 66：Second chemicals dosing plant
67：Antifoaming agent dosing system
Specific implementation mode
It is described in detail below in conjunction with the accompanying drawings.
The present invention high slat-containing wastewater refer to refinery(waste) water, coal chemical industrial waste water, circulatory system sewerage, reverse osmosis concentrated water with
And the waste water etc. containing complicated ingredient in sewage treatment plant.The TDS of the high slat-containing wastewater of the present invention is 5000~10000mg/L.
Total dissolved solid content i.e. in 1L high slat-containing wastewaters is 5000~10000mg.
Fig. 1 is the technological process rough schematic view of the present invention.As shown in Figure 1, the present invention provides a kind of high slat-containing wastewater
Zero-discharge treatment system, including cycle pretreatment unit, cycle minimizing unit and zero-emission unit.Pretreatment unit is recycled to use
Dispatch extremely cycle minimizing list after production water after reacting effluent brine with drug coagulation, softening is filtered by tubular type microstrainer
Member.The production water that cycle minimizing unit is used to recycle pretreatment unit processing passes through cartridge filter and at least one electric drive
Ion-exchange membrane facility carries out depth minus quantification treatment so that obtained condensed water dispatch is dense to fresh water tanks reuse, and by what is obtained
Contracting mixes saline solution dispatch to zero-emission unit.Zero-emission unit for will concentrate mix saline solution circulating-heating, evaporation, crystallization obtain
It is capable of the nitre and commodity salt of packing and selling.
As shown in Fig. 2, cycle pretreatment unit includes regulating reservoir 2, highly dense pond 4, tubular type microstrainer 6, at least one centre
Pond and sludge-tank 60.Regulating reservoir 2 is connect by elevator pump 3 with the highly dense pond 4 for being connected at least one chemicals dosing plant so that
Even brine waste carries out coagulation, softening precipitation after being reacted with drug.Highly dense pond 4 is connected by the first booster pump 5 with tubular type microstrainer 6
Connect with will treated production water dispatch to the first intermediate pool 8.And highly dense pond 4 connect the sludge will precipitate with sludge-tank 60
It is carried out dehydrating.Sludge-tank 60 connect pre- recycle the production water dispatch after dehydration to regulating reservoir 2 with regulating reservoir 2
Processing.
According to a preferred embodiment, cycle pretreatment unit further includes candle filter 7, and candle filter 7 connects
Between tubular type microstrainer 6 and the first intermediate pool 8.
According to a preferred embodiment, it is dry that sludge-tank 60 is connected with the sludge dewatering for carrying out dehydration and drying to sludge
Makeup sets 61.
Recycling pretreatment unit uses chemical method by hardness ions such as heavy metal ion, calcium and magnesiums reverse osmosis into concentrated water
It is effectively removed before, while removing most COD, silicon ion, organic colloidal matter.Pass through coagulation, the effect of absorption
Reduce COD, silicon ion concentration, keep it is reverse osmosis into water ph value 8.0~9.5.So that treated brine is in alkaline item
The tendency of the fouling of film surface silicon and organic contamination is inhibited under part, to counter-infiltration system reverse osmosis membrane surface avoid it is organic
Object pollutes and problem is blocked up in the dirt of calcium and magnesium fouling.Wherein, the tubular type microstrainer for being 1~5 micron by aperture generates chemical reaction
The further removal such as sediment, coagulation colloidal substance, so that pretreatment is reached the SDI indexs for meeting follow-up feed water by reverse osmosis, drop
It is low stifled to the dirt of the organic pollution, inorganic matter of follow-up reverse osmosis generation, make whole system processing waster water process more they tend to close
Reason ensure that system is long-term, stablizes, reliability service.
According to a preferred embodiment, cycle minimizing unit includes at least one booster pump, at least one ensured public security
Filter, at least one intermediate pool, at least one electrically-driven ion film device, high pressure reverse osmosis unit 15, active carbon filter
18, the second tubular type microstrainer 19, second level reverse osmosis apparatus 62 and/or fresh water tanks 63,
First intermediate pool 8 will be filtered by least one filter device being made of booster pump, cartridge filter
Water dispatch is produced to high pressure reverse osmosis unit 15, production water passes through 16 row of reverse osmosis concentrated pond to high pressure reverse osmosis unit 15 by treated
Send to active carbon filter 18 connected to it, active carbon filter 18 by the second tubular type microstrainer 19 and the first electric drive from
Sub- film device 23 connects, and the first electrically-driven ion film device 23 is connect with the second electrically-driven ion film device 26 so as to produce water process
Dispatch is anti-to the second strong brine case 27, the first electrically-driven ion film device 23 and the second strong brine case 27 and two level after recycling desalination
Permeability apparatus 62 connects jointly, and second level reverse osmosis apparatus 62 is connect with the first intermediate pool 8 and fresh water tanks 63.
According to a preferred embodiment, the first intermediate pool 8 passes sequentially through the mistake being made of booster pump, cartridge filter
It filters and presses reverse osmosis unit 11 in device connection, middle pressure reverse osmosis unit 11 is by the second intermediate pool 12 and by booster pump, security personnel
The filter device of filter composition is connect with high pressure reverse osmosis unit 15, the first electrically-driven ion film device 23 and the second electric drive
It is connected by the first strong brine case 24 and the 4th booster pump 25 between ion-exchange membrane facility 26.
Saliferous complexity waste water that the present invention is directed to is generally from the reverse osmosis concentrated water of 4 times of concentration or other high salinitys
Produce waste water.Its salt content TDS is typically in the range of 5000~10000mg/L, passes through middle pressure reverse osmosis unit and the reverse osmosis dress of high pressure
It sets and carries out preliminary minimizing processing concentrate and reach TDS about 50000mg/l present apparatus system can the system rate of recovery being reached 85%
Left and right.
First electrically-driven ion film device 23 is the with high salt of 50000mg/l to TDS with the second electrically-driven ion film device 26
Water is further concentrated.TDS is increased to 120000mg/l by the first electrically-driven ion film device 23.Second electrically-driven ion film
TDS is increased to 200000mg/l by device 26.Electrically-driven ion film device replaces the steaming of conventional multiple effect evaporation reduction low concentration
Evaporated water is greatly lowered in shampoo amount, saves energy consumption.Entire technological process minimizing reaches 95% or more water of recycling, TDS
The dense saline solution of about 200000mg/l is as evaporative crystallization unit raw material water.According to a preferred embodiment, zero-emission unit
Including feedstock preheater 29, nitre evaporated crystallization device 30, nitre thickener 36, nitre circulating pump 33, vapour compression machine 35, at least
One drying equipment, cooling water system 43, salt evaporated crystallization device 52,
Second strong brine case 27 is connect by the 5th booster pump 28 with feedstock preheater 29, feedstock preheater 29
Pass sequentially through nitre evaporated crystallization device 30, nitre thickener 36, whizzer 37, nitre mother liquor tank 39, nitre mother liquor pump 41 and freezing
Nitre crystallizing tank 42 connects,
Freezing nitre crystallizing tank 42 pass sequentially through the first thickener 47, freezing nitre whizzer 48, freezing nitre mother liquor tank 49,
Freezing nitre mother liquor pump 50, preheater 51 are connect with salt evaporated crystallization device 52,
Salt evaporated crystallization device 52 is connect with circulating pump 53, secondary heater 54 and the second thickener 56 respectively, and second adds
Hot device 54 is connect with the second vapour compression machine 55 and initial steam device 32 respectively, and the second thickener 56 passes sequentially through salt centrifugation
Device 57, the second drying equipment 58 are connect with the second metering packing device 59.
According to a preferred embodiment, nitre evaporated crystallization device 30 respectively with vacuum system 34, nitre circulating pump 33, first
Heater 31 and the first vapour compression machine 35 are separately connected, primary heater 31 and nitre circulating pump 33, initial steam device 32 and the
One vapour compression machine 35 is separately connected, and the first vapour compression machine 35 passes sequentially through cooling water system 43 and refrigeration station 44 and cooler
45 connections connect cold nitre circulating pump 46 between cooler 45 and freezing nitre crystallizing tank 42.
According to a preferred embodiment, the first baking is connected between whizzer 37 and the first metering packing device 40
Dry equipment 38, freezing nitre whizzer 48 are connect with nitre thickener 36.
According to a preferred embodiment, preheater 51 is connect with secondary heater 54 and reclamation set 64 respectively, and nitre steams
Hair crystallization apparatus 30 connect antifoaming agent dosing system 67 jointly with salt evaporated crystallization device.
By the two-stage minimizing process of the first electrically-driven ion film device and the second electrically-driven ion film device, formation
High concentration saline solution enters the preheater of evaporative crystallization, nitre crystallizes Guan County, by cycling through heater heating.In negative pressure state
Under, preliminary heat saline solution is provided to boiling using raw steam, is delayed the low temperature secondary dead steam generated using evaporation and is passed through steaming
Vapour compressor carries out the temperature that compression improves steam exhaust, and realization is continuously nitre tank saline solution evaporation thermal energy.Utilize salt-water system Na +//
Cl-, SO4 2--H2O phasors carry out nitre and sodium chloride according to liquid phase composition/% of the sodium sulphate and sodium chloride of 100 degree of temperature solutions
Crystallization Separation.Moreover, according to nitre mother liquor at a temperature of 75 degree or so solution remaining meltage, according to phasor carry out cryogenic freezing
Mode is further separated out ten water nitre.Melt analysis heat is carried out in the feed liquid to be separated that ten water nitre back dissolvings to crystallizing tank exclude jointly
Go out nitre, is finally reached and sub-prime separation is carried out to nitre and sodium chloride.
Embodiment one
Process flow diagram as shown in Figure 2 handles complicated ingredient industry brine waste, waste water using this integrated technique
It is anti-from the draining of Industrial Waste Water Treatments reuse water, water in water circulating system with water, production technology draining and Desultwater Station and two level
Permeate concentrated water and backwash water etc..
First, the waste water 1 that each road is sent is carried out by homogeneous by regulating reservoir 2 and measures adjusting.Raw water is sent by elevator pump 3
To highly dense pond 4.Herein the first chemicals dosing plant 65 and the second chemicals dosing plant 66 sequentially add lime or sodium hydroxide, sodium carbonate,
PAC、PAM.Sodium hydroxide is configured to the solution of 20% concentration, and dosage 1.5g/L is configured to 15% concentration sodium carbonate liquor.
The influent density that dosage is 3g/L carries out water demineralization.PAC is made into the molten of 20% concentration according to the concentration dosage of 30mg/L
Liquid.The solution that PAM is made into 0.3% concentration according to the amount of 3mg/L is added.Feelings need to be changed according to the practical each ion concentration of water inlet of water quality
Condition is adjusted dosage, otherwise easily causes fouling membrane, influences the service life of film.
Mixing liquid enters tubular type microstrainer 6 or immersed microfiltration pond 6.Filter tank total hrt is 2.5h.Certainly
Under right settlement action, supernatant enters back into candle filter 7 by tubular type microstrainer 6 or bag filters out water into the first intermediate pool 8.
Chemical sludge is discharged into sludge-tank 60 by gravitational settling from bottom, and device for dehydrating sladge waste is entered after sludge adjusts and carries out muddy water
Separation.Become the dewatered sludge after mud cake after sludge dewatering finally to carry out at sludge dehydrating and drying in sludge dehydrating and drying device 61
It sets.Middle pressure reverse osmosis unit 11 uses membrane material for aromatic polyamide composite material, and operating pressure is 2.0~3.5MPa, is returned
Yield is more than 70%, can retain 97.5% salts substances, can the raw water that average TDS is 6500mg/L be concentrated to TDS and is more than
21600mg/L.The concentrated water for accounting for total treating capacity 30% is entered high pressure reverse osmosis unit 15 after the processing of middle pressure reverse osmosis unit 11
Carry out further desalination and concentration.15 membrane material of high pressure reverse osmosis unit is aromatic polyamide composite material, operating pressure 3.5
~4.5MPa, the rate of recovery are more than 65%, can retain 97.2% or more salts substances, can be the original of 21600mg/L by average TDS
Water is concentrated to TDS and is more than 50000mg/L concentrated waters.Concentrated water after the concentration of high pressure reverse osmosis unit 15 is via active carbon filter
18 and second tubular type microstrainer 19 filter after enter the first electrically-driven ion film device 23 and carry out cycle desalination and concentration.First electricity
Driving 23 pressure of supply water of ion-exchange membrane facility is 0.20MPa, and the rate of recovery is more than 55%, can retain 96.2% or more salts substances,
The raw water that average TDS is 50000mg/L can be concentrated to TDS more than 200000mg/L or so.Account for the concentrate of total treating capacity 4%
Into follow-up micro- evaporative crystallization unit.The desalination fresh water of first electrically-driven ion film device 23 production enters two-pass reverse osmosis inlet tank
Both 62 further desalination of second level reverse osmosis apparatus.The reverse osmosis concentrated water of second level reverse osmosis apparatus 62 is returned by the first intermediate pool 8
Middle 11 inlet tank of pressure reverse osmosis unit.By the fresh water dispatch of 62 desalination of second level reverse osmosis apparatus generation to fresh water tanks 63, and
Dispatch is to reclamation set 64 to carry out fully recovering.
Raw water passes through cycle pretreatment unit and recycles the preliminary minimizing of reverse osmosis concentration of minimizing unit, generation
Compared with high-salt concentrated water heat exchange is carried out by raw material material reducing preheater 29 and high-temperature condensation water.Enter nitre after heat exchanger heating to steam
Crystallization apparatus 30 is sent out, circulating-heating is carried out to feed liquid and primary heater 31 using nitre circulating pump 33.MVR devices first lead to when starting
Enter raw steam, after feed liquid boiling, compresses temperature raising using the secondary dead steam that the first vapour compression machine 35 generates evaporator, substitute
Raw steam carries out circulating-heating to feed liquid.Compressed secondary high-temperature steam becomes high-temperature condensation water after heat exchanger exchanges heat.
Condensed water, which enters after the heat exchange of preheater 51 and feed liquid, to be condensed into low temperature cold condensate and is sent to reclamation set 64, reuse production technology.Root
According to salt-water system Na+//Cl-, SO4 2--H2Key component content in O phasors makes to reach oversaturated nitre from evaporated crystallization device 30
Discharge, into nitre thickener 36.The ten water nitre mixing that nitre is detached with follow-up freezing nitre is heated, and is centrifuged device 37 and is obtained
Simple substance salt.Simple substance salt is dried using the first drying equipment 38.Simple substance salt after drying is packed by the first metering packing device 40
Export trade.
Nitre is detached into mother liquor from being pumped in nitre mother liquor tank 39 to freezing in nitre crystallizing tank 42 by nitre mother liquor pump 41.Nitre mother liquor is cold
Jelly reaches -5 degree, isolated ten water nitre.Ten water nitre return to nitre thickener 36 and melt with nitre liquid progress heat, and temperature reduces and liquid containing nitre
Common separation nitre.
The mother liquor that freezing nitre generates is tied by the salt evaporation that is conveyed into of freezing nitre mother liquor tank 49 and freezing nitre mother liquor pump 50
Brilliant device 52.- salt concentrated water carries out heat exchange by 51 and high-temperature condensation water water, enters salt evaporative crystallization after heat exchanger heating
Device 52.Circulating-heating is carried out to saliferous feed liquid and secondary heater 54 using circulating pump 53.MVR devices are first passed through when starting
Raw steam after the secondary dead steam compression temperature raising that evaporator is generated using the second vapour compression machine 55, is substituted after feed liquid boiling
Raw steam carries out circulating-heating to feed liquid, compressed secondary high-temperature steam become after heat exchanger exchanges heat high-temperature condensation water into
Enter preheater 51.High-temperature condensation water is condensed into low temperature cold condensate and is sent to reclamation set 64, reuse produces work with after the heat exchange of salt feed liquid
Skill.According to salt-water system Na+//Cl-, SO4 2--H2Key component content in O phasors makes to reach oversaturated salt from salt evaporation knot
Brilliant device 52 is discharged, into the second thickener 56.Salt is through 57 isolated salt of salt whizzer.Salt passes through the second drying equipment
After 58 are dried to drying, export trade is packed by the second metering packing device 59.Antifoaming agent dosing system 67 is to nitre evaporated crystallization device
30 and salt evaporated crystallization device 52 add antifoaming agent.The finally formed a small amount of mixed salt of the present invention is through flashing to salt slurry.Salt slurry is dehydrated
Storage bay reason is carried out afterwards.
The water inlet index of the brine waste of the present invention and the salt index of processing procedure are as shown in table 1.
The simple substance salt sodium sulphate that the present invention detaches reaches 96% or more, and sodium chloride reaches 98% or more, and final mixed salt accounts for always
5% or less salt amount.Wherein, production water all recycles, and non-wastewater discharge reaches wastewater zero discharge.Condensation in processing procedure
Water water quality is excellent, can be used for circulating water system or Desultwater Station supplement water.Therefore, the present invention realizes in addition to recycling high-quality water
A variety of simple substance salt are recycled, the quantity of final mixed salt is greatly reduced, save a large amount of solidification disposal of waste expenses.The commodity salt of generation is sold
The processing cost for processing procedure of effectively examining and making cuts afterwards,.Realize low cost, the treatment process of zero-emission.
Embodiment two
The present embodiment is the improvement embodiment of embodiment one, is a kind of preferred embodiment of the present invention.The present embodiment is only
Pair components of system as directed different from embodiment one illustrates, and identical components of system as directed repeats no more.
It is connected with electro-coagulation equipment between regulating reservoir 2 and highly dense pond 4.Electro-coagulation equipment, by cylindrical acrylic resin
Shell and metal electrode composition.Using the medium carbon steel electrode that 6 sizes are 110mm × 90mm × 2mm as anode, and use 6
A size is stainless steel (SS 316) electrode of 110mm × 90mm × 1mm as cathode in electro-coagulation equipment.By the anode and
Cathode electrode is assembled with alternating sequence, wherein retaining the gaps 6mm between the electrodes.Applied for electro-coagulation equipment using DC power supply
DC electric current.DC electric current changes between 1.5 amperes to 3.5 amperes, and the residence time is 30 minutes.Brine waste forms two kinds of dirts
Mud is removed including the light weight sludge of organic impurities is swum on the water surface by skimming method.Including the heavy of inorganic impurity is dirty
Mud is removed by adding polyelectrolyte.Using 1ppm AT-7594 (WEXTECH) as polyelectrolyte with the inorganic dirt of rapid subsidence
Mud.
According to a preferred embodiment, electro-coagulation equipment is Spiral-flow type electrocoagulation device.As shown in figure 3, spiral-flow type is electric
Coacervation device 700 includes cathode 702, anode 703, water inlet 701, water outlet 705 and reative cell, insulation fixing seal lid 704
With insulated enclosure support plate 706.Wherein cathode 702 is rounding frustum stainless steel cathode shell.Anode 703 is cylindrical rod anode.Sun
Pole 703 is aluminium bar or iron staff.Insulation fixing seal lid 704 is set to 702 top of cathode.Cylindrical rod anode is in cathode 702
The heart is that axis is fixed by the fixing seal lid 704 that insulate.Insulated enclosure support plate 706 is set to the lower part of cathode 702.Water inlet
701 are set to the side shell lower end of cathode 702.Water outlet 705 is set to the upper end of 702 other side shell of cathode.Water inlet
701 and water outlet 705 be set in the same direction on cathode 703, and be set to the shell section tangential direction of cathode 703.Reative cell
The region formed between cathode 702 and cylindrical rod anode.As shown in figure 4, setting carries out by force between cathode 702 and anode 703
The insulation deflector 707 or insulation water conservancy diversion conduit of water conservancy diversion processed.Insulate deflector 707 or the water conservancy diversion conduit increase accessing pending water that insulate
Hydraulic detention time deflector 707 is set to by bonding agent on the inner wall of cathode 702.Deflector 707 is replaced by bonding agent
It is arranged on 702 inner wall of cathode and anode cylindrical rod.The deflector 707 being arranged alternately passes through bonding agent and anode cylindrical rod socket joint
Formula connects.Setting and 707 matched slot 708 of deflector on anode cylindrical rod.Deflector is PVC material insulation board.Bonding agent
For silastic material.
Pending brine waste enters from water inlet 701 in secant-shaped and reacts after regulating reservoir 2 carries out homogeneous amount processing
Room.It flows the fluid among the two poles of the earth to flow in spiral-flow type in reative cell, increases the flow hydraulic residence time.Meanwhile passing through
Apply direct current on the electrode, electrochemical reaction occurs in pending brine waste, generates Al (OH)3Or Fe (OH)3, in turn
Promote accessing pending water impurities particle that flocculation occurs.Eddy flow makes the turbulence effect of fluid aggravate, and can effectively wash away
It is deposited on the impurity of electrode surface, keeps the electrochemical reaction of electrode unaffected, ensures good flocculating effect.Finally handle water
Enter highly dense pond 4 from water outlet 705 and carries out subsequent processing.The step of subsequent processing, is identical as embodiment one.
Embodiment three
The present invention is improved embodiment on the basis of embodiment one and/or embodiment three.The present embodiment only pair with it is real
It applies the different components of system as directed of example one, embodiment two to illustrate, identical components of system as directed repeats no more.
The the first electrically-driven ion film device 23 and the second electrically-driven ion film device 26 of the present invention includes interval setting
An anode and a cathode.There is a filled chamber between anode and cathode.Filled chamber by diaphragm respectively with anode and cathode
Insulation set.The material of anode and cathode is activated carbon fibre.Diaphragm is amberplex or insulation porous septum.Filled chamber
It is the active carbon particle of 0.1~5.0mm by multiple grain sizes, carbon fiber or carbon nano-tube filled.Preferably, filled chamber is by multiple
The active carbon particle that grain size is 0.1~5.0mm is filled.
Pretreated saline solns enter in the chamber of electrically-driven ion film device, are filled in packing layer or packing layer
It immerses in saline solns.Power supply system provides DC constant voltage electric field to electrically-driven ion film device, makes zwitterion in direct current
It is adsorbed on the surfaces of two electrodes to two polar motions under field action, the ion in saline solns is made to be detached from saline solns, to
Realize desalination.In the present embodiment, intermediate filler layer thickness is 2cm, DC voltage 1.2V.Since filler surface has double electricity
Layer, charge density is higher, so that the resistance of Ion transfer reduces, accelerates the migration of ion, realizes Electro Sorb desalination
The raising of desalination speed.
First electrically-driven ion film device 23 carries out electrically-driven ion UF membrane to the moderate concentrated water of process, and that isolates is de-
Brine enters second level reverse osmosis apparatus 62.The filtrate of first electric drive film device 23 enters two level electric drive film device 26.Two level
Electric drive film device 26 carries out electrically-driven ion UF membrane again to the filtrate of process, and the desalted water isolated enters zero-emission list
Member.
According to a preferred embodiment, cycle minimizing unit of the invention is filled including at least two electrically-driven ion films
It sets.That is, in cycle minimizing unit, increase between the first electrically-driven ion film device and the second electrically-driven ion film at least one
Electrically-driven ion film device carries out depth concentration to form multistage electrically-driven ion film device, to brine waste.
According to a preferred embodiment, electrically-driven ion film device of the invention includes membrane stack, electrode assembly, ion friendship
Change film, anode chamber, cathode chamber.On the inside of anode chamber towards cathode direction be provided with cation-exchange membrane, anode protection room,
Anion-exchange membrane, the first enriched chamber of membrane stack.Towards positive extreme direction is provided with cation-exchange membrane, cathode is protected on the inside of cathode chamber
Protect room, anion-exchange membrane, membrane stack end enriched chamber.Flow is divided into two sections of level-one from import to outlet by cation-exchange membrane
Or level-one multistage.By flow from import to export direction, continuously it is arranged after the cation-exchange membrane that commutates two adjacent dense
Contracting room.It is provided with cation-exchange membrane between two adjacent enriched chambers.It is filled in first enriched chamber after flow commutation
Macropore mixed-bed resin.Macropore mixed-bed resin contains the negative resin that volume ratio is 50%~100%.The electrically-driven ion exchange membrane
Realization concentration and purifying brine waste can be synchronized.
According to a preferred embodiment, electrically-driven ion film device of the invention includes membrane stack, electrode assembly, ion friendship
Change film, positive plate, negative plate.Cathode direction is provided with cation-exchange membrane, anode protection room, anion on the inside of positive plate
Exchange membrane, the first enriched chamber of membrane stack.On the inside of cathode chamber towards positive extreme direction be provided with cation-exchange membrane, cathode protection room,
Anion-exchange membrane, membrane stack end enriched chamber.Flow is divided into two sections of level-one or one from import to outlet by cation-exchange membrane
Grade multistage.By flow from import to export direction, two adjacent enriched chambers are continuously set after the cation-exchange membrane that commutates.
It is provided with cation-exchange membrane between two adjacent enriched chambers.It is mixed filled with macropore in first enriched chamber after flow commutation
Bed resin.Macropore mixed-bed resin contains the negative resin that volume ratio is 50%~100%.The electrically-driven ion exchange membrane can be same
Step realizes concentration and purifying brine waste.
By multiple films of anode membrane, cavity block and baffle combination to regular arrangement between the anode and cathode.Anode membrane and the moon
Film is that low film hinders high performance homogeneous membrane and is effectively improved the partition board composition of flow-shape.The diaphragm is in highly concentrated brine concentration process
In, it can still keep compared with macroion dynamic exchange capacity and lower membrane surface resistance, lower water migrates through performance.Its power supply
High-frequency direct-current power supply is automatically switched using positive-negative polarity, module utilizes Digital Program Control power supply, is shaken using adjustable clearance high frequency
The output output high frequency current hogging of falling polarity DC is swung in the polarization layer of film surface easily formed, and breaks what ring was formed due to film surface
Calcium and magnesium cation under high concentration multiple in polarization layer destroys crystallization process and it is caused to generate molecule disproportionation, effectively plays resistance
Closely knit salt crust is only formed, and optimizes hydrodynamic condition, effectively reduces power consumption 30-50%.
Cycle pretreatment unit discharge saline solns enter in the compartment of depth concentration electrically-driven ion film device, electric drive
Ionic membrane causes to flow through under the action of applying direct current electric field the anions and canons directed movement in the saline solns of compartment, it is cloudy from
Son to anode direction move, cation to cathode direction move, to make the Ion transfer in fresh water compartment solution to concentrated water every
In room, the ion in saline solns is made to be detached from saline solns, the concentrated water to be concentrated and desalination fresh water.
Pending brine waste is after cycle pretreatment unit processing, and obtained brine waste is in the first electric drive
Diluting compartment and enriched chamber are respectively enterd by different flow ratio in ion-exchange membrane facility 23, is handed in the driving of DC electric field and zwitterion
It changes under the centrifugation of film under being acted on the faciliated diffusion of institute's potting resin, the heavy metal ion in diluting compartment flow and anion
Enriched chamber is migrated into, to obtain fresh water stream.Flow in enriched chamber is continuous by part cycle or closed cycle, concentration
Increase, obtains the concentrate of old metal.Fresh water is sent to fresh water recovery, and condensed water enters the second electrically-driven ion film device
It concentrates again.Finally obtained concentrate enters Zero discharging system, and salt made from earth containing a comparatively high percentage of sodium chloride and sodium salt are obtained through pervaporation, crystallization.To realize
The brine waste processing of continuous, cleaning, environmental protection is realized in the zero-emission of brine waste.
It should be noted that above-mentioned specific embodiment is exemplary, those skilled in the art can disclose in the present invention
Various solutions are found out under the inspiration of content, and these solutions also belong to disclosure of the invention range and fall into this hair
Within bright protection domain.It will be understood by those skilled in the art that description of the invention and its attached drawing are illustrative and are not
Constitute limitations on claims.Protection scope of the present invention is limited by claim and its equivalent.
Claims (10)
1. a kind of processing system of brine waste, including the cycle pretreatment unit, the cycle minimizing unit and zero that are arranged in succession
Exhaust unit, the zero-emission unit to recycle the concentration to the heating of concentration mixing saline solution, evaporation, crystallization by mixing saline solution
In salt made from earth containing a comparatively high percentage of sodium chloride and sodium salt,
It is characterized in that,
The cycle minimizing unit tentatively subtracts the production water of the cycle pretreatment unit processing by reverse osmosis unit
Quantification treatment, and the multistage electrically-driven ion film device by being made of at least one electrically-driven ion film device carries out depth
Concentration detaches the moisture in high slat-containing wastewater to fresh water tanks reuse with further minimizing, the concentration that depth is concentrated to give
Saline solution dispatch is mixed to the zero-emission unit, wherein the cycle minimizing unit including at least at least one electric drive from
Sub- film device, middle pressure reverse osmosis unit (11), high pressure reverse osmosis unit (15), active carbon filter (18), the second tubular type micro-filtration
Device (19), second level reverse osmosis apparatus (62) and fresh water tanks (63),
The high pressure reverse osmosis unit (15) will be concentrated by medium pressure reverse osmosis unit (11) in a manner of middle pressure osmosis filtration
The concentrated water that the production water of the cycle pretreatment unit discharge obtains obtains after being concentrated into horizontal high voltage osmosis filtration, to producing water
Carry out preliminary minimizing processing；
The fresh water that medium pressure reverse osmosis unit (11) and the high pressure reverse osmosis unit (15) generate is via the two level reverse osmosis
Reuse is to the fresh water tanks (63) after saturating device (62) is purified in a manner of reverse osmosis and ultraviolet-sterilization；
The active carbon filter (18) and the second tubular type microstrainer (19) is filtered successively to counter-infiltration dope and calcium
Dispatch to the multistage electrically-driven ion film device carries out depth minus quantification treatment after magnesium ion softening.
2. the processing system of brine waste as described in claim 1, which is characterized in that the cycle pretreatment unit is used for will
Production water after high slat-containing wastewater is reacted with pre-treatment medicaments passes through dispatch after the filtering of tubular type microstrainer to the cycle minimizing list
Member, wherein the cycle pretreatment unit includes at least regulating reservoir (2), highly dense pond (4), tubular type microstrainer (6) and sludge-tank
(60),
The highly dense pond (4) is produced after mixing the brine waste for measuring adjusting by the regulating reservoir (2) homogeneous and pre-treatment medicaments
Raw sludge is according to the sludge-tank (60) for draining into its underpart under gravity, after being handled by pre-treatment medicaments in the highly dense pond (4)
The production water via tubular type microstrainer (6) micro-filtration handle after enter cycle minimizing unit handled；
Wherein, the sludge in the sludge-tank (60) carries out mud-water separation by sludge dehydrating and drying device (61) in the form of press filtration
And the water of separation abjection is vented back to the regulating reservoir (2) or the highly dense pond (4) carries out cycle again and pre-processes.
3. the processing system of brine waste as claimed in claim 2, which is characterized in that the zero-emission unit includes at least original
Expect feed preheater (29), nitre evaporated crystallization device (30), nitre thickener (36), nitre circulating pump (33), the first vapour compression machine
(35), at least one drying equipment, cooling water system (43), salt evaporated crystallization device (52),
The cycle minimizing unit that the nitre evaporated crystallization device (30) will be preheated by the feedstock preheater (29)
The concentration mixing salt solution of discharge is vented back to the nitre evaporative crystallization after nitre circulating pump (33), primary heater (31) successively
Device (30) carries out circulating-heating and is concentrated and separated out salt made from earth containing a comparatively high percentage of sodium chloride and feed liquid with evaporative crystallization,
The salt made from earth containing a comparatively high percentage of sodium chloride that the feed liquid will be centrifuged out by the nitre thickener (36) into whizzer (37) is through first
It is packaged as commodity salt made from earth containing a comparatively high percentage of sodium chloride after drying equipment (38) drying,
The freezing of nitre mother liquor that the whizzer (37) is isolated up to enter after -5 degree freezing nitre crystallization apparatus (42) and by
Isolated ten water nitre is recycled to the feedstock preheater (29) and carries out following for salt made from earth containing a comparatively high percentage of sodium chloride by freezing nitre whizzer (48)
Ring Crystallization Separation,
It is described freezing nitre whizzer (48) detach supersaturated feed liquid dispatch to the salt evaporated crystallization device (52) with from
The isolated commodity salt of the heart.
4. the processing system of brine waste as claimed in claim 3, which is characterized in that the nitre evaporated crystallization device (30) exists
The low temperature secondary dead steam compression for being generated evaporation by the first vapour compression machine (35) under negative pressure or slight positive pressure state is weary to improve
Stripping temperature, so that the nitre circulating pump (33), primary heater (31) and the nitre evaporated crystallization device (30) were formed
There is circulating heater continual and steady thermal energy, the nitre evaporated crystallization device (30) to be existed using the first vapour compression machine (35)
Reference freezing nitre crystallization required temperature is connected by first vapour compression machine (35) under conditions of extracting and compressing indirect steam
It connects cooling water system (43) and keeps the freezing nitre crystallization apparatus (42) internal using cooler (45) and/or refrigeration station (44)
Required temperature.
5. the processing system of brine waste as claimed in claim 4, which is characterized in that the whizzer (37) is isolated
Nitre mother liquor enter nitre mother liquor tank (39), and carry out cooling knot into the freezing nitre crystallization apparatus (42) through nitre mother liquor pump (41)
Crystalline substance, the nitre mother liquor are adjusted after being emitted into the first thickener (47) after being crystallized in the freezing nitre crystallization apparatus (42)
Whole, freezing nitre crystallization apparatus (42) the connection cooler (45) simultaneously makes the freezing nitre crystallization dress by cold nitre circulating pump (46)
It sets (42) and is maintained at -6~-5 DEG C, freezing nitre mother liquor is heated by freezing nitre mother liquor pump (50) into preheater (51),
It is evaporated subsequently into the salt evaporated crystallization device (52) and under negative pressure crystallization；
The salt evaporated crystallization device (52) connects secondary heater (54) by circulating pump (53) and is filled to the salt evaporative crystallization
It sets (52) to be heated, the indirect steam that the salt evaporated crystallization device (52) generates passes through second vapour compression machine (55)
The heating of the preheater (51) internal liquid is extracted and is used for after the secondary heater (54) improves temperature,
After product after salt evaporative crystallization enters salt whizzer (57) separation by the second thickener (56), then by crystal
Commodity sodium salt is obtained after the second drying equipment (58) drying.
6. the processing system of the brine waste as described in one of claim 1 to 5, which is characterized in that the regulating reservoir (2) and institute
It states and is connected with Spiral-flow type electrocoagulation device (700) between highly dense pond (4), the Spiral-flow type electrocoagulation device (700) includes cathode
(702), anode (703), water inlet (701), water outlet (705), the reative cell formed between anode by cathode (702), absolutely
Edge fixing seal lid (704) and insulated enclosure support plate (706), insulation fixing seal lid (704) are set on cathode (702)
Portion, the anode formed by cylindrical rod is fixed by the fixing seal lid (704) that insulate by axis of the center of cathode (702), and insulation is close
Envelope support plate (706) is set to the lower part of cathode (702), and water inlet (701) is set to the side shell lower end of cathode (702),
Water outlet (705) is set to the upper end of cathode (702) other side shell, and water inlet (701) and water outlet (705) are set in the same direction
The shell section tangential direction of cathode (702)；
The electro-coagulation equipment (700) makes the regulating reservoir homogeneous measure the brine waste of adjusting in secant-shaped from water inlet
(701) enter reative cell and flowed in spiral-flow type in reative cell, under the action of the direct current that brine waste applies on the electrode
Electrochemical reaction occurs, so that flocculation occurs for brine waste impurities particle.
7. the processing system of the brine waste as described in one of claim 1 to 6, which is characterized in that
The multistage electrically-driven ion film device includes that the first electrically-driven ion film device (23) and the second electrically-driven ion film fill
It sets (26), the second electrically-driven ion film device (26) is by the first electrically-driven ion film device (23) thickening filtration
TDS is 1.2 × 105The concentrated water of mg/l carries out secondary concentration and TDS is obtained by filtration to be 2 × 105The concentration mixing salt solution of mg/l, institute
It states the isolated desalted water of the second electrically-driven ion film device (26) and is vented back to medium pressure reverse osmosis unit (11) to carry out
The cycle minimizing processing of primary minimizing and depth concentration.
8. the processing system of the brine waste as described in one of claim 1 to 7, which is characterized in that the cycle pretreatment is single
Member includes regulating reservoir, highly dense pond, tubular type microstrainer, at least one intermediate pool and sludge-tank, wherein the regulating reservoir is by carrying
Pump is risen to be connect with the highly dense pond for being connected at least one chemicals dosing plant so that uniformly brine waste carries out after reacting with drug
Coagulation, softening precipitation, the highly dense pond connect with the tubular type microstrainer by the first booster pump with incite somebody to action treated produce water arrange
It send to first intermediate pool, and the highly dense pond is connect with the sludge-tank to carry out the sludge of precipitation at dehydration
Reason, the sludge-tank are connect with the regulating reservoir to carry out the production water dispatch after dehydration to the regulating reservoir to recycle pre- place
Reason.
9. the processing system of brine waste as claimed in claim 7, which is characterized in that
The first electrically-driven ion film device (23) and the second electrically-driven ion film device (26) include spaced one
Anode and a cathode include at least one by anode membrane, cavity block and baffle combination structure of aligned transfer between the anode and cathode
At film pair, anode membrane and cavity block are that low film hinders high performance homogeneous membrane, and the uniform partition board of fluidised form is arranged between anode membrane and cavity block,
Power supply is that positive-negative polarity automatically switches high-frequency direct-current power supply, and module utilizes Digital Program Control power supply, using adjustable clearance high frequency
The concussion output high frequency current hogging of falling polarity DC destroys the pole formed due to film surface in the polarization layer of film surface easily formed
Change the calcium and magnesium cation under the high concentration multiple in layer.
10. the processing system of the brine waste as described in one of claim 1 to 9, which is characterized in that the cycle pretreatment is single
Member further includes candle filter, and the candle filter is connected between the tubular type microstrainer and first intermediate pool,
The sludge-tank is connected with the sludge dehydrating and drying device for carrying out dehydration and drying to sludge, wherein
First intermediate pool is connect by middle pressure reverse osmosis unit with the high pressure reverse osmosis unit, and the high pressure is reverse osmosis
Device will treated production water by reverse osmosis concentrated pond dispatch to it is connected to it except hard reactor and active carbon filter and
Tubular type micro-filtration filter, the active carbon filter are filled by the second tubular type micro-filtration filter and the first electrically-driven ion film
Connection is set, the first electrically-driven ion film device is connect with the second electrically-driven ion film device so as to produce water by cycle desalination
Dispatch to the second strong brine case, the first electrically-driven ion film device and the second strong brine case and the two-pass reverse osmosis fills afterwards
Common connection is set, the second level reverse osmosis apparatus is connect with first intermediate pool and the fresh water tanks；
The zero-emission unit includes feedstock preheater, nitre evaporated crystallization device, nitre thickener, nitre circulating pump, vapour pressure
Contracting machine, at least one drying equipment, cooling water system, salt evaporated crystallization device,
The second strong brine case is connect by the 5th booster pump with the feedstock preheater, the feedstock preheater
Pass sequentially through the nitre evaporated crystallization device, the nitre thickener, whizzer, nitre mother liquor tank, nitre mother liquor pump and freezing nitre
Crystallization apparatus connects, and the freezing nitre crystallization apparatus passes sequentially through the first thickener, freezing nitre whizzer, freezing nitre mother liquor
Slot, freezing nitre mother liquor pump, preheater connect with the salt evaporated crystallization device, the salt evaporated crystallization device respectively with cycle
Pump, secondary heater and the second thickener connection, the secondary heater respectively with the second vapour compression machine and initial steam device
Connection, second thickener passes sequentially through salt whizzer, the second drying equipment is connect with the second metering packing device, institute
It states nitre evaporated crystallization device to be separately connected with vacuum system, nitre circulating pump, primary heater and the first vapour compression machine respectively, institute
It states primary heater to be separately connected with the nitre circulating pump, the initial steam device and the first vapour compression machine, described first steams
Vapour compressor passes sequentially through cooling water system and refrigeration station is connect with cooler, the cooler and the freezing nitre crystallization apparatus
Between connect cold nitre circulating pump；
The first drying equipment is connected between the whizzer and the first metering packing device, the freezing nitre centrifuges
Device is connect with the nitre thickener, and the preheater is connect with secondary heater and reclamation set respectively, the nitre evaporative crystallization
Device connect antifoaming agent dosing system jointly with the salt evaporated crystallization device；
First intermediate pool passes sequentially through in the filter device connection being made of booster pump, cartridge filter and presses reverse osmosis dress
It sets, the filter device and the height that middle pressure reverse osmosis unit is formed by the second intermediate pool and by booster pump, cartridge filter
Reverse osmosis unit connection is pressed, it is dense by first between the first electrically-driven ion film device and the second electrically-driven ion film device
Brine tank and the connection of the 4th booster pump.
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| CN201810004576.3A CN108558099B (en) | 2015-12-23 | 2015-12-23 | High zero release processing system who contains salt waste water |
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| CN201810004576.3A CN108558099B (en) | 2015-12-23 | 2015-12-23 | High zero release processing system who contains salt waste water |
| CN201510981321.9A CN105540972B (en) | 2015-12-23 | 2015-12-23 | A kind of zero-discharge treatment system of high slat-containing wastewater |
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| CN201510981321.9A Active CN105540972B (en) | 2015-12-23 | 2015-12-23 | A kind of zero-discharge treatment system of high slat-containing wastewater |
| CN201810004576.3A Active CN108558099B (en) | 2015-12-23 | 2015-12-23 | High zero release processing system who contains salt waste water |
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| WO2020077917A1 (en) * | 2018-10-17 | 2020-04-23 | Bgt Group Co., Ltd | A multi-stage zero-emission treatment device for treating high-salt-content waste water |
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| CN105836954A (en) * | 2016-05-30 | 2016-08-10 | 北京沃特尔水技术股份有限公司 | System and method for efficient and energy-saving treatment of salt-containing wastewater |
| CN106746132B (en) * | 2017-02-17 | 2020-10-09 | 沈阳艾柏瑞环境科技有限公司 | 3R principle-based enterprise production wastewater zero-discharge process route |
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| CN107021581B (en) * | 2017-05-29 | 2021-02-19 | 新疆新鑫矿业股份有限公司阜康冶炼厂 | Preparation method of pure water |
| CN107162344B (en) * | 2017-07-03 | 2020-10-02 | 苏州华商新能源有限公司 | Sewage treatment method |
| CN108483774B (en) * | 2018-06-12 | 2021-08-06 | 贵州永合益环保科技有限公司 | Wastewater treatment method |
| CN108996796A (en) * | 2018-08-21 | 2018-12-14 | 成渝钒钛科技有限公司 | A kind of processing unit and processing method of vanadium waste |
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| CN108558099B (en) | 2020-10-27 |
| CN105540972B (en) | 2018-02-09 |
| CN108203197A (en) | 2018-06-26 |
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| CN108203197B (en) | 2020-07-31 |
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