CN107352727A - A kind of coal chemical industrial waste water goes out salt Zero discharging system and its implementation - Google Patents
A kind of coal chemical industrial waste water goes out salt Zero discharging system and its implementation Download PDFInfo
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- CN107352727A CN107352727A CN201710801359.2A CN201710801359A CN107352727A CN 107352727 A CN107352727 A CN 107352727A CN 201710801359 A CN201710801359 A CN 201710801359A CN 107352727 A CN107352727 A CN 107352727A
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- C02F9/00—Multistage treatment of water, waste water or sewage
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- 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
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- 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
- C02F1/08—Thin film evaporation
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- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
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- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
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- 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
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
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- 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
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- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
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- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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Abstract
The invention discloses coal chemical industrial waste water to go out salt Zero discharging system, the system includes concentration systems and divides salt system, described point of salt system includes monovalent salt vaporising device and divalent salts vaporising device, coal chemical industrial waste water by concentration systems and is divided under the collective effect of salt system, by the noxious pollutant separation in water body, it is recycled, realizes the process of industrial zero-emission.It can be kept completely separate and reclaim utility, greatly mitigate environmental pressure, form the new raw material of industry, reduce industrial production cost.The invention also discloses realizing that coal chemical industrial waste water goes out the method for salt zero-emission, including step Wastewater Pretreatment, stoste concentration be salt in stoste evaporation.Its iterative cycles processing procedure, while recovery Recyclable completely can be realized, solid discharge is ensured without the uniqueness in recycling and solution discharge, avoiding emission up to standard from repeating after being superimposed, reaction produces new pollutant again.
Description
Technical field
The present invention relates to the recycling non-pollution discharge technology of the coal chemical industrial waste water of field of Environment Protection, more particularly to a kind of coal
Wastewater from chemical industry goes out salt Zero discharging system and its implementation.
Background technology
Environmental pollution has been one of significant problem existing for today's society, mainly includes living garbage pollution and industry
Blowdown is polluted, in particular, in that discharge of industrial wastes, in the waste water in industrial production containing substantial amounts of organic matter, inorganic matter, metal class, with
And industrial salt, it directly discharges and exerted heavy pressures on to environment.
Present Industrial Waste Water Treatments are largely addition chemicals, arrange water body after precipitating metal deposition separation
To put, solid is directly recovered as cement raw material, and detection of such a method at the beginning of discharge can meet industrial wastewater discharge standard, but
After discharge, due to a large amount of salts substances in solution be present, can pressure be brought to environment when industrial salt adds up excessive, be in
Negative growth, and the solid residue as cement raw material is directly used in, due to wherein containing substantial amounts of metal, in calcination process
With other substance reactions, cement quality is directly affected, and in such a method, metal and salt are also the important raw material of industry,
And it directly discharges two class materials, also cause the waste of resource, and the difficulty of recycling is big.
The content of the invention
With reference to the deficiencies in the prior art, the invention provides a kind of coal chemical industrial waste water to go out salt Zero discharging system and its realization side
Method, effectively solve, secondary pollution and Recyclable recycle the problem of difficulty is big after coal chemical industrial waste water processing discharge.
The purpose of the present invention is achieved through the following technical solutions：
A kind of coal chemical industrial waste water goes out salt Zero discharging system, the system include being used for concentrating the concentration systems of coal chemical industrial waste water with
And for separating point salt system of salt component, it is described to divide the monovalent salt vaporising device that salt system includes being connected with each other to be steamed with divalent salts
Transmitting apparatus；The concentration systems include pretreatment stage, and the pretreatment stage is sequentially connected resin softening equipment and first anti-
Penetration equipment；The pretreatment stage includes efficient sedimentation tank, the efficient sedimentation tank be sequentially connected regulating reservoir, oxidation pond and
Ultrafiltration apparatus, the ultrafiltration apparatus are connected with the resin softening equipment, are cooperated and are removed between the multiple equipment of concentration systems
The solid particle and metal ion gone in waste water forms stoste.
Further, for the efficient sedimentation tank to contain flocculant, the regulating reservoir is neutral regulating reservoir.
Further, multi-medium filtering equipment, the multi-medium filtering are additionally provided between the oxidation pond and ultrafiltration apparatus
Equipment is provided with liquid-phase outlet and solid-phase outlet, and the liquid-phase outlet connects the ultrafiltration apparatus, the solid-phase outlet and solid
Collecting device connects.
Further, the low concentration solution outlet connection recovery pond of first reverse osmosis equipment, first counter-infiltration
The highly concentrated solution outlet of equipment is sequentially connected anti-pollution reverse-osmosis equipment and nanofiltration device, and the nanofiltration equipment connects institute respectively
State divalent salts vaporising device film light with sea, the light film in sea is connected high-pressure flat plate film device, the high-pressure flat plate film device connection monovalence
Salt vaporising device.
Further, the high-pressure flat plate film device is also connected with the second reverse osmosis equipment, second reverse osmosis equipment
Low concentration solution outlet connection recovery pond, the highly concentrated solution outlet connection anti-pollution reverse-osmosis of second reverse osmosis equipment are set
It is standby.
Further, the monovalent salt vaporising device includes First Heat Exchanger, and the First Heat Exchanger is sequentially connected first
Air inlet degasser, Falling film heat transfer device, falling film separator, the first crystal separator, the first thickener and the first centrifuge, it is described
The solid-phase outlet connection self-chambering system of first centrifuge, the liquid-phase outlet connection mother liquor tank of first centrifuge, described first
Heat exchanger, Falling film heat transfer device and falling film separator are steam-plate type heat exchanger, and the Falling film heat transfer device is also connected with the first heat exchange
Device, some vapor is back to First Heat Exchanger recycling again.
Further, the first forced circulation heat exchanger is additionally provided between the falling film separator and the first crystal separator,
The outlet of the first forced circulation heat exchanger steam is also respectively connected with the First Heat Exchanger and Falling film heat transfer device.
Further, the divalent salts vaporising device includes the second heat exchanger, and second heat exchanger is sequentially connected second
Air inlet degasser, the second forced circulation heat exchanger, the second crystal separator, the second thickener and the second centrifuge, described
The solid-phase outlet connection packaging system of two centrifuges, the liquid-phase outlet connection mother liquor tank of first centrifuge, the last the second
Circulation heat exchanger processed is also connected with the second heat exchanger.
Further, the steam (vapor) outlet of second crystal separator is also connected with compressor, the compressor connection second
Forced circulation heat exchanger, the second forced circulation heat exchanger are steam-plate type heat exchanger, the second forced circulation heat exchanger
It is also connected with the second heat exchanger.
A kind of method realized coal chemical industrial waste water and go out salt zero-emission, comprises the following steps：
S1, Wastewater Pretreatment：Coal chemical industrial waste water is directed into the efficient sedimentation tank, wadding is added into efficient sedimentation tank
Solidifying agent, makes the focusing particles in mixed liquor precipitate to form suspension, suspension is filtered, the solution of gained import regulating reservoir with
Oxidation pond, mixed liquor of the solution in neutrality being adjusted in the regulating reservoir, oxidation pond is ozonation aerated pond, while by mixed liquor
Partial organic substances be oxidized to short chain molecule or carbon dioxide, part metals ion reduction forms insoluble matter；Then mixed liquor
Again by ultrafiltration apparatus, solid and stoste are obtained after separation, stoste imports resin softening equipment；
S2, stoste concentration：Stoste after the softening of resin softening equipment enters the first reverse osmosis equipment, and by first
The stoste of low concentration obtained by reverse osmosis equipment is imported in the recovery pond, and the saturation stoste importing antipollution of high concentration is anti-
Penetration equipment carries out further concentrating and separating, and the impurity removed in saturation stoste obtains solution, and solution passes through the nanofiltration device,
The nanofiltration device retains divalent salts, and imports divalent salts evaporation equipment, is passed through respectively by the solution of the nanofiltration equipment
The light film in the sea and high-pressure flat plate film device, finally obtain high concentration liquid and low-concentration liquid, high concentration liquid are imported
The monovalent salt vaporising device, by low-concentration liquid after the second level reverse osmosis apparatus carries out secondary concentration, concentrate is led
Enter the anti-pollution reverse-osmosis device, the stillness of night is imported in recovery pond；
The evaporation of salt in S3, stoste：Monovalent salt evaporates：Monovalence salting liquid enters lifting temperature in the First Heat Exchanger,
Solution is lifted 10-20 DEG C on the basis of former temperature, then by the first air inlet degasser separate vapour, then change by falling liquid film
Hot device heats up again, temperature is reached 80-100 DEG C, into falling film separator with carried out in the first forced circulation heat exchanger it is secondary
It is concentrated by evaporation, wherein, the indirect steam of the first forced circulation heat exchanger is recycled back into described first again after overcompression temperature raising
Heat exchanger recycles with Falling film heat transfer device, and after solution concentration reaches discharge concentration, concentrate enters thickener, then passes through centrifugation
Machine isolates crystalline solid monovalent salt, and mother liquor enters mother liquor tank；
Divalent salts evaporate：Divalent salt solutions enter lifting temperature in second heat exchanger, temperature is reached 80-100 DEG C,
Then the second air inlet degasser separate vapour is passed through, the solution after heating degassing is directly entered the second forced circulation heat exchanger,
Concentration is evaporated in the crystal separator, the steam after crystal separator separation is back to the second pressure by compressor and followed
In ring heat exchanger, the condensed water that the indirect steam of the second forced circulation heat exchanger condenses out is sharp again into the second heat exchanger
With material reaches higher concentration after concentration, completes gas-liquid separation in separator, it is laggard that solution concentration reaches discharge concentration
Enter thickener, then crystalline solid divalent salts are isolated by centrifuge, mother liquor enters mother liquor tank.
The beneficial effects of the invention are as follows：
1st, the present invention uses solid-liquid continuous separating system, first washes out the order that solid insoluble purifies solution again, effectively
Reclaim in waste water using material more than 90%, greatly mitigate environmental pressure, meanwhile, produce the new raw material of industry, reduce
Industrial production cost；
2nd, it is of the invention to divide salt vapo(u)rization system, using a point evaporation technology for effect falling liquid film, system amount of liquid storage is substantially reduced, is passed through
Boiling point corresponding to distinguishing various concentrations, is used efficient Systems of Centrifugal Compressor Unit, is carried using effective temperature difference, compressor to greatest extent
It can meet requirement for the temperature difference, be compared with traditional MVR evaporators, greatly reduce the energy consumption of system；
3rd, in method of the invention, the method for its continuous processing, iterative cycles processing procedure, it can realize that recovery can completely
While regenerant, ensure that solid discharge without the uniqueness in recycling and solution discharge, avoids emission weight up to standard
Overlapping reacts again after adding produces new pollutant.
Brief description of the drawings
Fig. 1 is the block diagram that coal chemical industrial waste water provided in an embodiment of the present invention goes out salt Zero discharging system；
Fig. 2 is that coal chemical industrial waste water provided in an embodiment of the present invention goes out salt Zero discharging system concrete structure block diagram；
Fig. 3 is the block diagram of monovalent salt vaporising device in Fig. 2；
Fig. 4 is the block diagram of divalent salts vaporising device in Fig. 2；
Fig. 5 is the method provided in an embodiment of the present invention realized coal chemical industrial waste water and go out salt zero-emission.
Embodiment
To make the purpose, technical scheme and advantage of the embodiment of the present invention clearer, below in conjunction with the embodiment of the present invention
In accompanying drawing, the technical scheme in the embodiment of the present invention is clearly and completely described, it is clear that described embodiment is
Part of the embodiment of the present invention, rather than whole embodiments.The present invention implementation being generally described and illustrated herein in the accompanying drawings
The component of example can be configured to arrange and design with a variety of.Therefore, the reality of the invention to providing in the accompanying drawings below
The detailed description for applying example is not intended to limit the scope of claimed invention, is merely representative of the selected embodiment of the present invention,
Rather than whole embodiment.Based on the embodiment in the present invention, those of ordinary skill in the art are not making creative labor
The every other embodiment obtained under the premise of dynamic, belongs to the scope of protection of the invention.
Embodiment 1：
As shown in figure 1, Fig. 1 shows that coal chemical industrial waste water provided in an embodiment of the present invention goes out salt Zero discharging system, the system
Including concentration systems and divide salt system, divide salt system to include monovalent salt vaporising device and divalent salts vaporising device, by coal chemical industry
Waste water is by concentration systems and divides under the collective effect of salt system, by the noxious pollutant separation in water body, is recycled,
Realize the process of industrial zero-emission.
As shown in Fig. 2 concentration systems include pretreatment stage, resin softening equipment and permeability and separation equipment, pretreatment
Stage includes efficient sedimentation tank, and efficient sedimentation tank is sequentially connected regulating reservoir, oxidation pond and ultrafiltration apparatus, efficient sedimentation tank be containing
There is flocculant, regulating reservoir is PH regulating reservoirs, and ultrafiltration apparatus is redox, filter plant, between the multiple equipment of concentration systems
Cooperate the solid particle and metal ion formation stoste removed in waste water.
Wherein specifically, setting quick mixer in high speed pellets pond, make the coagulant and lime rapid dispersion added,
It is sufficiently mixed with raw water and uniformly, forms small flco.Raw water by Pre-coagulation flow to the circular guide shell set in reaction tank
Bottom, reversely it is well mixed from the bottom to top by the agitating paddle in guide shell, high sludge concentration improves the effect of flocculation, shape
Into after larger floccule body, rapid precipitation and concentration, separation metal recovery is arranged outside the solid after precipitation.Inclined tube is set in pond, remained
Remaining alumen ustum is detained on inclined tube, and bottom of pond is fallen into after being combined into big alumen ustum, ensures effluent quality, and water outlet enters in regulating reservoir, adjusts
Save pH value after by aeration tank ozone oxidation reduce, import ultrafiltration apparatus separation be finely divided from.
More specifically, multi-medium filtering equipment, the liquid of multi-medium filtering equipment are additionally provided between oxidation pond and ultrafiltration apparatus
Mutually outlet connection ultrafiltration apparatus, the solid-phase outlet connection solid collecting device of multi-medium filtering equipment, it enters solid particulate matter
Row separation and collection.
Specifically, permeability and separation equipment includes the first reverse osmosis equipment, the low concentration solution outlet of the first reverse osmosis equipment
Recovery pond is connected, the highly concentrated solution outlet of the first reverse osmosis equipment is sequentially connected anti-pollution reverse-osmosis equipment and nanofiltration device,
Nanofiltration equipment connects divalent salts vaporising device film light with sea respectively, the light film in sea is connected high-pressure flat plate film device, high-pressure flat plate
Film device connects monovalent salt vaporising device.
It is further preferred that high-pressure flat plate film device is also connected with the second reverse osmosis equipment, the second reverse osmosis equipment it is low dense
Spend taphole connection recovery pond, the highly concentrated solution outlet connection anti-pollution reverse-osmosis equipment of the second reverse osmosis equipment.
As shown in figure 3, monovalent salt vaporising device includes First Heat Exchanger, First Heat Exchanger is sequentially connected the first air inlet degassing
Device, Falling film heat transfer device, falling film separator, the first crystal separator, the first thickener and the first centrifuge, the first centrifuge
Solid-phase outlet connects self-chambering system, the liquid-phase outlet connection mother liquor tank of the first centrifuge, First Heat Exchanger, Falling film heat transfer device and drop
Membrane separator is steam-plate type heat exchanger, and Falling film heat transfer device is also connected with First Heat Exchanger.
Wherein specifically, being additionally provided with the first forced circulation heat exchanger between falling film separator and the first crystal separator, the
The second outlet of one forced circulation heat exchanger is also respectively connected with First Heat Exchanger and Falling film heat transfer device, and self-chambering system is that solid is automatic
Collection device.
In practical work process, membrane separator and the first crystal separator also by compressor connect Falling film heat transfer device and
First forced circulation heat exchanger, it is mainly by after indirect steam compresses heating again in membrane separator and the first crystal separator
Recycle, it is ensured that the maximization of using energy source.
As shown in figure 4, divalent salts vaporising device includes the second heat exchanger, second heat exchanger is sequentially connected the second air inlet
Degasser, the second forced circulation heat exchanger, the second crystal separator, the second thickener and the second centrifuge, the second centrifuge
Solid-phase outlet connection packaging system, the liquid-phase outlet connection mother liquor tank of the first centrifuge, the second forced circulation heat exchanger also connects
Connect the second heat exchanger.
Wherein, packaging system is the collection device of solid.
More specifically, the steam (vapor) outlet of the second crystal separator is also connected with compressor, and the compressor connection second is forced
Circulation heat exchanger, the second forced circulation heat exchanger are steam-plate type heat exchanger, and the second forced circulation heat exchanger is also connected with second and changed
Hot device, the circulation heating of indirect steam, returns again to system utilization, maintains whole system to reach thermal balance.
For the individual equipment of the system using automatic control system monitoring, operation, it is soft using the configuration of function admirable
Part.With powerful configuration function, whole project total system figure most can be reasonably completed, technological process picture, control flow is total
The windows displays such as figure；Dynamic technological process picture；Equipment running status and procedure parameter；The state at each independent control station
The automatic record of display, alarm and event；Online printing, tendency chart, production report generation, data processing, upper control order
Send, the technical functionality such as auto-manual switching.And maintenance of the user that the editing dialog frame to Chinesize more makes in the later stage simply may be used
OK.
Embodiment 2：
As shown in figure 5, Fig. 5 shows the method provided in an embodiment of the present invention realized coal chemical industrial waste water and go out salt zero-emission,
Comprise the following steps：
S1, Wastewater Pretreatment：Coal chemical industrial waste water is directed into the efficient sedimentation tank, wadding is added into efficient sedimentation tank
Solidifying agent, makes the focusing particles in mixed liquor precipitate to form suspension, suspension is filtered, the solution of gained import regulating reservoir with
Oxidation pond, mixed liquor of the solution in neutrality being adjusted in the regulating reservoir, oxidation pond is ozonation aerated pond, while by mixed liquor
Partial organic substances be oxidized to short chain molecule or carbon dioxide, part metals ion reduction forms insoluble matter；Then mixed liquor
Again by ultrafiltration apparatus, solid and stoste are obtained after separation, stoste imports resin softening equipment；
Wherein, ultrafiltration apparatus includes ultrafiltration body apparatus, ultrafiltration recoil pressure device and chemistry reinforcement recoil pressure device.
Ultrafiltration body apparatus is made up of hyperfiltration membrane assembly, operated pneumatic valve, pressure gauge, flowmeter, pipe valve, balladeur train etc..This is
System uses external compression type hollow fiber ultrafiltration membrane, has good contamination resistance and backwash, cleaning recovery capability.In order to ensure being
System is capable of the operation of long-term safety stabilization, avoids membrane module from bearing higher operating load, this programme design membrane component water flux
No more than 40L/ (m2·h)。
Ultrafiltration apparatus production water configuration flow indication, to control the normal safe operation of ultrafiltration apparatus.Ultrafiltration apparatus is intake
And pressure gauge is installed at production water, water inlet is equipped with pressure switch, can effectively monitor the operation of system.Ultrafiltration apparatus is provided with the spot
Controller dial plate.
Ultrafiltration apparatus is arranged on a framework, and for membrane component by the way of being arranged in juxtaposition, Inlet and outlet water main pipe sets cleaning
It is connected with valve, during to clean with cleaning fluid inlet/outlet pipe.Whole pipelines and joint, in addition to all branch are equipped with framework
Frame, fastener, fixture etc., and the design of framework meets local earthquake intensity.
The rich product such as suspension, colloid, bacterium and the larger molecular organicses of ultrafiltration system retention is in the surface of film, these dirts
The presence of thing can influence the normal filtration of system, to ensure the stable operation of system, reach the good ability for removing dirt, be equipped with
Backwashing system periodically backwashes to ultrafiltration apparatus.In order to which backwash is more thorough, backwash uses air water joint backwash mode, instead
Using ultrafiltration production water, compressed air needed for backwash comes from technique compressed air reservoir in wash water source.
In order to recover the filtration flux of milipore filter, extend the Chemical cleaning cycle, in milipore filter backwash irregularly to backwash
Chemical agent is added in water, typically uses pickling and alkali cleaning.Pickling uses hydrochloric acid, and alkali cleaning uses NaOH+NaC1O.
S2, stoste concentration：Stoste after the softening of resin softening equipment enters the first reverse osmosis equipment, and by first
The stoste of low concentration obtained by reverse osmosis equipment is imported in the recovery pond, and the saturation stoste importing antipollution of high concentration is anti-
Penetration equipment carries out further concentrating and separating, and the impurity removed in saturation stoste obtains solution, and solution passes through the nanofiltration device,
The nanofiltration device retains divalent salts, and imports divalent salts evaporation equipment, is passed through respectively by the solution of the nanofiltration equipment
The light film in the sea and high-pressure flat plate film device, finally obtain high concentration liquid and low-concentration liquid, high concentration liquid are imported
The monovalent salt vaporising device, by low-concentration liquid after the second level reverse osmosis apparatus carries out secondary concentration, concentrate is led
Enter the anti-pollution reverse-osmosis device, the stillness of night is imported in recovery pond；
The evaporation of salt in S3, stoste：Monovalent salt evaporates：Monovalence salting liquid enters lifting temperature in the First Heat Exchanger,
Then pass through the first air inlet degasser separate vapour, then heated up again by Falling film heat transfer device, into falling film separator and first
Double evaporation-cooling concentration is carried out in forced circulation heat exchanger, wherein, the indirect steam of the first forced circulation heat exchanger carries through overcompression
The First Heat Exchanger is recycled back into after temperature again to recycle with Falling film heat transfer device, it is dense after solution concentration reaches discharge concentration
Contracting liquid enters thickener, then isolates crystalline solid monovalent salt by centrifuge, and mother liquor enters mother liquor tank；
The stoste to be come by high-pressure flat plate film squeezes into preheating heat exchanger by feed pump, and feeding liquid is with steaming in plate type heat exchanger
Vapour condensed water, fresh steam are (reserved) to carry out heat exchange, enters the circulation of Falling film heat transfer device after being warming up to evaporating temperature, is separated in falling liquid film
Concentration is evaporated in device.After material is by once concentrating, the solution after gas-liquid separation, which enters crystal separator and first, to be forced
Circulation heat exchanger continues cycling through evaporation and concentration；Material reaches higher concentration in crystal separator, and gas-liquid is completed in separator
Separation.After solution concentration reaches discharge concentration, concentrate isolates crystalline solid one by being pumped into thickener, then by centrifuge
Valency salt, mother liquor enter mother liquor tank.In addition, the indirect steam come out from gas-liquid separator, clean after abundant gas-liquid separation
Indirect steam passes through compressor, and after indirect steam is compressed, temperature can raise 16 DEG C or so, and the steam increasing temperature and pressure after compression is beaten
Enter Falling film heat transfer device heated material.During heated material, this part high-temperature steam is condensed into water and flow to condensate filling and by steaming
Distilled water pump is pumped into plate type heat exchanger and exchanged heat with material liquid, and temperature is down to 30 DEG C or so discharge systems.Material after preheated enters
After evaporator, and steam after compression carries out heat exchange evaporation, and whole system reaches thermal balance.
Divalent salts evaporate：Divalent salt solutions enter lifting temperature in the second heat exchanger, then by the second air inlet degasser
Separate vapour, the solution after heating degassing are directly entered the second forced circulation heat exchanger, are evaporated in crystal separator dense
Contracting, the steam after crystal separator separation are back in the second forced circulation heat exchanger by compressor, and the second forced circulation is changed
The condensed water that the indirect steam of hot device condenses out reuses into the second heat exchanger, and material reaches higher after concentration
Concentration, gas-liquid separation is completed in separator, solution concentration enters thickener after reaching discharge concentration, then is isolated by centrifuge
Crystalline solid divalent salts, mother liquor enter mother liquor tank.
Stoste after being handled by nanofiltration device squeezes into preheating heat exchanger by material pump, feeding liquid and steam in plate type heat exchanger
Condensed water, fresh steam are (reserved) to carry out heat exchange, enters the circulation of the second forced circulation heat exchanger after being warming up to evaporating temperature, is tying
Concentration is evaporated in brilliant separator.Material reaches higher concentration by thing after concentration, and gas-liquid separation is completed in separator.It is molten
After liquid concentration reaches discharging saturated concentration, concentrate isolates crystalline solid divalence by being pumped into thickener, then by centrifuge
Salt, mother liquor enter mother liquor tank.The indirect steam come out from crystal separator, after abundant gas-liquid separation, clean secondary steaming
Vapour enters compressor, and after indirect steam is compressed, temperature can raise 18 DEG C or so, and the steam increasing temperature and pressure after compression squeezes into second
Forced circulation heat exchanger heated material.During heated material, this part high-temperature steam be condensed into water flow to condensate fill and by
Distilled water pump is pumped into plate type heat exchanger and exchanged heat with material liquid, and temperature is down to 30 DEG C or so discharge systems.Material after preheated enters
After entering evaporator, and steam after compression carries out heat exchange evaporation, and whole system reaches thermal balance.Mother liquor caches by mother liquor
Tank, crystal is thrown away finally by centrifuge into cooling reactor by heat exchanger heat exchange and removes dry packing, remaining liq enters mother liquor
Tank.
Finally it should be noted that：Above-described embodiments are merely to illustrate the technical scheme, rather than to it
Limitation；Although the present invention is described in detail with reference to the foregoing embodiments, it will be understood by those within the art that：
It can still modify to the technical scheme described in previous embodiment, or which part or all technical characteristic are entered
Row equivalent substitution；And these modifications or substitutions, the essence of appropriate technical solution is departed from various embodiments of the present invention technical side
The scope of case.
Claims (10)
1. a kind of coal chemical industrial waste water goes out salt Zero discharging system, it is characterised in that：The system includes being used to concentrate coal chemical industrial waste water
Concentration systems and point salt system for separating salt component, it is described to divide salt system to include the monovalent salt vaporising device being connected with each other
With divalent salts vaporising device；The concentration systems include pretreatment stage, and the pretreatment stage is sequentially connected resin softening and set
It is standby with the first reverse osmosis equipment；The pretreatment stage includes efficient sedimentation tank, the efficient sedimentation tank be sequentially connected regulating reservoir,
Oxidation pond and ultrafiltration apparatus, the ultrafiltration apparatus is connected with the resin softening equipment, between the multiple equipment of concentration systems
Cooperate the solid particle and metal ion formation stoste removed in waste water.
2. coal chemical industrial waste water as claimed in claim 1 goes out salt Zero discharging system, it is characterised in that：Add in the efficient sedimentation tank
Added with flocculant, the regulating reservoir is neutral regulating reservoir.
3. coal chemical industrial waste water as claimed in claim 2 goes out salt Zero discharging system, it is characterised in that：The oxidation pond is set with ultrafiltration
Multi-medium filtering equipment is additionally provided between standby, the multi-medium filtering equipment is provided with liquid-phase outlet and solid-phase outlet, the liquid
Mutually outlet connects the ultrafiltration apparatus, and the solid-phase outlet is connected with solid collecting device.
4. coal chemical industrial waste water as claimed in claim 2 goes out salt Zero discharging system, it is characterised in that：First reverse osmosis equipment
Low concentration solution outlet connection recovery pond, to be sequentially connected antipollution anti-for the highly concentrated solution outlet of first reverse osmosis equipment
Penetration equipment and nanofiltration device, the nanofiltration equipment connect the divalent salts vaporising device and the light film in sea, the light film connection in sea respectively
High-pressure flat plate film device, the high-pressure flat plate film device connect monovalent salt vaporising device.
5. coal chemical industrial waste water as claimed in claim 4 goes out salt Zero discharging system, it is characterised in that：The high-pressure flat plate film device
The second reverse osmosis equipment is also connected with, the low concentration solution outlet connection recovery pond of second reverse osmosis equipment, described second is anti-
The highly concentrated solution outlet connection anti-pollution reverse-osmosis equipment of penetration equipment.
6. the coal chemical industrial waste water as described in claim 1 or 4 goes out salt Zero discharging system, it is characterised in that：The monovalent salt evaporation
Device includes First Heat Exchanger, and the First Heat Exchanger is sequentially connected the first air inlet degasser, Falling film heat transfer device, falling liquid film separation
Device, the first crystal separator, the first thickener and the first centrifuge, the solid-phase outlet connection self-chambering system of first centrifuge
System, the liquid-phase outlet connection mother liquor tank of first centrifuge, the First Heat Exchanger, Falling film heat transfer device and falling film separator are equal
For steam-plate type heat exchanger, the Falling film heat transfer device is also connected with First Heat Exchanger, some vapor is back to the first heat exchange again
Device reuses.
7. coal chemical industrial waste water as claimed in claim 6 goes out salt Zero discharging system, it is characterised in that：The falling film separator and the
The first forced circulation heat exchanger is additionally provided between one crystal separator, the outlet of the first forced circulation heat exchanger steam also divides
The First Heat Exchanger and Falling film heat transfer device are not connected.
8. the coal chemical industrial waste water as described in claim 1 or 4 goes out salt Zero discharging system, it is characterised in that：The divalent salts evaporation
Device includes the second heat exchanger, and second heat exchanger is sequentially connected the second air inlet degasser, the second forced circulation heat exchanger,
Two crystal separators, the second thickener and the second centrifuge, the solid-phase outlet connection packaging system of second centrifuge, institute
The liquid-phase outlet connection mother liquor tank of the first centrifuge is stated, the second forced circulation heat exchanger is also connected with the second heat exchanger.
9. coal chemical industrial waste water as claimed in claim 8 goes out salt Zero discharging system, it is characterised in that：Second crystal separator
Steam (vapor) outlet be also connected with compressor, the compressor connects the second forced circulation heat exchanger, the second forced circulation heat exchange
Device is steam-plate type heat exchanger, and the second forced circulation heat exchanger is also connected with the second heat exchanger.
A kind of 10. method realized coal chemical industrial waste water and go out salt zero-emission, it is characterised in that：Comprise the following steps：
S1, Wastewater Pretreatment：Coal chemical industrial waste water is directed into the efficient sedimentation tank, flocculation is added into efficient sedimentation tank
Agent, make the focusing particles in mixed liquor precipitate to form suspension, suspension is filtered, the solution of gained imports regulating reservoir and oxygen
To change pond, mixed liquor of the solution in neutrality is adjusted in the regulating reservoir, oxidation pond is ozonation aerated pond, while by mixed liquor
Partial organic substances are oxidized to short chain molecule or carbon dioxide, and part metals ion reduction forms insoluble matter；Then mixed liquor is again
By ultrafiltration apparatus, solid and stoste are obtained after separation, stoste imports resin softening equipment；
S2, stoste concentration：Stoste after the softening of resin softening equipment enters the first reverse osmosis equipment, and by the first reverse osmosis
The stoste of low concentration obtained by saturating equipment is imported in the recovery pond, and the saturation stoste of high concentration imports anti-pollution reverse-osmosis
Equipment carries out further concentrating and separating, and the impurity removed in saturation stoste obtains solution, and solution passes through the nanofiltration device, described
Nanofiltration device retains divalent salts, and imports divalent salts evaporation equipment, by the solution of the nanofiltration equipment respectively by described
The light film in sea and high-pressure flat plate film device, finally obtain high concentration liquid and low-concentration liquid, high concentration liquid is imported described in
Monovalent salt vaporising device, by low-concentration liquid after the second level reverse osmosis apparatus carries out secondary concentration, concentrate imports institute
Anti-pollution reverse-osmosis device is stated, the stillness of night is imported in recovery pond；
The evaporation of salt in S3, stoste：Monovalent salt evaporates：Monovalence salting liquid enters lifting temperature in the First Heat Exchanger, makes molten
Liquid lifts 10-20 DEG C on the basis of former temperature, then by the first air inlet degasser separate vapour, then by Falling film heat transfer device
Heat up again, temperature is reached 80-100 DEG C, double evaporation-cooling is carried out into falling film separator and the first forced circulation heat exchanger
Concentration, wherein, the indirect steam of the first forced circulation heat exchanger is recycled back into first heat exchange again after overcompression temperature raising
Device recycles with Falling film heat transfer device, and after solution concentration reaches discharge concentration, concentrate enters thickener, then passes through centrifuge point
Crystalline solid monovalent salt is separated out, mother liquor enters mother liquor tank；
Divalent salts evaporate：Divalent salt solutions enter lifting temperature in second heat exchanger, temperature is reached 80-100 DEG C, then
By the second air inlet degasser separate vapour, the solution after heating degassing is directly entered the second forced circulation heat exchanger, described
Concentration is evaporated in crystal separator, the steam after crystal separator separation is back to the second forced circulation by compressor and changed
In hot device, the condensed water that the indirect steam of the second forced circulation heat exchanger condenses out reuses into the second heat exchanger, warp
Material reaches higher concentration after crossing concentration, and gas-liquid separation is completed in separator, solution concentration reach enter after discharge concentration it is thick
Thick device, then crystalline solid divalent salts are isolated by centrifuge, mother liquor enters mother liquor tank.
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| CN108128969A (en) * | 2017-12-19 | 2018-06-08 | 德蓝水技术股份有限公司 | A kind of five embrane method combined treatment integrated approaches for coal chemical industry wastewater zero emission |
| CN108862856A (en) * | 2018-07-05 | 2018-11-23 | 上海文赟环境工程事务所 | A kind of acetate fiber waste water reclaiming processing method |
| CN111661888A (en) * | 2020-06-15 | 2020-09-15 | 方诺传热系统(江苏)有限公司 | Falling film type air cooler based on evaporative air cooling technology and wastewater treatment process |
| CN113772884A (en) * | 2021-09-03 | 2021-12-10 | 西安交通大学 | Coking wastewater treatment system and method |
| CN116891309A (en) * | 2023-06-14 | 2023-10-17 | 惠州大亚湾惠绿环保服务有限公司 | High-hardness high-salinity oily sewage treatment system |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108128969A (en) * | 2017-12-19 | 2018-06-08 | 德蓝水技术股份有限公司 | A kind of five embrane method combined treatment integrated approaches for coal chemical industry wastewater zero emission |
| CN108862856A (en) * | 2018-07-05 | 2018-11-23 | 上海文赟环境工程事务所 | A kind of acetate fiber waste water reclaiming processing method |
| CN111661888A (en) * | 2020-06-15 | 2020-09-15 | 方诺传热系统(江苏)有限公司 | Falling film type air cooler based on evaporative air cooling technology and wastewater treatment process |
| CN113772884A (en) * | 2021-09-03 | 2021-12-10 | 西安交通大学 | Coking wastewater treatment system and method |
| CN113772884B (en) * | 2021-09-03 | 2022-12-13 | 西安交通大学 | Coking wastewater treatment system and method |
| CN116891309A (en) * | 2023-06-14 | 2023-10-17 | 惠州大亚湾惠绿环保服务有限公司 | High-hardness high-salinity oily sewage treatment system |
| CN116891309B (en) * | 2023-06-14 | 2024-05-14 | 惠州大亚湾惠绿环保服务有限公司 | High-hardness high-salinity oily sewage treatment system |
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