CN109205902A - The industrial reverse osmosis waste heat recovery processing system of high-salt wastewater - Google Patents
The industrial reverse osmosis waste heat recovery processing system of high-salt wastewater Download PDFInfo
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- CN109205902A CN109205902A CN201811145689.1A CN201811145689A CN109205902A CN 109205902 A CN109205902 A CN 109205902A CN 201811145689 A CN201811145689 A CN 201811145689A CN 109205902 A CN109205902 A CN 109205902A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 60
- 238000001223 reverse osmosis Methods 0.000 title claims abstract description 59
- 238000012545 processing Methods 0.000 title claims abstract description 30
- 238000011084 recovery Methods 0.000 title claims abstract description 28
- 239000002918 waste heat Substances 0.000 title claims abstract description 23
- 239000012141 concentrate Substances 0.000 claims abstract description 50
- 239000012528 membrane Substances 0.000 claims abstract description 44
- 238000000034 method Methods 0.000 claims abstract description 17
- 238000007781 pre-processing Methods 0.000 claims abstract description 11
- 238000002425 crystallisation Methods 0.000 claims description 49
- 238000001035 drying Methods 0.000 claims description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 39
- 230000008025 crystallization Effects 0.000 claims description 29
- 238000010438 heat treatment Methods 0.000 claims description 22
- 239000013078 crystal Substances 0.000 claims description 21
- 239000007789 gas Substances 0.000 claims description 15
- 238000000926 separation method Methods 0.000 claims description 13
- 238000005189 flocculation Methods 0.000 claims description 10
- 230000016615 flocculation Effects 0.000 claims description 10
- 238000004062 sedimentation Methods 0.000 claims description 10
- 238000009833 condensation Methods 0.000 claims description 9
- 230000005494 condensation Effects 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 9
- 239000007921 spray Substances 0.000 claims description 8
- 238000005086 pumping Methods 0.000 claims description 6
- 150000003839 salts Chemical class 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 5
- 238000012546 transfer Methods 0.000 claims description 5
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 4
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 3
- 239000003456 ion exchange resin Substances 0.000 claims description 3
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 2
- 239000007787 solid Substances 0.000 abstract description 8
- 239000000463 material Substances 0.000 description 10
- 239000000084 colloidal system Substances 0.000 description 8
- 239000000243 solution Substances 0.000 description 8
- 239000011347 resin Substances 0.000 description 7
- 229920005989 resin Polymers 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 241000894006 Bacteria Species 0.000 description 5
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- 150000001768 cations Chemical class 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 2
- 241000700605 Viruses Species 0.000 description 2
- 238000011953 bioanalysis Methods 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 239000012267 brine Substances 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 230000002209 hydrophobic effect Effects 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 239000012452 mother liquor Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 150000003384 small molecules Chemical class 0.000 description 2
- 229910001415 sodium ion Inorganic materials 0.000 description 2
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 238000004056 waste incineration Methods 0.000 description 2
- -1 Ca in raw water2+ Chemical class 0.000 description 1
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- 101710088194 Dehydrogenase Proteins 0.000 description 1
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- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 230000035772 mutation Effects 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
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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
- 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
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- 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
- C02F1/043—Details
-
- 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
- C02F1/048—Purification of waste water by 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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- 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
- C02F2001/5218—Crystallization
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/22—Eliminating or preventing deposits, scale removal, scale prevention
Abstract
The present invention relates to the reverse osmosis waste heat recovery processing systems of industrial high-salt wastewater, including high-salt wastewater preprocessing module, reverse osmosis membrane processing module, level-one evaporator, second level MVR evaporator, crystallizer and drier, the high-salt wastewater preprocessing module pre-processes industrial high-salt wastewater, and pretreated waste water is transported to reverse osmosis membrane processing module to be filtered, and filtered concentrate is successively passed through into level-one evaporator and second level MVR evaporator, then high concentration concentrate is obtained from second level MVR evaporator enter crystallizer, ingot in crystallizer is delivered to the crystalline solid obtained in drier to the end, between the level-one evaporator and second level MVR evaporator, it is provided with vapor recovery between second level MVR evaporator and crystallizer and utilizes pipeline.
Description
Technical field
It is especially a kind of that high-salt wastewater and evaporative crystallization are handled using recovery waste heat the present invention relates to sewage treatment field
System.
Background technique
Waste incineration, dangerous waste incineration, metallurgy, petrochemical industry, pharmacy, coal chemical industry generate largely in process of production
High-salt wastewater, usual salt content reach 20000mg/L or more, and the salts substances of high concentration to biological growth and development and are bred very
Unfavorable, osmotic pressure is high, salinity is high, microbial cell dehydration causes cellular plasm to separate；Salting out makes dehydrogenase activity
It reduces；Chloride ion height is to the toxic effect of bacterium；Salinity is high, and the density of waste water increases, and activated sludge easily floats loss, thus
Seriously affect the normal operation of biological treatment system.
The processing of industrial high-salt wastewater is one of the difficult point studied both at home and abroad and hot spot, both at home and abroad to the research of high-salt wastewater
Mainly there are bioanalysis and physico-chemical process.Bioanalysis shows higher organic removal rate when handling high-salt wastewater, but
Longer domestication is usually required using Biochemical method high-salt wastewater, and the time needed for the higher acclimation sludge of salinity in waste water
It is longer；In addition, microorganism is sensitive to the change of environment, the mutation of salinity would generally generate serious interference to processing system.Object
Physicochemical method mainly has evaporation, electrochemical method, ion-exchange, absorption, membrane separation technique etc., in some applications can
The salinity and organic matter in waste water are enough removed, but generally all suffers from higher cost, and easily cause the secondary pollution of regenerative wastewater.
Summary of the invention
The present invention is provided and a kind of handled high-salt wastewater using recovery waste heat and steamed to solve the deficiency of above-mentioned technology
The system for sending out crystallization.
In order to solve the above-mentioned technical problem, including high-salt wastewater preprocessing module, reverse osmosis membrane processing module, level-one are evaporated
Device, second level MVR evaporator, crystallizer and drier, the high-salt wastewater preprocessing module carry out industrial high-salt wastewater pre-
Processing, and pretreated waste water is transported to reverse osmosis membrane processing module and is filtered, and filtered concentrate is first
Afterwards by level-one evaporator and second level MVR evaporator, high concentration concentrate then is obtained from second level MVR evaporator and enters knot
Crystallization in crystallizer, is delivered to the crystalline solid obtained in drier to the end by brilliant device, and the level-one evaporator and second level MVR steam
It sends out between device, vapor recovery is provided between second level MVR evaporator and crystallizer and utilizes pipeline.
With the above structure, high-salt wastewater is pre-processed first, removes large particulate matter and reduction in waste water
COD in water, but 0.1-10um bacterium below, suspended matter, colloid, minerals, salinity can not be filtered out etc., so reverse osmosis need to be passed through
The organic matter and inorganic matter of the secondary treatment removal 0.1-1nm of permeable membrane.I.e. by pretreatment, guarantee the treatment effect of reverse osmosis membrane
And service life is sent into level-one evaporator by reverse osmosis membrane after waste water is further concentrated, water purification flows into reuse water system.
Steam heats the original steam reuse using cooling tower cooler to evaporator, utilizes resource, energy saving.Evaporator second level is steamed
Vapour is heated for rear class, solves the use of steam efficiency, and each evaporator also configures main steam pipe and main steam is accessed heating.
It can also be with vapour compression machine to second level MVR evaporator circulating-heating.Into after crystallizer, remaining concentrate evaporative crystallization.Crystallization
Body valve outlet? and it is delivered to crystallizing and drying device, by forming crystalline solid output after crystallizing and drying.The program can accomplish high-salt wastewater
Zero-emission.
As a further improvement of the present invention, the high-salt wastewater preprocessing module includes that high-salt wastewater is wadded a quilt with cotton first
Liquid after flocculation sedimentation is carried out the ion exchange resin of sofening treatment by the flocculation sedimentation tank that retrogradation is formed sediment.
With the above structure, (by adding such as PAC in flocculation sedimentation tank, ferric trichloride flocculant can be right
The negative electrical charge of colloid surface carries out unstability processing, and colloid is captured on the micro floc of nascent state, while by precipitating
Journey greatly reduces concentration of suspension in waste water, avoids blocking+exchanger resin softening of exchanger resin: may be containing excessive in raw water
Fouling cation, such as Ca2+、Mg2+、Ba2+And Sr2+Deng needing to carry out softening pretreatment.It is replaced using sodium ion and removes fouling
Type cation, resins exchange use brine regeneration after being saturated.To reduce the scale problems of reverse osmosis membrane.After adopting the above structure,
The subsequent damage to reverse osmosis membrane can be reduced, and the impurity of most can be filtered in advance, it is from efficiency and whole
Biggish guarantee has all been obtained in service life.
As a further improvement of the present invention, the reverse osmosis membrane processing module includes connecting with (exchanger resin device) pipeline
Connect the booster pump for increasing inlet hydraulic and the reverse osmosis membrane filt with booster pump piping connection, the reverse osmosis membrane mistake
Filter includes the reverse osmosis membrane and pure water discharge outlet that reverse osmosis membrane filt is arranged in, the reverse osmosis membrane filt and level-one
Evaporator pipeline connects, and the pumping motor for pumping liquid is provided in the pipeline of connection.
With the above structure, reverse osmosis membrane aperture as low as nanoscale, under pressure, hydrone can pass through
Reverse osmosis membrane, and the impurity such as inorganic salts, heavy metal ion, organic matter, colloid, bacterium, virus in waste water can not pass through.
As a further improvement of the present invention, the level-one evaporator includes evaporator inner cavity, is arranged in level-one evaporator
The spray head for being used to spray concentrate that is interior intracavitary and being connected with reverse osmosis membrane pipeline, is arranged in the first steam of evaporator outer wall
Air intake is arranged in the first steam gas outlet on evaporator outer wall top, the first concentrate of level-one evaporator outer wall is arranged in
Outlet, described first steam air intake one end is connected to evaporator inner cavity, and the connectivity part of the other end is provided with main steam
It manages, is provided on the main steam pipe for providing the steam generator of steam to level-one evaporator inner cavity.
With the above structure, main steam pipe can provide original steam to level-one evaporator, and level-one evaporator makes
With three-dimensional overall process heating is sprayed, aloft spraying, declined with small molecule or little particle down, spray process heating surface area is big,
Can be rapidly heated to osmosis filtration film filtered concentrate heating.
As a further improvement of the present invention, the first concentrate connecting tube is provided on the first concentrate outlet
Road, described first concentrate connecting pipe one end are connected with level-one evaporator, and the other end is connected with second level MVR evaporator, described
Second level MVR evaporator includes the inner cavity MVR, and injector head that is intracavitary in MVR and being connected with concentrate connecting tube pipeline is arranged in, setting
In the second steam air intake of MVR evaporator outer wall, the second steam gas outlet on evaporator outer wall top is set, is arranged two
Second concentrate outlet of grade MVR evaporator outer wall, described second steam air intake one end are connected to the inner cavity MVR, and the other end connects
Logical main steam pipe, is additionally provided with steam between the evaporator inner cavity of the level-one evaporator and the inner cavity MVR of second level MVR evaporator
Pipeline is recycled, and the second steam air intake also passes through Steam Recovery while connecting main steam pipe and utilizes pipeline and one
The first steam gas outlet connection of grade evaporator.
With the above structure, it is provided with Steam Recovery and utilizes pipeline, it can be by the steam recycling of level-one evaporator
Into second level MVR evaporator, the technical effect of waste heat recycling is played.
As a further improvement of the present invention, the crystallizer includes crystallizer outer wall, the crystallisation chamber being set in outer wall,
Separation concentrated solution tank, concentrating return-flow pump and heat exchanger, the second concentrate outlet of the second level MVR evaporator outer wall
On be provided with the second concentrate connecting pipe, described second concentrate connecting pipe one end is connected with second level MVR evaporator, another
End is connected with crystallisation chamber, and the separation concentrated solution tank is positioned adjacent to crystallisation chamber bottom side, and the concentrating return-flow pump is set to
Far from crystallisation chamber side, concentrate pumps after flowing out from crystallisation chamber to separation concentrated solution tank, then by concentrating return-flow separation concentrated solution tank
The concentrate being concentrated in flow container is delivered in heat exchanger, described heat exchanger one end is connected with concentrating return-flow pump, the other end
It is connected with the second concentrate connecting pipe.The heat exchanger includes heating outer wall and heating chamber, the heat exchanger heating
Outer wall is provided with steam pipeline (trace) mouth, and the main steam pipe is connected with steam pipeline (trace) mouth, and heats to heat exchanger outer
Wall is heated, and is provided with third steam air intake on the crystallizer outer wall, the third steam air intake can respectively with master
Steam pipe and the second steam gas outlet pipeline are connected, second steam gas outlet one end and third steam air intake pipeline phase
Even, the other end is connected with the second steam air intake pipeline.
With the above structure, the heat exchanger in crystallizer needs heat source to go to provide heating function, and utilizes second level
Steam in MVR evaporator and main steam pipe heats the outer wall of heat exchanger, to can not need to provide
In the case where external heat source, heat exchanger is heated using itself extra steam.And flow container is concentrated, concentrating return-flow
Pump and heat exchanger form a heat cycles, and concentrate is constantly heated, to obtain crystalline solid to the end.
As a further improvement of the present invention, the drying device includes at crystal feed device and crystal drying
Device is managed, the crystallisation chamber bottom is provided with crystallization outlet, is connected at the crystallization outlet crystallization progress is whole
The disc type blanking machine of blanking is closed, the disc type blanking machine includes the driving motor that blanking plate and driving blanking plate are driven,
One end of the blanking plate is connected with crystallization outlet, and the other end is connected with crystal feed device.
With the above structure, the use of drying device can be dehydration completely in the form of help crystallisation body is finally discharged
State, and need to carry out material transmission between drying device and crystallisation chamber just and the dry working condition between crystallization turn can be achieved
Change, using material can be prevented to be discharged excessively after disc type blanking machine quickly, is extruded on feed device, thus can not be just
Material is quickly transferred in drying device by victory, and disc type blanking machine then carries out orderly row to the material in blanking process
Cloth allows transfer process to become more smooth.
As a further improvement of the present invention, the crystal feed device includes crystal screw elevator, the knot
Brilliant object screw elevator one end is connect with the blanking plate of disc type blanking machine, and the other end is connect with crystal drying process device, institute
Stating crystal drying process device is vacuum rake style drier, including drying chamber, is set to the crystallization waste heat layer on drying chamber upper layer,
It is set to the crystallizing and drying layer in drying chamber middle layer, is set to the crystallizing and drying finished layer of drying chamber lower layer, and is disposed through
The hot axis for Stirring heat transfer in drying chamber middle layer, the hot axis are driven by hot axis driving motor.
With the above structure, the working principle of vacuum rake style drier is constantly heated to material by hot axis
Dry and hydrophobic technical effect is played in stirring.
As a further improvement of the present invention, the reverse osmosis multiple-effect waste heat evaporative crystallization recovery system of the industrial high-salt wastewater
It further include condensing water heat exchanger, the first condensed water discharge outlet, the second condensed water discharge outlet and third condensed water discharge outlet, altogether
Heat exchange is carried out into condensation water heat exchanger with guiding condensed water, the condensation water heat exchanger includes cooling water inlet
And condensed water discharge outlet.
With the above structure, so the condensed water of discharge can be handled and is emitted into cooling tower by setting,
Generate an effective cooling water circulating treatment procedure.
Detailed description of the invention
Fig. 1 show industrial high-salt wastewater processing system general assembly drawing；
Fig. 2 show high-salt wastewater preprocessing module treatment process schematic diagram；
Fig. 3 show reverse osmosis membrane processing modular structure schematic diagram；
Fig. 4 show level-one evaporation structure schematic diagram；
Fig. 5 show MVR evaporation structure schematic diagram；
Fig. 6 show mold structure schematic diagram；
Fig. 7 show dryer configuration schematic diagram.
Specific embodiment
As shown in Figure 1, including high-salt wastewater preprocessing module 1, reverse osmosis membrane processing module 2, level-one evaporator 3, second level
MVR evaporator 4, crystallizer 5 and drier 6, the high-salt wastewater preprocessing module 1 are located industrial high-salt wastewater in advance
Reason, and pretreated waste water is transported to reverse osmosis membrane processing module 2 and is filtered, and filtered concentrate is successive
By level-one evaporator 3 and second level MVR evaporator 4, the entrance of high concentration concentrate is then obtained from second level MVR evaporator 4
Crystallization in crystallizer 5 is delivered to the crystalline solid obtained in drier to the end, the level-one evaporator and second level by crystallizer 5
Between MVR evaporator, it is provided with vapor recovery between second level MVR evaporator and crystallizer and utilizes pipeline.First to mother liquor into
Row pretreatment, but pretreatment can not wherein filter out 0.1-10um bacterium below, suspended matter, pigment, colloid, minerals, salt,
Enter so 0.1-1nm organic matter inorganic matter can will be completely cut off by the secondary treatment of reverse osmosis membrane.And pass through Wastewater Pretreatment,
Reduce impurity when film is filtered, protect reverse osmosis membrane is not damaged to enhance service life, passes through reverse osmosis membrane mistake
After filter, mother liquor is further concentrated and is sent into level-one evaporator 3, water purification flows into recycle-water.Steam will be originally using cooling tower cooler
Steam reuse to evaporator heat, saved energy consumption.Evaporator second steam is heated for rear class, solves steam efficiency
It uses, each evaporator also configures main steam pipe and main steam is accessed heating.It can also be with vapour compression machine to second level MVR evaporator
Circulating-heating.Into after crystallizer, remaining concentrate evaporative crystallization.Crystalline solid valve outlet is simultaneously delivered to crystallizing and drying device, passes through
The last crystalline solid output of crystallizing and drying.The program can accomplish high-salinity wastewater zero-emission.
The high-salt wastewater preprocessing module includes the flocculation sedimentation tank 11 that high-salt wastewater is carried out to flocculation sedimentation first,
Liquid after flocculation sedimentation is carried out to the ion exchange resin 12 of sofening treatment.By added in flocculation sedimentation tank as PAC,
The flocculants such as ferric trichloride can carry out unstability processing to the negative electrical charge of colloid surface, and colloid is captured to the small wadding of nascent state
On shape object, while concentration of suspension in waste water is greatly reduced by precipitation process, avoids blocking+exchanger resin of exchanger resin soft
Change: may be containing excessive fouling cation, such as Ca in raw water2+、Mg2+、Ba2+And Sr2+Deng needing to carry out softening pretreatment.Make
It is replaced with sodium ion and removes fouling type cation, use brine regeneration after resins exchange saturation.To reduce the fouling of reverse osmosis membrane
Problem.After adopting the above structure, it is possible to reduce the subsequent damage to reverse osmosis membrane, and the miscellaneous of most can be filtered in advance
Matter has all obtained biggish guarantee from efficiency and on whole service life.
The reverse osmosis membrane processing module 2 include be used to increase with filtering ponds piping connection the booster pump 21 of inlet hydraulic with
And the reverse osmosis membrane filt 22 with booster pump piping connection, the reverse osmosis membrane filt 22 include being arranged in reverse osmosis membrane mistake
The reverse osmosis film 221 and pure water discharge outlet 222 of filter, the reverse osmosis membrane filt 22 connect with 3 pipeline of level-one evaporator
It connects, and is provided with the pumping motor for pumping liquid in the pipeline of connection.Reverse osmosis membrane aperture as low as nanoscale, one
Under fixed pressure, hydrone can be inorganic salts, heavy metal ion, organic matter, colloid in the water of source, thin by reverse osmosis membrane
The impurity such as bacterium, virus can not be by reverse osmosis membrane, so that the condensed water that makes the pure water that can be penetrated and can not penetrate strictly is distinguished
It comes.
The level-one evaporator 3 include evaporator inner cavity 31, be arranged in level-one evaporator inner cavity 31 and and reverse osmosis membrane
The spray head 32 for being used to spray concentrate that pipeline is connected, is arranged in the first steam air intake 33 of evaporator outer wall, and setting exists
The first concentrate outlet 35 of level-one evaporator outer wall, institute is arranged in the first steam gas outlet 34 on evaporator outer wall top
33 one end of the first steam air intake connection evaporator inner cavity is stated, and the connectivity part of the other end is provided with main steam pipe 7, it is described
It is provided on main steam pipe 7 for providing the steam generator of steam to level-one evaporator inner cavity 31.Main steam pipe can be to one
Grade evaporator provides original steam, and level-one evaporator 3 is heated using the three-dimensional overall process of spray, is aloft sprayed down, with small
Molecule or little particle decline, spray process heating surface area is big, can be rapidly heated and add to the filtered concentrate of osmosis filtration film
Heat.The first concentrate connecting pipe 351, the first concentrate connecting pipe are provided on the first concentrate outlet 35
351 one end are connected with level-one evaporator 3, and the other end is connected with second level MVR evaporator 4, and the second level MVR evaporator 4 includes MVR
Inner cavity 41, the injector head 42 for being arranged in the inner cavity MVR 41 and being connected with concentrate connecting tube pipeline are arranged outside MVR evaporator
Second steam air intake 43 of wall, is arranged in the second steam gas outlet 44 on evaporator outer wall top, and setting is evaporated in second level MVR
Second concentrate outlet 45 of device outer wall, described second steam air intake, 43 one end are connected to the inner cavity MVR 41, other end connection master
Steam pipe is additionally provided with Steam Recovery between the evaporator inner cavity of the level-one evaporator and the inner cavity MVR of second level MVR evaporator
Using pipeline 47, and the second steam air intake also pass through while connecting main steam pipe 7 Steam Recovery using pipeline 47 with
First steam gas outlet 44 of level-one evaporator is connected to.
Pipeline is utilized provided with Steam Recovery, it can be by the steam recycling of level-one evaporator 3 to second level MVR evaporator 4
In, play the technical effect of waste heat recycling.The crystallizer 5 includes crystallizer outer wall 51, the crystallization being set in outer wall 51
Room 52, separation concentrated solution tank 53, concentrating return-flow pump 54 and heat exchanger 55, the second of the second level MVR evaporator outer wall are dense
The second concentrate connecting pipe 451, described second concentrate connecting pipe, 451 one end and second level are provided on contracting liquid outlet 45
MVR evaporator 4 is connected, and the other end is connected with crystallisation chamber 52, and the separation concentrated solution tank 53 is positioned adjacent to crystallisation chamber bottom one
Side, concentrating return-flow pump 54 are set to separation concentrated solution tank 53 far from crystallisation chamber side, concentrate flowed out from crystallisation chamber after to
Separation concentrated solution tank 53, then the concentrate being concentrated in flow container is delivered in heat exchanger by concentrating return-flow pump 54, the heat is handed over
55 one end of parallel operation is connected with concentrating return-flow pump 54, and the other end is connected with the second concentrate connecting pipe 451.The heat exchanger 55
Including heating outer wall 551 and heating chamber 552, the heat exchanger heating outer wall is provided with steam pipeline (trace) mouth 553, described
Main steam pipe 7 is connected with steam pipeline (trace) mouth 553, and heats to heat exchanger heating outer wall 551, outside the crystallizer
Third steam air intake 512 is provided on wall 51, the third steam air intake 512 can be steamed with main steam pipe and second respectively
44 pipeline of vapour gas outlet is connected, and second steam gas outlet, 44 one end is connected with 512 pipeline of third steam air intake, the other end
It is connected with 43 pipeline of the second steam air intake.
Heat exchanger 55 in crystallizer needs heat source to go to provide heating function, and utilizes second level MVR evaporator 4 and master
Steam in steam pipe 7 heats come the outer wall 551 to heat exchanger, to can not need to provide the feelings of external heat source
Under condition, heat exchanger is heated using itself extra steam.And flow container 53 is concentrated, concentrating return-flow pump 54 and heat
Exchanger 55 forms a heat cycles, and concentrate is constantly heated, to obtain crystalline solid to the end.The dry dress
Setting 6 includes crystal feed device 61 and crystal drying process device 62, and 52 bottom of crystallisation chamber is provided with crystallization row
Outlet 521, it is described to crystallize the disc type blanking machine 8 for being connected at outlet 521 and crystallization integrate blanking, the disc type
Blanking machine 8 includes the driving motor 82 that blanking plate 81 and driving blanking plate are driven, one end of the blanking plate 81 and knot
Brilliant outlet is connected, and the other end is connected with crystal feed device 61.
The use of drying device 6 can be complete dewatering state in the form of help crystallisation body is finally discharged, and drying device 6
It needs to carry out material transmission between crystallisation chamber 52 just and the dry working condition conversion between crystallization can be achieved, use disc type
Blanking machine 8 can prevent material to be discharged quickly excessively later, be extruded on feed device, thus can not be fast and convenient by object
Material is transferred in drying device, and disc type blanking machine then carries out orderly arrangement to the material in blanking process, allows transfer process
Become more smooth.The crystal feed device 61 includes crystal screw elevator 61, the crystal screw elevator
61 one end are connect with the blanking plate 81 of disc type blanking machine 8, and the other end 61 is connect with crystal drying process device 62, the crystallization
Object drying process device 62 is vacuum rake style drier, including drying chamber 621, is set to the crystallization waste heat layer on drying chamber upper layer
622, it is set to the crystallizing and drying layer 623 in drying chamber middle layer, is set to the crystallizing and drying finished layer 624 of drying chamber lower layer, and
It is disposed through the hot axis 625 for Stirring heat transfer in drying chamber middle layer, the hot axis is driven by hot axis driving motor.Very
The working principle of empty rake type dryer is constantly to carry out heating stirring to material by hot axis 625, is played dry and hydrophobic
Technical effect.The crystallization chamber outer wall bottom is provided with third condensed water discharge outlet, the reverse osmosis multiple-effect of the industry high-salt wastewater
Waste heat evaporative crystallization recovery system further includes condensation water heat exchanger 9, the first condensed water discharge outlet 91, the second condensed water discharge outlet
92 and third condensed water discharge outlet 93 jointly by condensed water guide to condensation water heat exchanger in carry out heat exchange, the condensation
Water heat exchanger 9 includes cooling water inlet and condensed water discharge outlet.So setting can will be at the condensed water of discharge
It manages and is emitted into cooling tower, generate an effective cooling water circulating treatment procedure.
Claims (10)
1. the reverse osmosis waste heat recovery processing system of industrial high-salt wastewater, it is characterised in that: including high-salt wastewater preprocessing module, instead
Permeable membrane processing module, level-one evaporator, second level MVR evaporator, crystallizer and drier, the high-salt wastewater pre-process mould
Block pre-processes industrial high-salt wastewater, and pretreated waste water is transported to reverse osmosis membrane processing module and was carried out
Filter, and filtered concentrate is successively passed through into level-one evaporator and second level MVR evaporator, then from second level MVR evaporator
In obtain high concentration concentrate and enter crystallizer, the crystallization that the ingot in crystallizer is delivered in drier to the end
Body between the level-one evaporator and second level MVR evaporator, is provided with steam and returns between second level MVR evaporator and crystallizer
It receives and utilizes pipeline.
2. the reverse osmosis waste heat recovery processing system of industry high-salt wastewater according to claim 1, it is characterised in that: the height
Salt Wastewater Pretreatment module includes the flocculation sedimentation tank that high-salt wastewater is carried out to flocculation sedimentation first, by the liquid after flocculation sedimentation
The ion exchange resin of body progress sofening treatment.
3. the reverse osmosis waste heat recovery processing system of industry high-salt wastewater according to claim 2, it is characterised in that: described anti-
Permeable membrane processing module includes being used to increase the booster pump of inlet hydraulic with filtering ponds piping connection and connecting with pressurization pump conduit
The reverse osmosis membrane filt connect, the reverse osmosis membrane filt include be arranged in reverse osmosis membrane filt reverse osmosis film and
Pure water discharge outlet, the reverse osmosis membrane filt are connect with level-one evaporator pipeline, and are arranged in the pipeline of connection useful
In the pumping motor for pumping liquid.
4. the reverse osmosis waste heat recovery processing system of industry high-salt wastewater according to claim 3, it is characterised in that: described one
Grade evaporator includes evaporator inner cavity, is arranged in intracavitary in level-one evaporator and is connected with reverse osmosis membrane pipeline dense for spraying
The spray head of contracting liquid is arranged in the first steam air intake of evaporator outer wall, first steam on evaporator outer wall top is arranged in
The first concentrate outlet of level-one evaporator outer wall, the first steam air intake one end connection evaporation is arranged in gas outlet
Device inner cavity, and the connectivity part of the other end is provided with main steam pipe, it is provided on the main steam pipe for being evaporated to level-one
The steam generator of device inner cavity offer steam.
5. industry high-salt wastewater reverse osmosis waste heat recovery processing system according to claim 4, it is characterised in that: described the
The first concentrate connecting pipe is provided on one concentrate outlet, described first concentrate connecting pipe one end and level-one are evaporated
Device is connected, and the other end is connected with second level MVR evaporator, and the second level MVR evaporator includes the inner cavity MVR, is arranged intracavitary in MVR
And the injector head being connected with concentrate connecting tube pipeline, the second steam air intake of MVR evaporator outer wall is set, and setting is being steamed
The second concentrate outlet of MVR evaporator outer wall is arranged in the second steam gas outlet for sending out device outer wall top, and described second steams
Vapour air intake one end is connected to the inner cavity MVR, and the other end is connected to main steam pipe, the evaporator inner cavity of the level-one evaporator and second level
Steam Recovery is additionally provided between the inner cavity MVR of MVR evaporator using pipeline, and the second steam air intake is in connection main steam
Also pass through Steam Recovery while pipe to be connected to using pipeline with the first steam gas outlet of level-one evaporator.
6. the reverse osmosis waste heat recovery processing system of industry high-salt wastewater according to claim 5, it is characterised in that: the knot
Brilliant device includes crystallizer outer wall, and the crystallisation chamber being set in outer wall, separation concentrated solution tank, concentrating return-flow pumps and heat exchanger,
It is provided with the second concentrate connecting pipe on second concentrate outlet of the second level MVR evaporator outer wall, described second is dense
Contracting liquid connecting pipe one end is connected with second level MVR evaporator, and the other end is connected with crystallisation chamber, and the separation concentrated solution tank is set to
Neighbouring crystallisation chamber bottom side, the concentrating return-flow pump are set to separation concentrated solution tank far from crystallisation chamber side, and concentrate is from knot
To separation concentrated solution tank after the outflow of brilliant room, then by concentrating return-flow pump the concentrate being concentrated in flow container is delivered in heat exchanger,
Described heat exchanger one end is connected with concentrating return-flow pump, and the other end is connected with the second concentrate connecting pipe.
7. the reverse osmosis waste heat recovery processing system of industry high-salt wastewater according to claim 6, it is characterised in that: the heat
Exchanger includes heating outer wall and heating chamber, and the heat exchanger heating outer wall is provided with steam pipeline (trace) mouth, the master
Steam pipe is connected with steam pipeline (trace) mouth, and heats to heat exchanger heating outer wall, is arranged on the crystallizer outer wall
Have a third steam air intake, the third steam air intake can respectively with main steam pipe and the second steam gas outlet pipeline phase
Even, second steam gas outlet one end is connected with third steam air intake pipeline, the other end and the second steam air intake pipeline
It is connected.
8. the reverse osmosis waste heat recovery processing system of industry high-salt wastewater according to claim 7, it is characterised in that: described dry
Dry device includes crystal feed device and crystal drying process device, and the crystallisation chamber bottom is provided with crystallization discharge
Mouthful, the disc type blanking machine that crystallization integrate blanking, the disc type blanking machine packet are connected at the crystallization outlet
One end of the driving motor for including blanking plate and blanking plate being driven to be driven, the blanking plate is connected with crystallization outlet, separately
One end is connected with crystal feed device.
9. the reverse osmosis waste heat recovery processing system of industry high-salt wastewater according to claim 8, it is characterised in that: the knot
Brilliant object feed device includes crystal screw elevator, the blanking plate of crystal screw elevator one end and disc type blanking machine
Connection, the other end are connect with crystal drying process device, and the crystal drying process device is vacuum rake style drier, packet
Drying chamber is included, the crystallization waste heat layer on drying chamber upper layer is set to, is set to the crystallizing and drying layer in drying chamber middle layer, is set to drying
The crystallizing and drying finished layer of chamber lower layer, and it is disposed through the hot axis for Stirring heat transfer in drying chamber middle layer, the hot axis
It is driven by hot axis driving motor.
10. the reverse osmosis waste heat recovery processing system of industry high-salt wastewater according to claim 9, it is characterised in that: institute of institute
Stating the reverse osmosis multiple-effect waste heat evaporative crystallization recovery system of industrial high-salt wastewater further includes condensation water heat exchanger, first condensation
Water outlet, the second condensed water discharge outlet and third condensed water discharge outlet jointly guide condensed water to condensation hydrothermal exchange
Heat exchange is carried out in device, the condensation water heat exchanger includes cooling water inlet and condensed water discharge outlet.
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