CN109205902B - Industrial high-salt wastewater reverse osmosis waste heat recovery treatment system - Google Patents
Industrial high-salt wastewater reverse osmosis waste heat recovery treatment system Download PDFInfo
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- CN109205902B CN109205902B CN201811145689.1A CN201811145689A CN109205902B CN 109205902 B CN109205902 B CN 109205902B CN 201811145689 A CN201811145689 A CN 201811145689A CN 109205902 B CN109205902 B CN 109205902B
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- 238000001223 reverse osmosis Methods 0.000 title claims abstract description 60
- 239000002351 wastewater Substances 0.000 title claims abstract description 60
- 239000002918 waste heat Substances 0.000 title claims abstract description 23
- 238000011084 recovery Methods 0.000 title claims abstract description 19
- 238000002425 crystallisation Methods 0.000 claims abstract description 60
- 230000008025 crystallization Effects 0.000 claims abstract description 60
- 239000012528 membrane Substances 0.000 claims abstract description 46
- 239000013078 crystal Substances 0.000 claims abstract description 30
- 238000004064 recycling Methods 0.000 claims abstract description 9
- 238000001914 filtration Methods 0.000 claims abstract description 6
- 239000012141 concentrate Substances 0.000 claims description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 45
- 239000000243 solution Substances 0.000 claims description 39
- 238000001035 drying Methods 0.000 claims description 36
- 238000010438 heat treatment Methods 0.000 claims description 33
- 238000010992 reflux Methods 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 8
- 239000007921 spray Substances 0.000 claims description 8
- 238000001704 evaporation Methods 0.000 claims description 6
- 238000005086 pumping Methods 0.000 claims description 6
- 238000004062 sedimentation Methods 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 5
- 238000005189 flocculation Methods 0.000 claims description 5
- 230000016615 flocculation Effects 0.000 claims description 5
- 238000012546 transfer Methods 0.000 claims description 5
- 238000002347 injection Methods 0.000 claims description 4
- 239000007924 injection Substances 0.000 claims description 4
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- 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
- 238000004891 communication Methods 0.000 claims description 3
- 230000008020 evaporation Effects 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
- 230000000149 penetrating effect Effects 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 3
- 230000003311 flocculating effect Effects 0.000 claims description 2
- 239000007789 gas Substances 0.000 claims 5
- 238000000034 method Methods 0.000 description 14
- 150000003839 salts Chemical class 0.000 description 9
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- -1 Ca2+ Chemical class 0.000 description 2
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 2
- 241000700605 Viruses Species 0.000 description 2
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- 238000006243 chemical reaction Methods 0.000 description 2
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- 229910001385 heavy metal Inorganic materials 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
- 239000011148 porous material Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000008213 purified water Substances 0.000 description 2
- 238000011160 research 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
- 238000004056 waste incineration Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
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- 230000000813 microbial effect Effects 0.000 description 1
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- 239000012452 mother liquor Substances 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 230000035772 mutation Effects 0.000 description 1
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- 238000011197 physicochemical method Methods 0.000 description 1
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- 231100000331 toxic Toxicity 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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to an industrial high-salt wastewater reverse osmosis waste heat recovery treatment system which comprises a high-salt wastewater pretreatment module, a reverse osmosis membrane treatment module, a first-stage evaporator, a second-stage MVR evaporator, a crystallizer and a dryer, wherein the high-salt wastewater pretreatment module is used for pretreating industrial high-salt wastewater, the pretreated wastewater is conveyed to the reverse osmosis membrane treatment module for filtration, filtered concentrated solution sequentially passes through the first-stage evaporator and the second-stage MVR evaporator, then high-concentration concentrated solution is obtained from the second-stage MVR evaporator and enters the crystallizer, a crystallization block in the crystallizer is conveyed to the dryer to obtain final crystals, and vapor recycling pipelines are arranged between the first-stage MVR evaporator and the second-stage MVR evaporator and between the second-stage MVR evaporator and the crystallizer.
Description
Technical Field
The invention relates to the field of sewage treatment, in particular to a system for treating high-salt wastewater by utilizing recovered waste heat and evaporating and crystallizing.
Background
Waste incineration, hazardous waste incineration, metallurgy, petrochemical industry, pharmacy and coal chemical industry produce a large amount of high-salt wastewater in the production process, the salt content is generally more than 20000mg/L, the high-concentration salt substances are very unfavorable to the growth and development and propagation of organisms, the osmotic pressure is high, the salt concentration is high, and the cell plasma separation is caused by the dehydration of microbial cells; salting out to reduce dehydrogenase activity; the chloride ion has high toxic action on bacteria; the salt concentration is high, the density of the wastewater is increased, and the activated sludge is easy to float and run off, so that the normal operation of a biological treatment system is seriously influenced.
The treatment of industrial high-salt wastewater is one of the difficulties and hot spots of domestic and foreign research, and the domestic and foreign research on the high-salt wastewater mainly comprises a biological method and a physical and chemical method. Biological methods exhibit higher organic removal rates when treating high-salt wastewater, but treatment of high-salt wastewater with biological methods generally requires longer acclimation periods, and longer times for acclimating sludge with higher salinity in the wastewater; in addition, microorganisms are sensitive to environmental changes and mutations in salinity often create serious disturbances to the processing system. The physicochemical method mainly comprises an evaporation method, an electrochemical method, an ion exchange method, an adsorption method, a membrane separation technology and the like, and can remove salt and organic matters in the wastewater in certain applications, but generally has higher cost and is easy to cause secondary pollution of the regenerated wastewater.
Disclosure of Invention
The invention aims to solve the defects of the technology and provides a system for treating high-salt wastewater by utilizing recovered waste heat and evaporating and crystallizing.
In order to solve the technical problems, the high-salt wastewater pretreatment device comprises a high-salt wastewater pretreatment module, a reverse osmosis membrane treatment module, a first-stage evaporator, a second-stage MVR evaporator, a crystallizer and a dryer, wherein the high-salt wastewater pretreatment module is used for pretreating industrial high-salt wastewater, the pretreated wastewater is conveyed to the reverse osmosis membrane treatment module for filtration, the filtered concentrated solution sequentially passes through the first-stage evaporator and the second-stage MVR evaporator, then the high-concentration concentrated solution is obtained from the second-stage MVR evaporator and enters the crystallizer, crystals in the crystallizer are conveyed to the dryer to obtain final crystals, and a vapor recycling pipeline is arranged between the first-stage evaporator and the second-stage MVR evaporator and between the second-stage MVR evaporator and the crystallizer.
After the structure is adopted, the high-salt wastewater is pretreated firstly to remove large-particle matters in the wastewater and reduce COD in the water, but bacteria, suspended matters, colloid, mineral matters, salt and the like below 0.1-10um cannot be filtered, so that organic matters and inorganic matters with the size of 0.1-1nm are removed through secondary treatment of a reverse osmosis membrane. The pretreatment ensures the treatment effect and the service life of the reverse osmosis membrane, the wastewater is further concentrated through the reverse osmosis membrane and then is sent to the first-stage evaporator, and the purified water flows into the reuse water system. The steam cooled by the cooling tower is recycled to the evaporator for heating, so that the resources are utilized and the energy consumption is saved. The evaporator secondary steam is used for heating the later stage, so that the use of steam efficiency is solved, and each evaporator is also provided with a main steam pipe for connecting main steam for heating. The vapor compressor may also be used to cyclically heat the secondary MVR evaporator. After entering the crystallizer, the residual concentrated solution is evaporated and crystallized. And discharging the crystals outside the valve, conveying the crystals to a crystallization dryer, and forming crystals after crystallization and drying. The scheme can realize zero discharge of high-salt wastewater.
As a further improvement of the present invention, the high-salt wastewater pretreatment module includes a flocculation precipitation tank that first flocculates and precipitates the high-salt wastewater, and an ion exchange resin that softens the flocculated and precipitated liquid.
After the structure is adopted, negative charges on the surface of the colloid can be destabilized by adding flocculating agents such as PAC, ferric trichloride and the like into a flocculation sedimentation tank, the colloid is captured on nascent micro floccules, meanwhile, the concentration of suspended matters in wastewater is greatly reduced through a sedimentation process, blockage of exchange resin and softening of the exchange resin are avoided, excessive scale cations such as Ca2+, mg2+, ba2+ and Sr2+ possibly contained in raw water need to be softened and pretreated, the scale cations are removed by sodium ion replacement, and the resin is regenerated by brine after being exchanged and saturated, so that the scale problem of a reverse osmosis membrane is reduced.
As a further improvement of the present invention, the reverse osmosis membrane treatment module includes a booster pump connected to a (exchange resin device) pipeline for increasing a feed liquid pressure, and a reverse osmosis membrane filter connected to the booster pump pipeline, the reverse osmosis membrane filter including a reverse osmosis membrane provided at the reverse osmosis membrane filter and a pure water discharge port, the reverse osmosis membrane filter being connected to a primary evaporator pipeline, and a pumping motor for pumping liquid being provided in the connected pipeline.
After the structure is adopted, the pore diameter of the reverse osmosis membrane is as small as nano, and under certain pressure, water molecules can pass through the reverse osmosis membrane, and inorganic salts, heavy metal ions, organic matters, colloid, bacteria, viruses and other impurities in the wastewater can not pass through the reverse osmosis membrane.
As a further improvement of the invention, the primary evaporator comprises an evaporator inner cavity, a spray header which is arranged in the primary evaporator inner cavity and is connected with a reverse osmosis membrane pipeline and used for spraying concentrated solution, a first steam inlet which is arranged on the outer wall of the evaporator, a first steam outlet which is arranged on the upper part of the outer wall of the evaporator, a first concentrated solution outlet which is arranged on the outer wall of the primary evaporator, one end of the first steam inlet is communicated with the evaporator inner cavity, and a main steam pipe is arranged at the communication position of the other end of the first steam inlet, and a steam generator which is used for providing steam for the primary evaporator inner cavity is arranged on the main steam pipe.
After adopting above-mentioned structure, main steam pipe can provide original steam to the one-level evaporimeter, and the one-level evaporimeter uses and sprays three-dimensional overall process heating, sprays downwards in the eminence to small molecule or tiny particle decline, and spray the process heated area is big, can heat up the concentrate rapid heating after the filtration of filter membrane.
As a further improvement of the invention, a first concentrated solution connecting pipeline is arranged on the first concentrated solution outlet, one end of the first concentrated solution connecting pipeline is connected with the first-stage evaporator, the other end of the first concentrated solution connecting pipeline is connected with the second-stage MVR evaporator, the second-stage MVR evaporator comprises an MVR inner cavity, a jet head which is arranged in the MVR inner cavity and is connected with a concentrated solution connecting pipeline, a second steam inlet which is arranged on the outer wall of the MVR evaporator, a second steam outlet which is arranged on the upper part of the outer wall of the evaporator, and a second concentrated solution outlet which is arranged on the outer wall of the second-stage MVR evaporator, wherein one end of the second steam inlet is communicated with the MVR inner cavity, the other end of the second steam inlet is communicated with the main steam pipe, a steam recycling pipeline is further arranged between the evaporator inner cavity of the first-stage evaporator and the MVR inner cavity of the second-stage MVR evaporator, and the second steam inlet is also communicated with the first steam outlet of the first-stage evaporator through the steam recycling pipeline while being connected with the main steam pipe.
After adopting above-mentioned structure, set up vapor recovery and utilized the pipeline, can retrieve the vapor of primary evaporator again to the secondary MVR evaporimeter in, played waste heat recovery's technical effect.
As a further improvement of the invention, the crystallizer comprises an outer wall of the crystallizer, a crystallization chamber arranged in the outer wall, a separation concentrate tank, a concentrate reflux pump and a heat exchanger, wherein a second concentrate connecting pipeline is arranged on a second concentrate discharge outlet of the outer wall of the secondary MVR evaporator, one end of the second concentrate connecting pipeline is connected with the secondary MVR evaporator, the other end of the second concentrate connecting pipeline is connected with the crystallization chamber, the separation concentrate tank is arranged on one side adjacent to the bottom of the crystallization chamber, the concentrate reflux pump is arranged on one side of the separation concentrate tank far away from the crystallization chamber, concentrate flows out from the crystallization chamber to the separation concentrate tank, the concentrate in the concentrate tank is conveyed into the heat exchanger by the concentrate reflux pump, and one end of the heat exchanger is connected with the concentrate reflux pump while the other end is connected with the second concentrate connecting pipeline. The heat exchanger comprises a heating outer wall and a heating cavity, wherein the heating outer wall of the heat exchanger is provided with a heating steam pipeline opening, the main steam pipe is connected with the heating steam pipeline opening and used for heating the heating outer wall of the heat exchanger, a third steam air inlet is formed in the outer wall of the crystallizer and can be respectively connected with the main steam pipe and a second steam air outlet pipeline, one end of the second steam air outlet is connected with the third steam air inlet pipeline, and the other end of the second steam air outlet is connected with the second steam air inlet pipeline.
After the structure is adopted, the heat exchanger in the crystallizer needs a heat source to provide a heating function, and the steam in the secondary MVR evaporator and the main steam pipe is utilized to heat the outer wall of the heat exchanger, so that the heat exchanger can be heated by utilizing redundant steam under the condition that an external heat source is not required to be provided. And the concentrated solution tank, the concentrated reflux pump and the heat exchanger form a heating cycle, and the concentrated solution is continuously heated to obtain the final crystals.
As a further improvement of the invention, the dryer comprises a crystal feeding device and a crystal drying treatment device, the bottom of the crystallization chamber is provided with a crystal discharge port, the crystal discharge port is connected with a disc type blanking machine for integrally blanking crystals, the disc type blanking machine comprises a blanking plate and a driving motor for driving the blanking plate to drive, one end of the blanking plate is connected with the crystal discharge port, and the other end of the blanking plate is connected with the crystal feeding device.
After the structure is adopted, the last discharged form of crystals can be helped to be in a complete dehydration state by using the drier, and the working state conversion between drying and crystallization can be realized by conveying materials between the drier and a crystallization chamber.
As a further improvement of the invention, the crystallizer feeding device comprises a crystallizer spiral lifting machine, one end of the crystallizer spiral lifting machine is connected with a blanking plate of a disc type blanking machine, the other end of the crystallizer spiral lifting machine is connected with a crystallizer drying treatment device, the crystallizer drying treatment device is a vacuum rake dryer and comprises a drying cavity, a crystallization waste heat layer arranged at the upper layer of the drying cavity, a crystallization drying layer arranged at the middle layer of the drying cavity, a crystallization drying finished product layer arranged at the lower layer of the drying cavity and a hot shaft penetrating through the middle layer of the drying cavity and used for stirring and heat transfer, and the hot shaft is driven by a hot shaft driving motor.
After the structure is adopted, the working principle of the vacuum rake dryer is that materials are continuously heated and stirred by a hot shaft, so that the technical effects of drying and dewatering are achieved.
As a further improvement of the invention, the industrial high-salt wastewater reverse osmosis multi-effect waste heat evaporation crystallization recovery system further comprises a condensed water heat exchanger, a first condensed water outlet, a second condensed water outlet and a third condensed water outlet, wherein condensed water is led into the condensed water heat exchanger for heat exchange, and the condensed water heat exchanger comprises a cooling water injection port and a condensed water outlet.
With the above structure, the discharged condensed water can be treated and discharged into the cooling tower, and an effective cooling water circulation treatment process is generated.
Drawings
FIG. 1 is a schematic diagram of an industrial high-salinity wastewater treatment system;
FIG. 2 is a schematic diagram showing a treatment process of the high-salt wastewater pretreatment module;
FIG. 3 is a schematic diagram of a reverse osmosis membrane treatment module;
FIG. 4 is a schematic view of a primary evaporator;
FIG. 5 is a schematic view of the MVR evaporator;
FIG. 6 is a schematic diagram of a structure of a crystallizer;
fig. 7 shows a schematic diagram of a dryer structure.
Detailed Description
As shown in fig. 1, the high-salt wastewater pretreatment device comprises a high-salt wastewater pretreatment module 1, a reverse osmosis membrane treatment module 2, a first-stage evaporator 3, a second-stage MVR evaporator 4, a crystallizer 5 and a dryer 6, wherein the high-salt wastewater pretreatment module 1 pretreats industrial high-salt wastewater, conveys the pretreated wastewater to the reverse osmosis membrane treatment module 2 for filtration, sequentially passes filtered concentrated solution through the first-stage evaporator 3 and the second-stage MVR evaporator 4, then obtains high-concentration concentrated solution from the second-stage MVR evaporator 4, enters the crystallizer 5, conveys crystals in the crystallizer 5 to the dryer to obtain final crystals, and a vapor recycling pipeline is arranged between the first-stage MVR evaporator and the second-stage MVR evaporator and between the second-stage MVR evaporator and the crystallizer. Firstly, the mother solution is pretreated, but bacteria, suspended matters, pigments, colloid, mineral substances and salt below 0.1-10um cannot be filtered out, so that organic matters and inorganic matters with the size of 0.1-1nm can be isolated from entering through secondary treatment of a reverse osmosis membrane. Through pretreatment of wastewater, impurities are reduced during membrane filtration, a reverse osmosis membrane is protected from damage, the service life is prolonged, after the reverse osmosis membrane is used for filtration, mother liquor is further concentrated and sent to the first-stage evaporator 3, and purified water flows into reuse water. The steam cooled by the cooling tower is recycled to the evaporator for heating, so that the energy consumption is saved. The evaporator secondary steam is used for heating the later stage, so that the use of steam efficiency is solved, and each evaporator is also provided with a main steam pipe for connecting main steam for heating. The vapor compressor may also be used to cyclically heat the secondary MVR evaporator. After entering the crystallizer, the residual concentrated solution is evaporated and crystallized. And discharging the crystals outside the valve, conveying the crystals to a crystallization dryer, and finally outputting the crystals through crystallization drying. The scheme can realize zero discharge of high-salt wastewater.
The high-salt wastewater pretreatment module comprises a flocculation sedimentation tank 11 for flocculating and settling the high-salt wastewater, and an ion exchange resin 12 for softening the flocculated and settled liquid. The flocculating agent such as PAC, ferric trichloride and the like is added into the flocculation sedimentation tank to perform destabilization treatment on negative charges on the surface of the colloid, the colloid is captured on nascent micro floccules, and meanwhile, the concentration of suspended matters in wastewater is greatly reduced through the sedimentation process, so that blockage of exchange resin and softening of the exchange resin are avoided: the raw water may contain excessive scaling cations such as ca2+, mg2+, ba2+, sr2+ and the like, and softening pretreatment is required. The scale type cations were removed by sodium ion displacement, and the resin was regenerated with brine after saturation. Thereby reducing the fouling problem of the reverse osmosis membrane. After adopting above-mentioned structure, can reduce the damage to reverse osmosis membrane afterwards to can filter a large amount of impurity in advance, both obtain great guarantee in efficiency and whole life.
The reverse osmosis membrane treatment module 2 comprises a booster pump 21 connected with a filter tank pipeline for increasing the pressure of feed water and a reverse osmosis membrane filter 22 connected with the booster pump pipeline, wherein the reverse osmosis membrane filter 22 comprises a reverse osmosis membrane 221 and a pure water discharge port 222 which are arranged on the reverse osmosis membrane filter, the reverse osmosis membrane filter 22 is connected with the primary evaporator 3 in a pipeline, and a water pumping motor for pumping liquid is arranged in the connected pipeline. The pore diameter of the reverse osmosis membrane is as small as nano, and under a certain pressure, water molecules can pass through the reverse osmosis membrane, and impurities such as inorganic salts, heavy metal ions, organic matters, colloid, bacteria, viruses and the like in source water cannot pass through the reverse osmosis membrane, so that permeable pure water and impermeable concentrated water can be strictly distinguished.
The primary evaporator 3 comprises an evaporator inner cavity 31, a spray header 32 which is arranged in the primary evaporator inner cavity 31 and connected with a reverse osmosis membrane pipeline and used for spraying concentrated solution, a first steam air inlet 33 which is arranged on the outer wall of the evaporator, a first steam air outlet 34 which is arranged on the upper part of the outer wall of the evaporator, a first concentrated solution outlet 35 which is arranged on the outer wall of the primary evaporator, one end of the first steam air inlet 33 is communicated with the evaporator inner cavity, a main steam pipe 7 is arranged at the communication position of the other end, and a steam generator which is used for providing steam for the primary evaporator inner cavity 31 is arranged on the main steam pipe 7. The main steam pipe can provide original steam for the primary evaporator, and the primary evaporator 3 is heated by using a spray three-dimensional whole process, is sprayed downwards at a high position, descends by small molecules or small particles, has a large heating area in the spray process, and can rapidly heat up and heat concentrated solution filtered by the reverse osmosis filter membrane. The first concentrated solution outlet 35 is provided with a first concentrated solution connecting pipeline 351, one end of the first concentrated solution connecting pipeline 351 is connected with the first-stage evaporator 3, the other end of the first concentrated solution connecting pipeline 351 is connected with the second-stage MVR evaporator 4, the second-stage MVR evaporator 4 comprises an MVR inner cavity 41, an ejector 42 which is arranged in the MVR inner cavity 41 and is connected with a concentrated solution connecting pipeline, a second steam inlet 43 which is arranged on the outer wall of the MVR evaporator, a second steam outlet 44 which is arranged on the upper part of the outer wall of the evaporator, a second concentrated solution outlet 45 which is arranged on the outer wall of the second-stage MVR evaporator, one end of the second steam inlet 43 is communicated with the MVR inner cavity 41, the other end of the second steam inlet is communicated with a main steam pipe, a steam recycling pipeline 47 is further arranged between the evaporator inner cavity of the first-stage evaporator and the MVR inner cavity of the second-stage MVR evaporator, and the second steam inlet is also communicated with the first steam outlet 44 of the first-stage evaporator through the steam recycling pipeline 47 while being connected with the main steam pipe 7.
The steam recycling pipeline is arranged, so that the steam of the primary evaporator 3 can be recycled to the secondary MVR evaporator 4, and the technical effect of waste heat recovery is achieved. The crystallizer 5 comprises a crystallizer outer wall 51, a crystallization chamber 52, a separation concentrate tank 53, a concentrate reflux pump 54 and a heat exchanger 55, wherein the crystallization chamber 52 is arranged in the outer wall 51, a second concentrate connecting pipeline 451 is arranged on a second concentrate discharge port 45 of the outer wall of the secondary MVR evaporator, one end of the second concentrate connecting pipeline 451 is connected with the secondary MVR evaporator 4, the other end of the second concentrate connecting pipeline is connected with the crystallization chamber 52, the separation concentrate tank 53 is arranged on one side adjacent to the bottom of the crystallization chamber, the concentrate reflux pump 54 is arranged on one side, far away from the crystallization chamber, of the separation concentrate tank 53, concentrate flows out from the crystallization chamber to the separation concentrate tank 53, the concentrate in the concentrate tank is conveyed to the heat exchanger by the concentrate reflux pump 54, one end of the heat exchanger 55 is connected with the concentrate reflux pump 54, and the other end of the heat exchanger 55 is connected with the second concentrate connecting pipeline 451. The heat exchanger 55 comprises a heating outer wall 551 and a heating cavity 552, the heating outer wall of the heat exchanger is provided with a heating steam pipeline opening 553, the main steam pipe 7 is connected with the heating steam pipeline opening 553 and heats the heating outer wall 551 of the heat exchanger, the outer wall 51 of the crystallizer is provided with a third steam air inlet 512, the third steam air inlet 512 can be respectively connected with a main steam pipe and a second steam air outlet 44 pipeline, one end of the second steam air outlet 44 is connected with the third steam air inlet 512 pipeline, and the other end is connected with the second steam air inlet 43 pipeline.
The heat exchanger 55 in the crystallizer requires a heat source to provide a heating function, and the steam in the secondary MVR evaporator 4 and the main steam pipe 7 is used to heat the outer wall 551 of the heat exchanger, so that the heat exchanger can be heated by the extra steam without providing an external heat source. And the concentrated solution tank 53, the concentrated reflux pump 54 and the heat exchanger 55 form a heating cycle, and the concentrated solution is continuously heated to obtain the final crystal. The dryer 6 comprises a crystal feeding device 61 and a crystal drying treatment device 62, a crystal discharge opening 521 is arranged at the bottom of the crystallization chamber 52, a disc type blanking machine 8 for integrally blanking crystals is connected to the position of the crystal discharge opening 521, the disc type blanking machine 8 comprises a blanking plate 81 and a driving motor 82 for driving the blanking plate to drive, one end of the blanking plate 81 is connected with the crystal discharge opening, and the other end of the blanking plate 81 is connected with the crystal feeding device 61.
The use of the drier 6 can help the last discharged form of crystals to be in a complete dehydration state, and the material transfer between the drier 6 and the crystallization chamber 52 is needed to realize the conversion of the working state between the drying and the crystallization, so that excessive discharge of materials can be prevented at one time after the tray type blanking machine 8 is adopted, the materials are extruded on the feeding device, and therefore, the materials cannot be conveniently and rapidly transferred to the drier, and the tray type blanking machine orderly arranges the materials in the blanking process, so that the transfer process becomes smoother. The crystallization feeding device 61 comprises a crystallization spiral lifting machine 61, one end of the crystallization spiral lifting machine 61 is connected with a blanking plate 81 of the disc type blanking machine 8, the other end 61 is connected with a crystallization drying treatment device 62, the crystallization drying treatment device 62 is a vacuum rake dryer and comprises a drying cavity 621, a crystallization waste heat layer 622 arranged on the upper layer of the drying cavity, a crystallization drying layer 623 arranged on the middle layer of the drying cavity, a crystallization drying finished product layer 624 arranged on the lower layer of the drying cavity and a hot shaft 625 penetrating through the middle layer of the drying cavity and used for stirring and heat transfer, and the hot shaft is driven by a hot shaft driving motor. The working principle of the vacuum rake dryer is that the hot shaft 625 continuously heats and stirs materials, so that the technical effects of drying and dewatering are achieved. The bottom of the outer wall of the crystallization chamber is provided with a third condensate water discharge port, the industrial high-salt wastewater reverse osmosis multi-effect waste heat evaporation crystallization recovery system further comprises a condensate water heat exchanger 9, the first condensate water discharge port 91, the second condensate water discharge port 92 and the third condensate water discharge port 93 guide condensate water to the condensate water heat exchanger for heat exchange, and the condensate water heat exchanger 9 comprises a cooling water injection port and a condensate water discharge port. This arrangement allows the discharged condensate to be treated and discharged to the cooling tower, resulting in an efficient cooling water circulation process.
Claims (10)
1. Industrial high-salt wastewater reverse osmosis waste heat recovery treatment system, which is characterized in that: the high-salt wastewater pretreatment module is used for pretreating industrial high-salt wastewater, the pretreated wastewater is conveyed to the reverse osmosis membrane treatment module for filtering, filtered concentrated solution sequentially passes through the first-stage evaporator and the second-stage MVR evaporator, then high-concentration concentrated solution is obtained from the second-stage MVR evaporator and enters the crystallizer, a crystallization block in the crystallizer is conveyed to the dryer to obtain final crystals, and a vapor recycling pipeline is arranged between the first-stage evaporator and the second-stage MVR evaporator and between the second-stage MVR evaporator and the crystallizer.
2. The industrial high-salt wastewater reverse osmosis waste heat recovery treatment system according to claim 1, wherein: the high-salt wastewater pretreatment module comprises a flocculation sedimentation tank for flocculating and settling high-salt wastewater, and an ion exchange resin for softening the flocculated and settled liquid.
3. The industrial high-salt wastewater reverse osmosis waste heat recovery treatment system according to claim 2, wherein: the reverse osmosis membrane treatment module comprises a booster pump connected with a filter tank pipeline and used for increasing the pressure of inlet liquid and a reverse osmosis membrane filter connected with the booster pump pipeline, wherein the reverse osmosis membrane filter comprises a reverse osmosis membrane and a pure water discharge port, the reverse osmosis membrane filter is connected with a primary evaporator pipeline, and a water pumping motor used for pumping liquid is arranged in the connected pipeline.
4. The industrial high-salt wastewater reverse osmosis waste heat recovery treatment system according to claim 3, wherein: the primary evaporator comprises an evaporator inner cavity, a spray header which is arranged in the primary evaporator inner cavity and connected with a reverse osmosis membrane pipeline and used for spraying concentrated solution, a first steam inlet which is arranged on the outer wall of the evaporator, a first steam outlet which is arranged on the upper part of the outer wall of the evaporator, and a first concentrated solution outlet which is arranged on the outer wall of the primary evaporator, wherein one end of the first steam inlet is communicated with the evaporator inner cavity, and a main steam pipe is arranged at the communication position of the other end of the first steam inlet, and a steam generator which is used for providing steam for the primary evaporator inner cavity is arranged on the main steam pipe.
5. The industrial high-salt wastewater reverse osmosis waste heat recovery treatment system according to claim 4, wherein: the utility model discloses a concentrated solution evaporator, including first concentrated solution discharge port, second concentrated solution discharge port, first concentrated solution connecting tube is last to be provided with first concentrated solution connecting tube, first concentrated solution connecting tube one end links to each other with the one-level evaporimeter, and the other end links to each other with the second grade MVR evaporimeter, the second grade MVR evaporimeter includes the MVR inner chamber, set up at the MVR intracavity and with the continuous injection head of concentrated solution connecting tube pipeline, set up the second steam gas inlet at the outer wall of MVR evaporimeter, set up the second steam gas outlet on the outer wall upper portion of evaporimeter, set up the second concentrated solution discharge port at the outer wall of MVR evaporimeter, second steam gas inlet one end intercommunication MVR inner chamber, the other end intercommunication main steam pipe, still be provided with vapor recycle pipeline between the MVR inner chamber of one-level evaporimeter and the second grade MVR evaporimeter to the second steam gas inlet still communicates with the first steam gas outlet of one-level evaporimeter through vapor recycle pipeline when connecting the main steam pipe.
6. The industrial high-salt wastewater reverse osmosis waste heat recovery treatment system according to claim 5, wherein: the crystallizer comprises an outer wall of the crystallizer, a crystallization chamber arranged in the outer wall, a separation concentrate tank, a concentration reflux pump and a heat exchanger, wherein a second concentrate connecting pipeline is arranged on a second concentrate outlet of the outer wall of the secondary MVR evaporator, one end of the second concentrate connecting pipeline is connected with the secondary MVR evaporator, the other end of the second concentrate connecting pipeline is connected with the crystallization chamber, the separation concentrate tank is arranged on one side adjacent to the bottom of the crystallization chamber, the concentration reflux pump is arranged on one side, far away from the crystallization chamber, of the separation concentrate tank, concentrate flows out from the crystallization chamber and then flows into the separation concentrate tank, the concentration concentrate in the concentrate tank is conveyed into the heat exchanger by the concentration reflux pump, one end of the heat exchanger is connected with the concentration reflux pump, and the other end of the heat exchanger is connected with the second concentrate connecting pipeline.
7. The industrial high-salt wastewater reverse osmosis waste heat recovery treatment system according to claim 6, wherein: the heat exchanger comprises a heating outer wall and a heating cavity, wherein the heating outer wall of the heat exchanger is provided with a heating steam pipeline opening, the main steam pipe is connected with the heating steam pipeline opening and used for heating the heating outer wall of the heat exchanger, a third steam air inlet is formed in the outer wall of the crystallizer and can be respectively connected with the main steam pipe and a second steam air outlet pipeline, one end of the second steam air outlet is connected with the third steam air inlet pipeline, and the other end of the second steam air outlet is connected with the second steam air inlet pipeline.
8. The industrial high-salt wastewater reverse osmosis waste heat recovery treatment system according to claim 7, wherein: the dryer comprises a crystallization feeding device and a crystallization drying treatment device, a crystallization outlet is formed in the bottom of the crystallization chamber, a disc type blanking machine for integrating and blanking crystallization is connected to the crystallization outlet, the disc type blanking machine comprises a blanking plate and a driving motor for driving the blanking plate to drive, one end of the blanking plate is connected with the crystallization outlet, and the other end of the blanking plate is connected with the crystallization feeding device.
9. The industrial high-salt wastewater reverse osmosis waste heat recovery treatment system according to claim 8, wherein: the crystallization feeding device comprises a crystallization spiral lifting machine, one end of the crystallization spiral lifting machine is connected with a blanking plate of a disc type blanking machine, the other end of the crystallization spiral lifting machine is connected with a crystallization drying treatment device, the crystallization drying treatment device is a vacuum rake dryer and comprises a drying cavity, a crystallization waste heat layer arranged on the upper layer of the drying cavity, a crystallization drying layer arranged on the middle layer of the drying cavity, a crystallization drying finished product layer arranged on the lower layer of the drying cavity and a hot shaft penetrating through the middle layer of the drying cavity and used for stirring and heat transfer, and the hot shaft is driven by a hot shaft driving motor.
10. The industrial high-salt wastewater reverse osmosis waste heat recovery treatment system according to claim 9, wherein: the industrial high-salt wastewater reverse osmosis multi-effect waste heat evaporation crystallization recovery system further comprises a condensate water heat exchanger, a first condensate water outlet, a second condensate water outlet and a third condensate water outlet, wherein the condensate water is guided into the condensate water heat exchanger for heat exchange through the three condensate water outlets, and the condensate water heat exchanger comprises a cooling water injection port and a condensate water outlet.
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| CN113800704B (en) * | 2021-11-17 | 2022-02-22 | 浙江晟格生物科技有限公司 | Ion exchange resin regeneration activation wastewater distillation concentration treatment method |
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