CN209276303U - Coal water slurry gasification waste water divides salt to crystallize zero-discharge treatment system - Google Patents
Coal water slurry gasification waste water divides salt to crystallize zero-discharge treatment system Download PDFInfo
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- CN209276303U CN209276303U CN201822037294.1U CN201822037294U CN209276303U CN 209276303 U CN209276303 U CN 209276303U CN 201822037294 U CN201822037294 U CN 201822037294U CN 209276303 U CN209276303 U CN 209276303U
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 260
- 150000003839 salts Chemical class 0.000 title claims abstract description 180
- 239000002002 slurry Substances 0.000 title claims abstract description 80
- 239000002351 wastewater Substances 0.000 title claims abstract description 76
- 238000002309 gasification Methods 0.000 title claims abstract description 43
- 239000003245 coal Substances 0.000 title claims abstract description 41
- 208000028659 discharge Diseases 0.000 title claims abstract description 21
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 137
- 238000001728 nano-filtration Methods 0.000 claims abstract description 102
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 86
- 239000013078 crystal Substances 0.000 claims abstract description 59
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 58
- 239000011780 sodium chloride Substances 0.000 claims abstract description 43
- 239000000126 substance Substances 0.000 claims abstract description 37
- 229910052938 sodium sulfate Inorganic materials 0.000 claims abstract description 27
- 235000011152 sodium sulphate Nutrition 0.000 claims abstract description 27
- 239000012452 mother liquor Substances 0.000 claims description 93
- 238000001704 evaporation Methods 0.000 claims description 64
- 230000008020 evaporation Effects 0.000 claims description 64
- 239000007788 liquid Substances 0.000 claims description 46
- 239000007787 solid Substances 0.000 claims description 41
- 238000001764 infiltration Methods 0.000 claims description 40
- 238000004519 manufacturing process Methods 0.000 claims description 37
- 230000008676 import Effects 0.000 claims description 33
- 238000001035 drying Methods 0.000 claims description 27
- PALNZFJYSCMLBK-UHFFFAOYSA-K magnesium;potassium;trichloride;hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[Cl-].[Cl-].[Cl-].[K+] PALNZFJYSCMLBK-UHFFFAOYSA-K 0.000 claims description 26
- 238000007710 freezing Methods 0.000 claims description 25
- 230000008014 freezing Effects 0.000 claims description 25
- 238000000926 separation method Methods 0.000 claims description 23
- 239000000463 material Substances 0.000 claims description 22
- 230000003647 oxidation Effects 0.000 claims description 18
- 238000007254 oxidation reaction Methods 0.000 claims description 18
- 238000001953 recrystallisation Methods 0.000 claims description 18
- 238000005342 ion exchange Methods 0.000 claims description 13
- 238000007599 discharging Methods 0.000 claims description 9
- 238000000108 ultra-filtration Methods 0.000 claims description 8
- 238000005096 rolling process Methods 0.000 claims description 7
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 239000002699 waste material Substances 0.000 claims description 3
- 238000012545 processing Methods 0.000 abstract description 31
- 238000011084 recovery Methods 0.000 abstract description 11
- 238000001914 filtration Methods 0.000 abstract description 9
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000002156 mixing Methods 0.000 abstract description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 26
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 14
- 238000002425 crystallisation Methods 0.000 description 14
- 230000008025 crystallization Effects 0.000 description 14
- 239000000377 silicon dioxide Substances 0.000 description 13
- 229910052681 coesite Inorganic materials 0.000 description 12
- 229910052906 cristobalite Inorganic materials 0.000 description 12
- 229910052682 stishovite Inorganic materials 0.000 description 12
- 229910052905 tridymite Inorganic materials 0.000 description 12
- 238000000034 method Methods 0.000 description 11
- 239000005416 organic matter Substances 0.000 description 10
- 239000000243 solution Substances 0.000 description 10
- 238000010025 steaming Methods 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 239000006227 byproduct Substances 0.000 description 6
- 238000005261 decarburization Methods 0.000 description 6
- 230000018044 dehydration Effects 0.000 description 6
- 238000006297 dehydration reaction Methods 0.000 description 6
- 229910052710 silicon Inorganic materials 0.000 description 6
- 239000010703 silicon Substances 0.000 description 6
- 239000010802 sludge Substances 0.000 description 6
- 230000008859 change Effects 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 239000003250 coal slurry Substances 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 4
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 230000003750 conditioning effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000008018 melting Effects 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
- 238000005457 optimization Methods 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 239000012047 saturated solution Substances 0.000 description 3
- 235000012239 silicon dioxide Nutrition 0.000 description 3
- PANBYUAFMMOFOV-UHFFFAOYSA-N sodium;sulfuric acid Chemical compound [Na].OS(O)(=O)=O PANBYUAFMMOFOV-UHFFFAOYSA-N 0.000 description 3
- 239000003643 water by type Substances 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 239000002957 persistent organic pollutant Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 1
- 241001282153 Scopelogadus mizolepis Species 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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Abstract
The utility model discloses a kind of coal water slurry gasification waste water, and salt to be divided to crystallize zero-discharge treatment system comprising pretreatment system divides salt system, sodium chloride crystal system and salt crystal system.The utility model has the advantage of, on the basis of meeting system service requirement, it simplifies traditional coal-water-slurry gasification waste water and setting chemical tendering, filtering, membranous system is repeated using the processing of high slat-containing wastewater processing system, the system of reducing invests to build expense, reduces the energy consumption of pretreatment system；A point salt system is optimized, carries out second level nanofiltration after mixing in proportion using reverse osmosis produced water with a nanofiltration concentrated water again, the operating pressure of second level nanofiltration is reduced, improves the second level nanofiltration rate of recovery, extend service life of equipment；Crystal system is optimized, the rate of recovery and purity of sodium chloride and sodium sulphate are improved.
Description
Technical field:
The utility model relates to coal gasification field, in particular to a kind of coal water slurry gasification waste water divides salt to crystallize zero discharge treatment
System.
Background technique:
Coal water slurry gasification technology is a kind of Coal Gasification Technology using water-coal-slurry as coal gasification raw material, due to coal water slurry gasification skill
The reaction temperature and pressure of art are higher, and the effective component in water-coal-slurry may be implemented to convert completely in gasification furnace, and water-coal-slurry
Middle carrying, the organic matter, pollutant and the solid impurity that are generated in gasification enter in coal water slurry gasification waste water, water-coal-slurry gas
Change waste water after Treatment for Reuse can circulating and recovering, the rate of recovery is up to 80%；And 20% other coal water slurry gasification is useless
In water, not only salt content is high, while the comparison of ingredients of pollutant is complicated, and organic pollutant category is more, concentration is high and most toxicity
It is relatively strong, belong to the middle and high concentration organic wastewater of difficult for biological degradation.
Currently, generally handle with the following method for this part coal water slurry gasification waste water: 1, directly sending sewage
Treatment plant's processing, but since environmental requirement in recent years is further stringent, sewage treatment plant's treatment scale constantly reduces, and can not dissolve big
Scale wastewater has seriously affected the development of coal chemical industry；2, direct evaporation drying, after coal water slurry gasification waste water evaporation drying
Generate carnallite, carnallite not only complicated component, and also it is soluble, the pollutant leakage accident that is easy to happen is stacked for a long time, it is serious dirty
Environment is contaminated, current environmental requirement is not met；3, coal water slurry gasification wastewater treatment is carried out using high slat-containing wastewater processing system, such as schemed
Shown in 1, there are the following problems: 1) coal water slurry gasification waste water successively being carried out to Treated sewage reusing processing, concentrate processing and divided at salt
Reason, Treated sewage reusing processing system are generally arranged chemical tendering, filtering, membranous system, concentrate processing system be generally arranged chemical tendering,
Filtering, membranous system, ion exchange softening, it is soft that a point salt treatment system of building on the basis of concentrate processing system also needs to be arranged chemistry
Change, advanced oxidation, divides salt, evaporative crystallization at filtering；It follows that handling coal water slurry gasification using high slat-containing wastewater processing system
Waste water, need repeat be arranged chemical tendering, filtering, membranous system, cause existing high slat-containing wastewater processing system invest to build it is at high cost,
Energy consumption is high；2) existing high slat-containing wastewater processing system divides the salt system to carry out level-one nanofiltration to concentrate treated waste water, and one
Grade nanofiltration concentrated water carries out second level nanofiltration again, and second level nanofiltration operating pressure is larger, leads to the reduction of the second level nanofiltration rate of recovery, and equipment uses
Service life is short；The production water of second level nanofiltration carries out salt separating treatment, and the concentrated water of second level nanofiltration carries out after advanced oxidation removes organic matter
Saltcake separation evaporates separation mother liquor to salt and carries out saltcake recycling, to improve the saltcake rate of recovery, but do not pay close attention to by-product sulfate crystal
In purity salt, various evaporations and freezing mother liquor the problem of salinity recycling, lead to that by-product sulfate crystal purity salt is low, TOC high, it is miscellaneous
Salt yield is high, and the raising of carnallite yield necessarily causes carnallite processing cost high, increases burden to coal chemical industry enterprises.
Utility model content:
At low cost, carnallite low output, by-product crystal salt purity is high are invested to build the purpose of this utility model is to provide a kind of
Coal water slurry gasification waste water divides salt to crystallize zero-discharge treatment system.
The purpose of this utility model is implemented by following technical solution: coal water slurry gasification waste water divides salt to crystallize zero discharge treatment system
System comprising pretreatment system divides salt system, sodium chloride crystal system and salt crystal system, and the ion of the pretreatment system is handed over
The water outlet of exchange device is connect with the water inlet of the primary reverse osmosis system of described point of salt system, and the second level of described point of salt system is received
The concentrated water outlet of filter system is connect with the water inlet of the saltcake Multi-effect evaporation crystallizer of the sodium chloride crystal system, described to divide salt system
The concentrated water outlet of the three-level counter-infiltration system of system is connect with the import of the salt Multi-effect evaporation crystallizer of the salt crystal system, described
The mother liquor outlet of saltcake Multi-effect evaporation crystallizer, the salt Multi-effect evaporation crystallizer mother liquor outlet respectively with mother liquor freezing and crystallizing
The import of device connects, and the slurry outlet of the mother liquor freezing and crystallizing device is connect with the import of liquid separation centrifuge, the liquid separation centrifugation
The solids outlet of machine is connect with the material inlet of the saltcake dissolving tank of the sodium chloride crystal system；The mother liquor freezing and crystallizing device
Mother liquor outlet connect with the import of the first mother liquid evaporation device of the salt crystal system, the slurry of the first mother liquid evaporation device
Outlet is connect with the import of mother liquor centrifuge, the solid outlet of the mother liquor centrifuge and the salt Multi-effect evaporation crystallizer into
Mouth connection, the mother liquor outlet of the first mother liquid evaporation device are connect with the import of the carnallite drier.
Further, the pretreatment system includes chemical tendering equipment, filter plant and the ion-exchange unit, institute
The water inlet for stating chemical tendering equipment is connect with coal water slurry gasification waste line, the water outlet of the chemical tendering equipment with it is described
The water inlet of filter plant connects, and the water outlet of the filter plant is connect with the water inlet of the ion-exchange unit；It is described
Mud scraper is equipped in chemical tendering equipment, the mud discharging mouth of the chemical tendering equipment and the feed inlet of filter press connect.
Further, the filter plant includes V-type filter tank and ultrafiltration apparatus, the water outlet in the V-type filter tank with it is described
The water inlet of ultrafiltration apparatus connects.
Further, described point of salt system includes the primary reverse osmosis system, reuse pool, decarbonizer, second level reverse osmosis
Permeable system, advanced oxidation system, level-one nanofiltration system, the second level nanofiltration system, nanofiltration produce pond, the reverse osmosis system of the three-level
System and level Four counter-infiltration system, the production water out of the primary reverse osmosis system are connect with the water inlet of the reuse pool, institute
The concentrated water outlet for stating primary reverse osmosis system is connect with the water inlet of the decarbonizer, the water outlet of the decarbonizer and described two
The water inlet connection of grade counter-infiltration system；The water inlet company for producing water out and the reuse pool of the two-stage reverse osmosis system
It connects, the concentrated water outlet of the two-stage reverse osmosis system is connect with the water inlet of the advanced oxidation system；The advanced oxidation system
The water outlet of system is connect with the water inlet of the level-one nanofiltration system, the production water out of the level-one nanofiltration system and the nanofiltration
The water inlet connection in pond is produced, the concentrated water outlet of the level-one nanofiltration system is connect with the water inlet of the second level nanofiltration system,
The water inlet of the second level nanofiltration system also passes through regulating valve and connect with the water outlet of the reuse pool；Second level nanofiltration system
The production water out of system is connect with the water inlet that the nanofiltration produces pond；The nanofiltration produces the water outlet and the three-level reverse osmosis in pond
The water inlet of permeable system connects, the water inlet company for producing water out and the level Four counter-infiltration system of the three-level counter-infiltration system
It connects；The production water out of the level Four counter-infiltration system is connect with the water inlet of the reuse pool, the level Four counter-infiltration system
Concentrated water outlet with the nanofiltration production pond water inlet connect；The three-level counter-infiltration system be disc tube reverse osmosis (dt-ro) system,
Any one in electric drive membranous system or rolling counter-infiltration system, the level Four counter-infiltration system are disc tube reverse osmosis (dt-ro) system
Or any one in rolling counter-infiltration system.
Further, the sodium chloride crystal system includes the saltcake Multi-effect evaporation crystallizer, the saltcake dissolving tank, awns
Nitre recrystallizes evaporator, saltcake centrifuge and saltcake drying machine, the slurry outlet of the saltcake Multi-effect evaporation crystallizer with it is described
The import of liquid separation centrifuge connects, the material inlet of the material outlet of the saltcake dissolving tank and saltcake recrystallization evaporator
The material outlet of connection, saltcake recrystallization evaporator is connect with the material inlet of the saltcake centrifuge, the saltcake from
The solids outlet of scheming is connect with the feed inlet of the saltcake drying machine, and the discharge port and sodium sulphate of the saltcake drying machine store up
The import in storehouse connects.
Further, the salt crystal system includes the salt Multi-effect evaporation crystallizer, salt centrifuge, salt drying machine, institute
The solids outlet stated is connect with the material inlet of the salt centrifuge, and the solids outlet of the salt centrifuge and the salt are dry
The feed inlet of dry machine connects, and the discharge port of the salt drying machine is connect with the import of sodium chloride warehouse.
Further, further include having the second mother liquid evaporation device, the mother liquor outlet of the first mother liquid evaporation device with it is described
The import of second mother liquid evaporation device connects, and the import of the slurry outlet of the second mother liquid evaporation device and the carnallite drier connects
It connects.
The advantages of the utility model: 1, meet system service requirement on the basis of, it is useless to simplify traditional coal-water-slurry gasification
Water repeats setting chemical tendering, filtering, membranous system using the processing of high slat-containing wastewater processing system, and the system of reducing invests to build expense,
Reduce the energy consumption of pretreatment system.2, a point salt system is optimized, firstly, utilizing counter-infiltration system concentration, advanced oxidation system
Organic matter is removed, so that the water into nanofiltration system is met nanofiltration water inlet and requires；Secondly, dense using reverse osmosis produced water and a nanofiltration
Water carries out second level nanofiltration again after mixing in proportion, reduce the operating pressure of second level nanofiltration, improve the second level nanofiltration rate of recovery, extends
Service life of equipment.3, crystal system is optimized, sodium chloride crystal processing is carried out to the concentrated water that second level nanofiltration generates, second level is received
The production water that filter generates carries out salt crystallization treatment after reverse osmosis concentration, firstly, in sodium chloride crystal treatment process, by saltcake multiple-effect
The sodium sulphate that crystallizing evaporator generates carries out heavy molten, recrystallization, and obtains sulfate crystal salt again by evaporative crystallization, improves
The purity of sulfate crystal salt；Secondly, carrying out further evaporative crystallization for the mother liquor that freezing and crystallizing device generates, obtain
Solids is back in salt Multi-effect evaporation crystallizer and recrystallizes, and has recycled the sodium chloride in mother liquor, improves sodium chloride crystallization
The rate of recovery and purity of salt；Third, the mother liquor generated for salt Multi-effect evaporation crystallizer, saltcake Multi-effect evaporation crystallizer convey
Freezing and crystallizing is carried out in freezing and crystallizing device, obtained sal glauberi is delivered to the molten step of weight of sulfate crystal treatment process
Suddenly, heavy molten, recrystallization is carried out, the rate of recovery and purity of sodium sulphate are improved.
Detailed description of the invention:
In order to illustrate the embodiment of the utility model or the technical proposal in the existing technology more clearly, below will be to embodiment
Or attached drawing needed to be used in the description of the prior art is briefly described, it should be apparent that, the accompanying drawings in the following description is only
It is some embodiments of the utility model, for those of ordinary skill in the art, in the premise not made the creative labor
Under, it is also possible to obtain other drawings based on these drawings.
Fig. 1 is Conventional waste water Zero discharging system connection schematic diagram.
Fig. 2 is the integrated connection schematic diagram of embodiment 1.
Fig. 3 is that coal water slurry gasification waste water divides salt to crystallize Zero discharge treatment method flow chart.
Chemical tendering equipment 1, V-type filter tank 2, ultrafiltration apparatus 3, ion-exchange unit 4, primary reverse osmosis system 5, decarbonizer
6, reuse pool 7, two-stage reverse osmosis system 8, advanced oxidation system 9, level-one nanofiltration system 10, second level nanofiltration system 11, nanofiltration
Production pond 12, three-level counter-infiltration system 13, level Four counter-infiltration system 14, saltcake Multi-effect evaporation crystallizer 15, saltcake dissolving tank 16,
Saltcake recrystallization evaporator 17, saltcake centrifuge 18, saltcake drying machine 19, liquid separation centrifuge 20, salt Multi-effect evaporation crystallizer 21,
Salt centrifuge 22, salt drying machine 23, mother liquor freezing and crystallizing device 24, the first mother liquid evaporation device 25, the second mother liquid evaporation device 26, carnallite
Drier 27, filter press 28, regulating valve 29, mother liquor centrifuge 30.
Specific embodiment:
The following will be combined with the drawings in the embodiments of the present invention, carries out the technical scheme in the embodiment of the utility model
Clearly and completely describe, it is clear that the described embodiments are only a part of the embodiments of the utility model, rather than whole
Embodiment.Based on the embodiments of the present invention, those of ordinary skill in the art are without creative efforts
Every other embodiment obtained, fall within the protection scope of the utility model.
Embodiment 1:
As shown in Fig. 2, coal water slurry gasification waste water divides salt to crystallize zero-discharge treatment system comprising pretreatment system divides salt
System, sodium chloride crystal system and salt crystal system；
Pretreatment system can remove in waste water most total hardness, total alkalinity, heavy metal ion and suspended matter and
Part of silica, fluorine ion and organic matter, to ensure the normal table operation of follow-up system；Pretreatment system includes that chemistry is soft
Change equipment 1, filter plant and ion-exchange unit 4, the water inlet and coal water slurry gasification waste line of chemical tendering equipment 1 connect
It connects, the water outlet of chemical tendering equipment 1 and the water inlet of filter plant connect, and filter plant includes V-type filter tank 2 and ultrafiltration apparatus
3, the water outlet in V-type filter tank 2 is connect with the water inlet of ultrafiltration apparatus 3, the water outlet of filter plant and ion-exchange unit 4 into
Mouth of a river connection；Mud scraper is equipped in chemical tendering equipment 1, the mud discharging mouth of chemical tendering equipment 1 and the feed inlet of filter press 28 connect
It connects.
The water inlet of the water outlet of the ion-exchange unit 4 of pretreatment system and the primary reverse osmosis system 5 for dividing salt system
Connection, a point salt system includes primary reverse osmosis system 5, reuse pool 7, decarbonizer 6, two-stage reverse osmosis system 8, advanced oxidation
System 9, level-one nanofiltration system 10, second level nanofiltration system 11, nanofiltration production pond 12, three-level counter-infiltration system 13 and level Four are reverse osmosis
System 14, three-level counter-infiltration system 13 are appointing in disc tube reverse osmosis (dt-ro) system, electric drive membranous system or rolling counter-infiltration system
It anticipates one kind, in the present embodiment, reverse osmosis three-level is disc tube reverse osmosis (dt-ro) system；Level Four counter-infiltration system 14 is dish tubular type reverse osmosis
Any one in permeable system or rolling counter-infiltration system, in the present embodiment, reverse osmosis level Four is rolling counter-infiltration system；One
The production water out of grade counter-infiltration system 5 is connect with the water inlet of reuse pool 7, and the concentrated water of primary reverse osmosis system 5 is exported and taken off
The water inlet of carbon device 6 connects, and the water outlet of decarbonizer 6 is connect with the water inlet of two-stage reverse osmosis system 8；Two-stage reverse osmosis system
8 production water out is connect with the water inlet of reuse pool 7, concentrated water outlet and the advanced oxidation system 9 of two-stage reverse osmosis system 8
Water inlet connection；The water outlet of advanced oxidation system 9 is connect with the water inlet of level-one nanofiltration system 10, level-one nanofiltration system 10
It produces water out and is connect with the water inlet that nanofiltration produces pond 12, concentrated water outlet and the second level nanofiltration system 11 of level-one nanofiltration system 10
Water inlet connection, the water inlet of second level nanofiltration system 11 also pass through regulating valve 29 and connect with the water outlet of reuse pool 7；Second level is received
The production water out of filter system 11 is connect with the water inlet that nanofiltration produces pond 12；The water outlet and three-level in nanofiltration production pond 12 are reverse osmosis
The water inlet of system 13 connects, and the production water out of three-level counter-infiltration system 13 is connect with the water inlet of level Four counter-infiltration system 14；
The production water out of level Four counter-infiltration system 14 is connect with the water inlet of reuse pool 7, the concentrated water outlet of level Four counter-infiltration system 14
The water inlet for producing pond 12 with nanofiltration is connect.
Divide the saltcake Multi-effect evaporation crystallizer of the concentrated water outlet and sodium chloride crystal system of the second level nanofiltration system 11 of salt system
15 water inlet connection, sodium chloride crystal system include saltcake Multi-effect evaporation crystallizer 15, saltcake dissolving tank 16, saltcake recrystallization steaming
Device 17, saltcake centrifuge 18 and saltcake drying machine 19 are sent out, it can be Multi-effect evaporation crystallizer or Shen that saltcake, which recrystallizes evaporator 17,
Number evaporator please be recrystallized for saltcake disclosed in CN201720046981.2 Chinese patent, in the present embodiment, saltcake recrystallization
Evaporator 17 can be Multi-effect evaporation crystallizer.The slurry outlet of saltcake Multi-effect evaporation crystallizer 15 and liquid separation centrifuge 20 into
The material outlet of mouth connection, saltcake dissolving tank 16 is connect with the material inlet of saltcake recrystallization evaporator 17, and saltcake recrystallization steams
The material outlet of hair device 17 is connect with the material inlet of saltcake centrifuge 18, the solids outlet of saltcake centrifuge 18 and saltcake
The feed inlet of drying machine 19 connects, and the discharge port of saltcake drying machine 19 is connect with the import of sodium sulphate warehouse.
Divide the salt Multi-effect evaporation crystallizer 21 of the concentrated water outlet and salt crystal system of the three-level counter-infiltration system 13 of salt system
Import connection, salt crystal system includes salt Multi-effect evaporation crystallizer 21, salt centrifuge 22, salt drying machine 23, solids go out
Mouth is connect with the material inlet of salt centrifuge 22, and the solids outlet of salt centrifuge 22 is connect with the feed inlet of salt drying machine 23,
The discharge port of salt drying machine 23 is connect with the import of sodium chloride warehouse.
The mother liquor outlet of saltcake Multi-effect evaporation crystallizer 15, salt Multi-effect evaporation crystallizer 21 mother liquor outlet respectively with mother liquor
The import of freezing and crystallizing device 24 connects, and the slurry outlet of mother liquor freezing and crystallizing device 24 is connect with the import of liquid separation centrifuge 20, point
The solids outlet of liquid centrifuge 20 is connect with the material inlet of the saltcake dissolving tank 16 of sodium chloride crystal system；Mother liquor freezing and crystallizing
The mother liquor outlet of device 24 is connect with the import of the first mother liquid evaporation device 25 of salt crystal system, the slurry of the first mother liquid evaporation device 25
Material outlet is connect with the import of mother liquor centrifuge 30, solid outlet and the salt Multi-effect evaporation crystallizer 21 of mother liquor centrifuge 30
Import connection, the mother liquor outlet of the first mother liquid evaporation device 25 are connect with the import of the second mother liquid evaporation device 26, the second mother liquid evaporation
The slurry outlet of device 26 is connect with the import of carnallite drier 27.
Compared with Conventional waste water Zero discharging system (as shown in Figure 1), embodiment 1 is distinguished with it to be, eliminates V-type filter tank
2 and ultrafiltration apparatus 3 setting repeatedly, eliminate the softening of subsequent two-stage except computer hardware, calculated according to existing market price, this reality
The expense of investing to build for applying example reduces by 25,000,000 yuan/set than Conventional waste water Zero discharging system, and maintenance of equipment and renewal cost can drop every year
Low 450,000 yuan.
Embodiment 2:
Salt is divided to crystallize Zero discharge treatment method using the coal water slurry gasification waste water that embodiment 1 carries out, as shown in figure 3, it is wrapped
Include following steps:
S1. pre-process: coal water slurry gasification waste water is carried out into pretreatment system except hard drop after conditioning tank homogeneous average
It is turbid, except silicon, pH adjust, removal organic matter processing, it is specific as follows:
A1. chemical tendering: coal water slurry gasification waste water be delivered to chemical tendering equipment 1 carry out except drop firmly it is turbid, except silicon, removal have
The processing of machine object, obtains chemical tendering water, and the index of chemical tendering water is Ca2+≤50.00mg/l、Mg2+≤50.00mg/l、
SiO2≤ 15.00mg/l, turbidity≤20NTU；Obtained sludge is delivered to the dehydration of filter press 28, obtains dewatered sludge；
A2. it filters: being delivered to after chemical tendering water tune pH to 7 in filtration system and drop turbid, be obtained drainage, cross drainage
Turbidity≤1NTU；
A3. depth softens: crossing drainage and is delivered to progress depth softening in ion-exchange unit 4, arrives pretreated waste water；
Pretreated waste water is obtained, the index of pretreated waste water is Ca2+=0mg/l, Mg2+=0mg/l, SiO2≤
15.00mg/l, turbidity≤1NTU, pH 7；
S2. divide salt: pretreated waste water is delivered to primary reverse osmosis system 5 and is concentrated, and obtains a concentrated water；Concentrated water
It after tune pH is 4, is delivered in decarbonizer 6 and removes removing carbon dioxide, obtain decarburization water outlet；Decarburization water outlet is delivered to two-pass reverse osmosis system
System 8 is concentrated, and secondary concentrated water is obtained；Secondary concentrated water is delivered to the removal that advanced oxidation system 9 carries out organic matter, is aoxidized
Waste water；Primary reverse osmosis system 5, two-stage reverse osmosis system 8 production water be delivered in reuse pool 7, as recycle-water；Oxidation
Waste water is delivered to the once point salt treatment of level-one nanofiltration system 10, obtains a nanofiltration concentrated water；Nanofiltration concentrated water and reuse
Water is delivered to second level nanofiltration system 11 according to the ratio that volume ratio is 4:3 and carries out secondary point of salt treatment, and it is dense to obtain secondary nanofiltration
Water；Nanofiltration produces water, secondary nanofiltration produces water and is delivered in nanofiltration production pond 12, as salt waste water to be gone out；Salt waste water to be gone out
It is delivered to three-level counter-infiltration system 13 to be concentrated, obtains concentrated water three times and produces water three times；Water is produced three times is delivered to level Four reverse osmosis
Permeable system 14 is handled, and is obtained four production water and is delivered to reuse pool 7, is obtained four concentrated waters and is delivered to nanofiltration production pond 12,
It obtains four production water and is delivered to reuse pool 7；
S3. the output of sodium chloride: concentrated water is delivered to salt Multi-effect evaporation crystallizer 21 and is evaporated crystallization three times, obtains salt slurry
Material and salt mother liquor；Salt slurry is delivered in salt centrifuge 22 and is separated by solid-liquid separation, and obtains solid sodium chloride；Solid sodium chloride conveying
Being dried in salt drying machine 23 to water content is 0.1%, obtains sodium chloride crystal salt, the purity of sodium chloride crystal salt is
98.5%；
S4. the output of sodium sulphate: secondary nanofiltration concentrated water is delivered to saltcake Multi-effect evaporation crystallizer 15 and is evaporated crystallization,
Obtain saltcake slurry and saltcake mother liquor；Saltcake slurry is separated by solid-liquid separation, and solid sodium sulfate is obtained；Solid sodium sulfate is delivered to awns
It is molten that nitre dissolving tank 16 carries out weight, until solution in saltcake dissolving tank 16 is sodium sulphate saturated solution, obtains weight solution；Weight solution is defeated
It send to saltcake and recrystallizes evaporator 17, obtain recrystallization slurry；Recrystallization slurry is delivered to saltcake centrifuge 18 and carries out solid-liquid point
From obtaining solid sodium sulfate；It is 0.3% that solid sodium sulfate, which is delivered in saltcake drying machine 19 and dries to water content, obtains sulfuric acid
Sodium crystal salt, the TOC of sulfate crystal salt is 37mg/KG, purity 97%；
S5. the processing of mother liquor: salt mother liquor, saltcake mother liquor, which are delivered in mother liquor freezing and crystallizing device 24, carries out freezing and crystallizing,
COD≤18000mg/L of salt mother liquor, SiO2≤ 4000mg/l, COD≤30000mg/L of saltcake mother liquor, SiO2≤ 5000mg/l,
Obtain mother liquor slurry and freezing mother liquor；Mother liquor slurry obtains sal glauberi solid, sal glauberi after solid-liquid separation treatment
Solid Conveying and Melting carries out weight in the saltcake dissolving tank 16 into the output of S4. sodium sulphate molten；Freezing mother liquor is delivered to the steaming of the first mother liquor
A point salt is carried out in hair device 25, obtains mixed salt slurry and concentrated mother liquor；Mixed salt slurry obtains dehydration mixed salt, takes off after being separated by solid-liquid separation
Water mixed salt is delivered to the salt Multi-effect evaporation crystallizer 21 in the output of S3. sodium chloride；Concentrated mother liquor is first delivered to the steaming of the second mother liquor
Hair device 26 is concentrated, and secondary concentration mother liquor, the SiO of concentrated mother liquor are obtained2≤ 8000mg/l, then secondary concentration mother liquor is conveyed
It is dry in carnallite drier 27, obtain carnallite.
The identical waste water of 2 water quality and quantity of embodiment is delivered in Conventional waste water Zero discharging system (as shown in Figure 1) and is carried out
Processing, to second level nanofiltration operating pressure, sodium chloride crystallization purity salt and yield, sulfate crystal purity salt and yield, carnallite rate
It is detected and is compared, comparing result is as shown in table 1 below.
1 two groups of comparing results of table
As shown in Table 1, compared with routinely advising wastewater zero discharge system, the present embodiment utilizes reverse osmosis produced water and a nanofiltration
Concentrated water mixes in proportion, reduces the operating pressure of second level nanofiltration, improves the second level nanofiltration rate of recovery, extends equipment and uses the longevity
Life.In addition, the present embodiment by the optimization to crystal system, improve byproduct sodium chloride crystal salt, sulfate crystal salt it is pure
Degree and yield, and carnallite yield is reduced, carnallite processing cost can be reduced.
Embodiment 3:
Salt is divided to crystallize Zero discharge treatment method using the coal water slurry gasification waste water that embodiment 1 carries out, as shown in figure 3, it is wrapped
Include following steps:
S1. pre-process: coal water slurry gasification waste water is carried out into pretreatment system except hard drop after conditioning tank homogeneous average
It is turbid, except silicon, pH adjust, removal organic matter processing, it is specific as follows:
A1. chemical tendering: coal water slurry gasification waste water be delivered to chemical tendering equipment 1 carry out except drop firmly it is turbid, except silicon, removal have
The processing of machine object, obtains chemical tendering water, and the index of chemical tendering water is Ca2+≤50.00mg/l、Mg2+≤50.00mg/l、
SiO2≤ 15.00mg/l, turbidity≤20NTU；Obtained sludge is delivered to the dehydration of filter press 28, obtains dewatered sludge；
A2. it filters: being delivered to after chemical tendering water tune pH to 7.5 in filtration system and drop turbid, drainage is obtained, filter
Turbidity≤1NTU of water；
A3. depth softens: crossing drainage and is delivered to progress depth softening in ion-exchange unit 4, arrives pretreated waste water；
Pretreated waste water is obtained, the index of pretreated waste water is Ca2+=0mg/l, Mg2+=0mg/l, SiO2≤
15.00mg/l, turbidity≤1NTU, pH 7.5；
S2. divide salt: pretreated waste water is delivered to primary reverse osmosis system 5 and is concentrated, and obtains a concentrated water；Concentrated water
It after tune pH is 4.5, is delivered in decarbonizer 6 and removes removing carbon dioxide, obtain decarburization water outlet；Decarburization water outlet is delivered to two-pass reverse osmosis
System 8 is concentrated, and secondary concentrated water is obtained；Secondary concentrated water is delivered to the removal that advanced oxidation system 9 carries out organic matter, obtains oxygen
Change waste water；Primary reverse osmosis system 5, two-stage reverse osmosis system 8 production water be delivered in reuse pool 7, as recycle-water；Oxygen
Change waste water and be delivered to the once point salt treatment of level-one nanofiltration system 10, obtains a nanofiltration concentrated water；Nanofiltration concentrated water with return
Second level nanofiltration system 11 is delivered to according to the ratio that volume ratio is 4:3.5 with water and carries out secondary point of salt treatment, obtains secondary nanofiltration
Concentrated water；Nanofiltration produces water, secondary nanofiltration produces water and is delivered in nanofiltration production pond 12, as salt waste water to be gone out；Salt to be gone out is useless
Water is delivered to three-level counter-infiltration system 13 and is concentrated, and obtains concentrated water three times and produces water three times；It is anti-to be delivered to level Four for production water three times
Osmosis system 14 is handled, and is obtained four production water and is delivered to reuse pool 7, is obtained four concentrated waters and is delivered to nanofiltration production pond
12, it obtains four production water and is delivered to reuse pool 7；
S3. the output of sodium chloride: concentrated water is delivered to salt Multi-effect evaporation crystallizer 21 and is evaporated crystallization three times, obtains salt slurry
Material and salt mother liquor；Salt slurry is delivered in salt centrifuge 22 and is separated by solid-liquid separation, and obtains solid sodium chloride；Solid sodium chloride conveying
Being dried in salt drying machine 23 to water content is 0.08%, obtains sodium chloride crystal salt, the purity of sodium chloride crystal salt is
98.9%；
S4. the output of sodium sulphate: secondary nanofiltration concentrated water is delivered to saltcake Multi-effect evaporation crystallizer 15 and is evaporated crystallization,
Obtain saltcake slurry and saltcake mother liquor；Saltcake slurry is separated by solid-liquid separation, and solid sodium sulfate is obtained；Solid sodium sulfate is delivered to awns
It is molten that nitre dissolving tank 16 carries out weight, until solution in saltcake dissolving tank 16 is sodium sulphate saturated solution, obtains weight solution；Weight solution is defeated
It send to saltcake and recrystallizes evaporator 17, obtain recrystallization slurry；Recrystallization slurry is delivered to saltcake centrifuge 18 and carries out solid-liquid point
From obtaining solid sodium sulfate；It is 0.23% that solid sodium sulfate, which is delivered in saltcake drying machine 19 and dries to water content, obtains sulfuric acid
Sodium crystal salt, the TOC of sulfate crystal salt is 32mg/KG, purity 97.8%；
S5. the processing of mother liquor: salt mother liquor, saltcake mother liquor, which are delivered in mother liquor freezing and crystallizing device 24, carries out freezing and crystallizing,
COD≤18000mg/L of salt mother liquor, SiO2≤ 4000mg/l, COD≤30000mg/L of saltcake mother liquor, SiO2≤ 5000mg/l,
Obtain mother liquor slurry and freezing mother liquor；Mother liquor slurry obtains sal glauberi solid, sal glauberi after solid-liquid separation treatment
Solid Conveying and Melting carries out weight in the saltcake dissolving tank 16 into the output of S4. sodium sulphate molten；Freezing mother liquor is delivered to the steaming of the first mother liquor
A point salt is carried out in hair device 25, obtains mixed salt slurry and concentrated mother liquor；Mixed salt slurry obtains dehydration mixed salt, takes off after being separated by solid-liquid separation
Water mixed salt is delivered to the salt Multi-effect evaporation crystallizer 21 in the output of S3. sodium chloride；Concentrated mother liquor is first delivered to the steaming of the second mother liquor
Hair device 26 is concentrated, and secondary concentration mother liquor, the SiO of concentrated mother liquor are obtained2≤ 8000mg/l, then secondary concentration mother liquor is conveyed
It is dry in carnallite drier 27, obtain carnallite.
The identical waste water of 3 water quality and quantity of embodiment is delivered in Conventional waste water Zero discharging system (as shown in Figure 1) and is carried out
Processing produces second level nanofiltration operating pressure, sodium chloride crystallization purity salt and yield, sulfate crystal purity salt and yield, carnallite
Amount is detected and is compared, and comparing result is as shown in table 2 below.
2 two groups of comparing results of table
As shown in Table 2, compared with routinely advising wastewater zero discharge system, the present embodiment utilizes reverse osmosis produced water and a nanofiltration
Concentrated water mixes in proportion, reduces the operating pressure of second level nanofiltration, improves the second level nanofiltration rate of recovery, extends equipment and uses the longevity
Life.In addition, the present embodiment by the optimization to crystal system, improve byproduct sodium chloride crystal salt, sulfate crystal salt it is pure
Degree and yield, and carnallite yield is reduced, carnallite processing cost can be reduced.
Embodiment 4:
Salt is divided to crystallize Zero discharge treatment method using the coal water slurry gasification waste water that embodiment 1 carries out, as shown in figure 3, it is wrapped
Include following steps:
S1. pre-process: coal water slurry gasification waste water is carried out into pretreatment system except hard drop after conditioning tank homogeneous average
It is turbid, except silicon, pH adjust, removal organic matter processing, it is specific as follows:
A1. chemical tendering: coal water slurry gasification waste water be delivered to chemical tendering equipment 1 carry out except drop firmly it is turbid, except silicon, removal have
The processing of machine object, obtains chemical tendering water, and the index of chemical tendering water is Ca2+≤50.00mg/l、Mg2+≤50.00mg/l、
SiO2≤ 15.00mg/l, turbidity≤20NTU；Obtained sludge is delivered to the dehydration of filter press 28, obtains dewatered sludge；
A2. it filters: being delivered to after chemical tendering water tune pH to 8 in filtration system and drop turbid, be obtained drainage, cross drainage
Turbidity≤1NTU；
A3. depth softens: crossing drainage and is delivered to progress depth softening in ion-exchange unit 4, arrives pretreated waste water；
Pretreated waste water is obtained, the index of pretreated waste water is Ca2+=0mg/l, Mg2+=0mg/l, SiO2≤
15.00mg/l, turbidity≤1NTU, pH 8；
S2. divide salt: pretreated waste water is delivered to primary reverse osmosis system 5 and is concentrated, and obtains a concentrated water；Concentrated water
It after tune pH is 5, is delivered in decarbonizer 6 and removes removing carbon dioxide, obtain decarburization water outlet；Decarburization water outlet is delivered to two-pass reverse osmosis system
System 8 is concentrated, and secondary concentrated water is obtained；Secondary concentrated water is delivered to the removal that advanced oxidation system 9 carries out organic matter, is aoxidized
Waste water；Primary reverse osmosis system 5, two-stage reverse osmosis system 8 production water be delivered in reuse pool 7, as recycle-water；Oxidation
Waste water is delivered to the once point salt treatment of level-one nanofiltration system 10, obtains a nanofiltration concentrated water；Nanofiltration concentrated water and reuse
Water is delivered to second level nanofiltration system 11 according to the ratio that volume ratio is 4:4 and carries out secondary point of salt treatment, and it is dense to obtain secondary nanofiltration
Water；Nanofiltration produces water, secondary nanofiltration produces water and is delivered in nanofiltration production pond 12, as salt waste water to be gone out；Salt waste water to be gone out
It is delivered to three-level counter-infiltration system 13 to be concentrated, obtains concentrated water three times and produces water three times；Water is produced three times is delivered to level Four reverse osmosis
Permeable system 14 is handled, and is obtained four production water and is delivered to reuse pool 7, is obtained four concentrated waters and is delivered to nanofiltration production pond 12,
It obtains four production water and is delivered to reuse pool 7；
S3. the output of sodium chloride: concentrated water is delivered to salt Multi-effect evaporation crystallizer 21 and is evaporated crystallization three times, obtains salt slurry
Material and salt mother liquor；Salt slurry is delivered in salt centrifuge 22 and is separated by solid-liquid separation, and obtains solid sodium chloride；Solid sodium chloride conveying
Being dried in salt drying machine 23 to water content is 0.05%, obtains sodium chloride crystal salt, the purity of sodium chloride crystal salt is
99.2%；
S4. the output of sodium sulphate: secondary nanofiltration concentrated water is delivered to saltcake Multi-effect evaporation crystallizer 15 and is evaporated crystallization,
Obtain saltcake slurry and saltcake mother liquor；Saltcake slurry is separated by solid-liquid separation, and solid sodium sulfate is obtained；Solid sodium sulfate is delivered to awns
It is molten that nitre dissolving tank 16 carries out weight, until solution in saltcake dissolving tank 16 is sodium sulphate saturated solution, obtains weight solution；Weight solution is defeated
It send to saltcake and recrystallizes evaporator 17, obtain recrystallization slurry；Recrystallization slurry is delivered to saltcake centrifuge 18 and carries out solid-liquid point
From obtaining solid sodium sulfate；It is 0.19% that solid sodium sulfate, which is delivered in saltcake drying machine 19 and dries to water content, obtains sulfuric acid
Sodium crystal salt, the TOC of sulfate crystal salt is 28mg/KG, purity 99.1%；
S5. the processing of mother liquor: salt mother liquor, saltcake mother liquor, which are delivered in mother liquor freezing and crystallizing device 24, carries out freezing and crystallizing,
COD≤18000mg/L of salt mother liquor, SiO2≤ 4000mg/l, COD≤30000mg/L of saltcake mother liquor, SiO2≤ 5000mg/l,
Obtain mother liquor slurry and freezing mother liquor；Mother liquor slurry obtains sal glauberi solid, sal glauberi after solid-liquid separation treatment
Solid Conveying and Melting carries out weight in the saltcake dissolving tank 16 into the output of S4. sodium sulphate molten；Freezing mother liquor is delivered to the steaming of the first mother liquor
A point salt is carried out in hair device 25, obtains mixed salt slurry and concentrated mother liquor；Mixed salt slurry obtains dehydration mixed salt, takes off after being separated by solid-liquid separation
Water mixed salt is delivered to the salt Multi-effect evaporation crystallizer 21 in the output of S3. sodium chloride；Concentrated mother liquor is first delivered to the steaming of the second mother liquor
Hair device 26 is concentrated, and secondary concentration mother liquor, the SiO of concentrated mother liquor are obtained2≤ 8000mg/l, then secondary concentration mother liquor is conveyed
It is dry in carnallite drier 27, obtain carnallite.
The identical waste water of 4 water quality and quantity of embodiment is delivered in Conventional waste water Zero discharging system (as shown in Figure 1) and is carried out
Processing produces second level nanofiltration operating pressure, sodium chloride crystallization purity salt and yield, sulfate crystal purity salt and yield, carnallite
Amount is detected and is compared, and comparing result is as shown in table 3 below.
3 two groups of comparing results of table
As shown in Table 3, compared with routinely advising wastewater zero discharge system, the present embodiment utilizes reverse osmosis produced water and a nanofiltration
Concentrated water mixes in proportion, reduces the operating pressure of second level nanofiltration, improves the second level nanofiltration rate of recovery, extends equipment and uses the longevity
Life.In addition, the present embodiment by the optimization to crystal system, improve byproduct sodium chloride crystal salt, sulfate crystal salt it is pure
Degree and yield, and carnallite yield is reduced, carnallite processing cost can be reduced.
The above is only the preferred embodiment of the utility model only, is not intended to limit the utility model, all at this
Within the spirit and principle of utility model, any modification, equivalent replacement, improvement and so on should be included in the utility model
Protection scope within.
Claims (7)
1. coal water slurry gasification waste water divides salt to crystallize zero-discharge treatment system, which is characterized in that it includes pretreatment system, divides salt system
System, sodium chloride crystal system and salt crystal system, the water outlet of the ion-exchange unit of the pretreatment system divide salt system with described
The water inlet of the primary reverse osmosis system of system connects, concentrated water outlet and the saltcake of the second level nanofiltration system for dividing salt system
The water inlet of the saltcake Multi-effect evaporation crystallizer of crystal system connects, and the concentrated water of the three-level counter-infiltration system of described point of salt system goes out
Mouth is connect with the import of the salt Multi-effect evaporation crystallizer of the salt crystal system, and the mother liquor of the saltcake Multi-effect evaporation crystallizer goes out
Mouthful, the mother liquor outlet of the salt Multi-effect evaporation crystallizer connect respectively with the import of mother liquor freezing and crystallizing device, the mother liquor freezes
The slurry outlet of crystallizer is connect with the import of liquid separation centrifuge, solids outlet and the saltcake knot of the liquid separation centrifuge
The material inlet connection of the saltcake dissolving tank of crystallographic system system；The mother liquor outlet of the mother liquor freezing and crystallizing device and the salt crystal system
The first mother liquid evaporation device import connection, the import of the slurry outlet of the first mother liquid evaporation device and mother liquor centrifuge connects
It connects, the solid outlet of the mother liquor centrifuge is connect with the import of the salt Multi-effect evaporation crystallizer, first mother liquid evaporation
The mother liquor outlet of device is connect with the import of carnallite drier.
2. coal water slurry gasification waste water according to claim 1 divides salt to crystallize zero-discharge treatment system, which is characterized in that described
Pretreatment system includes chemical tendering equipment, filter plant and the ion-exchange unit, the water inlet of the chemical tendering equipment
Mouth is connect with coal water slurry gasification waste line, and the water outlet of the chemical tendering equipment and the water inlet of the filter plant connect
It connects, the water outlet of the filter plant is connect with the water inlet of the ion-exchange unit；It is equipped in the chemical tendering equipment
Mud scraper, the mud discharging mouth of the chemical tendering equipment and the feed inlet of filter press connect.
3. coal water slurry gasification waste water according to claim 2 divides salt to crystallize zero-discharge treatment system, which is characterized in that described
Filter plant includes V-type filter tank and ultrafiltration apparatus, and the water outlet in the V-type filter tank is connect with the water inlet of the ultrafiltration apparatus.
4. coal water slurry gasification waste water according to claim 1 divides salt to crystallize zero-discharge treatment system, which is characterized in that described
Point salt system includes the primary reverse osmosis system, reuse pool, decarbonizer, two-stage reverse osmosis system, advanced oxidation system, one
Grade nanofiltration system, the second level nanofiltration system, nanofiltration produce pond, the three-level counter-infiltration system and level Four counter-infiltration system, institute
The production water out for stating primary reverse osmosis system is connect with the water inlet of the reuse pool, the concentrated water of the primary reverse osmosis system
Outlet is connect with the water inlet of the decarbonizer, and the water inlet of the water outlet of the decarbonizer and the two-stage reverse osmosis system connects
It connects；The production water out of the two-stage reverse osmosis system is connect with the water inlet of the reuse pool, the two-stage reverse osmosis system
Concentrated water outlet connect with the water inlet of the advanced oxidation system；The water outlet of the advanced oxidation system is received with the level-one
The water inlet of filter system connects, and the production water out of the level-one nanofiltration system is connect with the water inlet that the nanofiltration produces pond, institute
The concentrated water outlet for stating level-one nanofiltration system is connect with the water inlet of the second level nanofiltration system, the water inlet of the second level nanofiltration system
Mouth is also connect by regulating valve with the water outlet of the reuse pool；The production water out of the second level nanofiltration system and the nanofiltration
Produce the water inlet connection in pond；The water outlet that the nanofiltration produces pond is connect with the water inlet of the three-level counter-infiltration system, institute
The production water out for stating three-level counter-infiltration system is connect with the water inlet of the level Four counter-infiltration system；The level Four counter-infiltration system
Production water out connect with the water inlet of the reuse pool, the outlet of the concentrated water of the level Four counter-infiltration system is produced with the nanofiltration
The water inlet in pond connects；The three-level counter-infiltration system is disc tube reverse osmosis (dt-ro) system, electric drive membranous system or rolling reverse osmosis
Any one in permeable system, the level Four counter-infiltration system are appointing in disc tube reverse osmosis (dt-ro) system or rolling counter-infiltration system
It anticipates one kind.
5. coal water slurry gasification waste water according to claim 1 divides salt to crystallize zero-discharge treatment system, which is characterized in that described
Sodium chloride crystal system include the saltcake Multi-effect evaporation crystallizer, the saltcake dissolving tank, saltcake recrystallization evaporator, saltcake from
Scheming and saltcake drying machine, the slurry outlet of the saltcake Multi-effect evaporation crystallizer are connect with the import of the liquid separation centrifuge,
The material outlet of the saltcake dissolving tank is connect with the material inlet of saltcake recrystallization evaporator, and the saltcake recrystallization steams
The material outlet of hair device is connect with the material inlet of the saltcake centrifuge, the solids of the saltcake centrifuge export with it is described
The feed inlet of saltcake drying machine connects, and the discharge port of the saltcake drying machine is connect with the import of sodium sulphate warehouse.
6. coal water slurry gasification waste water according to claim 1 divides salt to crystallize zero-discharge treatment system, which is characterized in that described
Salt crystal system includes the salt Multi-effect evaporation crystallizer, salt centrifuge, salt drying machine, and the solids exports and the salt
The material inlet of centrifuge connects, and the solids outlet of the salt centrifuge is connect with the feed inlet of the salt drying machine, described
The discharge port of salt drying machine is connect with the import of sodium chloride warehouse.
7. coal water slurry gasification waste water according to claim 1 divides salt to crystallize zero-discharge treatment system, which is characterized in that it is also
It include the second mother liquid evaporation device, the import of the mother liquor outlet of the first mother liquid evaporation device and the second mother liquid evaporation device connects
It connects, the slurry outlet of the second mother liquid evaporation device is connect with the import of the carnallite drier.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110357334A (en) * | 2018-12-05 | 2019-10-22 | 内蒙古荣信化工有限公司 | Coal water slurry gasification waste water divides salt crystallization zero-discharge treatment system and method |
| CN111977882A (en) * | 2020-09-16 | 2020-11-24 | 麦王环境技术股份有限公司 | High-salinity wastewater zero-emission quality-divided crystallization device and process |
| CN113072228A (en) * | 2020-01-03 | 2021-07-06 | 中国石油化工股份有限公司 | Method and system for treating salt-containing wastewater |
| CN113413762A (en) * | 2021-05-26 | 2021-09-21 | 中国神华煤制油化工有限公司 | Treatment method of reverse osmosis concentrated solution |
| CN114195302A (en) * | 2020-09-17 | 2022-03-18 | 中国石油化工股份有限公司 | Equipment and method for extracting sodium sulfate and sodium chloride from high-salinity wastewater in coal chemical industry |
| CN116253470A (en) * | 2023-03-17 | 2023-06-13 | 中国石油化工股份有限公司 | A zero-discharge treatment method and system for waste water containing miscellaneous salt |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110357334A (en) * | 2018-12-05 | 2019-10-22 | 内蒙古荣信化工有限公司 | Coal water slurry gasification waste water divides salt crystallization zero-discharge treatment system and method |
| CN110357334B (en) * | 2018-12-05 | 2024-11-05 | 内蒙古荣信化工有限公司 | System and method for zero-emission treatment of salt crystallization of coal-water slurry gasification wastewater |
| CN113072228A (en) * | 2020-01-03 | 2021-07-06 | 中国石油化工股份有限公司 | Method and system for treating salt-containing wastewater |
| CN111977882A (en) * | 2020-09-16 | 2020-11-24 | 麦王环境技术股份有限公司 | High-salinity wastewater zero-emission quality-divided crystallization device and process |
| CN114195302A (en) * | 2020-09-17 | 2022-03-18 | 中国石油化工股份有限公司 | Equipment and method for extracting sodium sulfate and sodium chloride from high-salinity wastewater in coal chemical industry |
| CN113413762A (en) * | 2021-05-26 | 2021-09-21 | 中国神华煤制油化工有限公司 | Treatment method of reverse osmosis concentrated solution |
| CN116253470A (en) * | 2023-03-17 | 2023-06-13 | 中国石油化工股份有限公司 | A zero-discharge treatment method and system for waste water containing miscellaneous salt |
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