CN110550792A - desulfurization wastewater recycling zero-discharge method - Google Patents
desulfurization wastewater recycling zero-discharge method Download PDFInfo
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- CN110550792A CN110550792A CN201810537012.6A CN201810537012A CN110550792A CN 110550792 A CN110550792 A CN 110550792A CN 201810537012 A CN201810537012 A CN 201810537012A CN 110550792 A CN110550792 A CN 110550792A
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- water
- magnesium sulfate
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 27
- 230000023556 desulfurization Effects 0.000 title claims abstract description 27
- 239000002351 wastewater Substances 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 22
- 238000004064 recycling Methods 0.000 title description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 96
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 66
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims abstract description 60
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 45
- 239000011780 sodium chloride Substances 0.000 claims abstract description 33
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims abstract description 30
- 235000019341 magnesium sulphate Nutrition 0.000 claims abstract description 30
- OSVXSBDYLRYLIG-UHFFFAOYSA-N dioxidochlorine(.) Chemical compound O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000001704 evaporation Methods 0.000 claims abstract description 21
- 230000008020 evaporation Effects 0.000 claims abstract description 20
- 239000007788 liquid Substances 0.000 claims abstract description 19
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 17
- 238000002425 crystallisation Methods 0.000 claims abstract description 15
- 230000008025 crystallization Effects 0.000 claims abstract description 15
- WRUGWIBCXHJTDG-UHFFFAOYSA-L magnesium sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Mg+2].[O-]S([O-])(=O)=O WRUGWIBCXHJTDG-UHFFFAOYSA-L 0.000 claims abstract description 15
- 239000012452 mother liquor Substances 0.000 claims abstract description 15
- 229940061634 magnesium sulfate heptahydrate Drugs 0.000 claims abstract description 12
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000004155 Chlorine dioxide Substances 0.000 claims abstract description 9
- 239000005708 Sodium hypochlorite Substances 0.000 claims abstract description 9
- 235000019398 chlorine dioxide Nutrition 0.000 claims abstract description 9
- 239000002699 waste material Substances 0.000 claims abstract description 8
- 230000008014 freezing Effects 0.000 claims abstract description 5
- 238000007710 freezing Methods 0.000 claims abstract description 5
- 239000012528 membrane Substances 0.000 claims description 37
- 150000002500 ions Chemical class 0.000 claims description 18
- 238000002156 mixing Methods 0.000 claims description 18
- 239000011575 calcium Substances 0.000 claims description 15
- 239000011777 magnesium Substances 0.000 claims description 12
- 239000012065 filter cake Substances 0.000 claims description 10
- 238000011084 recovery Methods 0.000 claims description 10
- 238000000108 ultra-filtration Methods 0.000 claims description 10
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 9
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 9
- 229910001424 calcium ion Inorganic materials 0.000 claims description 9
- 239000002131 composite material Substances 0.000 claims description 9
- 239000007789 gas Substances 0.000 claims description 9
- 239000002455 scale inhibitor Substances 0.000 claims description 9
- 229910052708 sodium Inorganic materials 0.000 claims description 9
- 239000011734 sodium Substances 0.000 claims description 9
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 9
- 235000011152 sodium sulphate Nutrition 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 8
- 239000003463 adsorbent Substances 0.000 claims description 8
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 7
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 239000003546 flue gas Substances 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 7
- 229910052791 calcium Inorganic materials 0.000 claims description 6
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 6
- 239000000920 calcium hydroxide Substances 0.000 claims description 6
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 6
- 229910052602 gypsum Inorganic materials 0.000 claims description 6
- 239000010440 gypsum Substances 0.000 claims description 6
- 229910052749 magnesium Inorganic materials 0.000 claims description 6
- 230000014759 maintenance of location Effects 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 239000006227 byproduct Substances 0.000 claims description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 4
- 239000002033 PVDF binder Substances 0.000 claims description 4
- 239000000701 coagulant Substances 0.000 claims description 4
- 229910052681 coesite Inorganic materials 0.000 claims description 4
- 229910052906 cristobalite Inorganic materials 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 4
- 229910001425 magnesium ion Inorganic materials 0.000 claims description 4
- 229920002981 polyvinylidene fluoride Polymers 0.000 claims description 4
- 230000008929 regeneration Effects 0.000 claims description 4
- 238000011069 regeneration method Methods 0.000 claims description 4
- 239000000377 silicon dioxide Substances 0.000 claims description 4
- 235000012239 silicon dioxide Nutrition 0.000 claims description 4
- 229910052682 stishovite Inorganic materials 0.000 claims description 4
- 229910052905 tridymite Inorganic materials 0.000 claims description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 3
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 claims description 3
- 230000002457 bidirectional effect Effects 0.000 claims description 3
- 230000033228 biological regulation Effects 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims description 3
- 239000013078 crystal Substances 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 3
- 229910052731 fluorine Inorganic materials 0.000 claims description 3
- 238000002347 injection Methods 0.000 claims description 3
- 239000007924 injection Substances 0.000 claims description 3
- 238000001223 reverse osmosis Methods 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 claims description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 2
- 238000000889 atomisation Methods 0.000 claims description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 2
- 238000010612 desalination reaction Methods 0.000 claims description 2
- 238000004821 distillation Methods 0.000 claims description 2
- 230000002349 favourable effect Effects 0.000 claims description 2
- 239000002245 particle Substances 0.000 claims description 2
- 239000000843 powder Substances 0.000 claims description 2
- 230000003014 reinforcing effect Effects 0.000 claims description 2
- 238000005201 scrubbing Methods 0.000 claims description 2
- 229910052719 titanium Inorganic materials 0.000 claims description 2
- 239000010936 titanium Substances 0.000 claims description 2
- 230000000630 rising effect Effects 0.000 claims 2
- 238000005352 clarification Methods 0.000 claims 1
- 238000005189 flocculation Methods 0.000 claims 1
- 230000016615 flocculation Effects 0.000 claims 1
- 238000004065 wastewater treatment Methods 0.000 abstract description 2
- 239000010802 sludge Substances 0.000 description 9
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 4
- 230000001276 controlling effect Effects 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000001954 sterilising effect Effects 0.000 description 3
- 239000003814 drug Substances 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 125000001741 organic sulfur group Chemical group 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/40—Magnesium sulfates
-
- 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
-
- 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
- C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
- C02F1/12—Spray 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/288—Treatment of water, waste water, or sewage by sorption using composite sorbents, e.g. coated, impregnated, multi-layered
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
- C02F1/385—Treatment of water, waste water, or sewage by centrifugal separation by centrifuging suspensions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- 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
- C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
-
- 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
- C02F2303/04—Disinfection
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Geology (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Materials Engineering (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
the invention relates to the field of desulfurization wastewater treatment, and discloses a desulfurization wastewater resource zero-discharge method, which comprises the following steps: concentrated water of an NF device passes through concentrated water of a magnesium sulfate concentration device and then passes through a magnesium sulfate evaporation crystallizer and a freezing separator to generate magnesium sulfate heptahydrate, the produced water of the NF device passes through a primary RO device and concentrated water of an HIRO device and then enters a sodium chloride crystallizer to generate sodium chloride, the concentrated water of the HIRO device passes through an electrolysis device to generate sodium hydroxide, chlorine dioxide and sodium hypochlorite, and waste liquid of the electrolysis device enters the sodium chloride crystallizer; the flue evaporation crystallization device evaporates and crystallizes mother liquor of the magnesium sulfate evaporation crystallizer and the sodium chloride crystallizer, and real zero emission is realized.
Description
Technical Field
The invention relates to the technical field of desulfurization wastewater treatment and environmental protection of thermal power plants, and particularly relates to a desulfurization wastewater resource zero-emission method.
Background
At present, the economy of China is developed at a high speed, and simultaneously, the environmental problem is increasingly serious along with the huge consumption of energy. In order to improve the current environmental situation, the national management of three wastes is getting tighter and tighter, the industrial wastewater zero discharge is accepted by a plurality of enterprises and professional personnel, and the implementation in the industrial field is gradually started. The water is used as an indispensable resource in the industrial field, and the discharge of concentrated brine is used as an important environmental protection index. The zero discharge implemented in the industrial wastewater field of China, especially in a thermal power plant, has the key problems of high operation cost and investment cost of desulfurization wastewater and lack of stable operation experience, and how to find a more stable treatment method and a technology with lower operation cost by experiments is being explored.
Under the normal operation condition of the desulfurization system, in order to keep stable operation and continuously discharge desulfurization wastewater, Mg in some desulfurization wastewater reaches more than 2000Mg, and in the softening process, Mg is required to be settled to generate Mg (OH) 2 by the traditional method, so that a large amount of OH radicals are added, a large amount of sludge is generated, and the operation and maintenance cost of the system is increased.
Therefore, it is necessary to develop a method for reducing the dosage of the desulfurization wastewater and simultaneously reducing the sludge discharge, and the obtained by-products can be recycled.
disclosure of Invention
the invention overcomes the defects of the prior art and provides a desulfurization wastewater resource zero-discharge method.
in view of the above problems of the prior art, according to one aspect of the present invention, to solve the above technical problems, the present invention provides a method for zero emission of desulfurization waste water, which comprises: the method comprises the following steps that desulfurization wastewater enters an NF device after being softened and clarified, concentrated water of the NF device passes through concentrated water of a magnesium sulfate concentration device and then passes through a magnesium sulfate evaporation crystallizer and a freezing separator to generate magnesium sulfate heptahydrate, produced water of the NF device passes through a first-stage RO device and concentrated water of an HIRO device and then enters a sodium chloride crystallizer to generate sodium chloride, concentrated water of the HIRO device passes through an electrolysis device to generate sodium hydroxide, chlorine dioxide and sodium hypochlorite, and waste liquid of the electrolysis device enters the sodium chloride crystallizer; the flue evaporation crystallization device evaporates and crystallizes mother liquor of the magnesium sulfate evaporation crystallizer and the sodium chloride crystallizer, and real zero emission is realized.
Compared with the prior art, the invention has the advantages that:
(1) adding high-efficiency composite inorganic adsorbent to obtain original organic sulfur, flocculant and coagulant aid, and reducing dosage;
(2) The high-pressure ozone device and the high-pressure ultraviolet device are arranged, so that COD is effectively reduced;
(3) Mg ions finally form magnesium sulfate heptahydrate, so that the dosage of precipitated magnesium ions is reduced, and simultaneously, sludge is also reduced;
(4) the sodium bed regenerates and utilizes the concentrated water of the HIRO device, thereby saving the medicament and saving part of the investment of the wastewater and the operation treatment cost;
(5) Concentrated water generated by the HIRO device enters an electrolysis device and a sodium chloride crystallizer, and a byproduct generated by the electrolysis device is comprehensively utilized;
(6) mother liquor of the evaporative crystallizer is discharged into a flue evaporative crystallization device, so that real zero emission is realized.
Drawings
For a clear explanation of the embodiments or prior art technical solutions of the present application, the drawings needed to be used in the description of the embodiments or prior art will be briefly described below, it is obvious that the drawings in the following description are only references to some embodiments in the present application, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts, and some parts of them can be used after adjustment.
FIG. 1 shows a preferred embodiment of a zero-emission method for recycling desulfurization waste water. In the figure, (101) desulfurization waste water, (102) magnesium sulfate heptahydrate, (103) sodium chloride, (104) sodium hydroxide, (105) chlorine dioxide, and (106) sodium hypochlorite.
Detailed Description
The present invention will be described in further detail with reference to examples, but the embodiments of the present invention are not limited thereto.
fig. 1 shows a zero emission method for recycling desulfurization wastewater according to an embodiment of the invention, which comprises the following steps: the method comprises the following steps that desulfurization waste water (101) is softened and clarified and then enters an NF device, concentrated water of the NF device passes through concentrated water of a magnesium sulfate concentration device and then passes through a magnesium sulfate evaporation crystallizer and a freezing separator to generate magnesium sulfate heptahydrate (102), produced water of the NF device passes through a first-stage RO device and concentrated water of an HIRO device and then enters a sodium chloride crystallizer to generate sodium chloride (103), concentrated water of the HIRO device passes through an electrolysis device to generate sodium hydroxide (104), chlorine dioxide (105) and sodium hypochlorite (106), and waste liquid of the electrolysis device enters the sodium chloride crystallizer; the flue evaporation crystallization device evaporates and crystallizes mother liquor of the magnesium sulfate evaporation crystallizer and the sodium chloride crystallizer, and real zero emission is realized.
(1) adding coagulant aid into desulfurized wastewater (101) generated by a desulfurization system before passing through a high-pressure cyclone, wherein the addition amount is 1 ~ 3ppm, the pressure of the high-pressure cyclone is more than PN40, the internal flow rate is 3m/s, the retention time is 30min, the overflow granularity D50 of the high-pressure cyclone is less than 1.0 mu m, the solid content of effluent is less than 5000ppm, and concentrated solution is discharged into the tail end of a vacuum belt conveyor and is separated from the underflow of an original gypsum cyclone;
(2) The water produced by the high-pressure cyclone enters a high-efficiency softener, calcium hydroxide and sodium hydroxide are respectively added into a front mixing tank of the high-efficiency softener, a PH meter is arranged at an outlet, the PH value is controlled to be about 9, sodium sulfate is added into a second front mixing tank, gypsum crystal seeds are simultaneously added to accelerate the formation of CaCO 4, an HCO 3 - detector is arranged at the inlet of the front mixing tank and is interlocked with the addition of calcium hydroxide and sodium hydroxide, a Ca hardness online monitor and a Mg hardness online monitor are arranged at the outlet of the second front mixing tank, the Ca hardness is controlled to be 40Mg/L, the effluent suspended matter is less than 50ppm, the residence time of the front mixing tank is 10min, a high-efficiency composite inorganic adsorbent and sodium sulfate are added into a reaction zone of the high-efficiency softener, the addition amount of the high-efficiency composite inorganic adsorbent is 10 ~ 50ppm, the addition amount of the sodium sulfate is 1.05 times of CA ions, an annular addition mixer is adopted in the reaction zone, a lifting mixer is adopted, 5m/s, a variable frequency motor is adopted to carry out frequency regulation, the residence time is 16min, the lifting amount is more than 15 ~ 20 times of inlet water, the high-efficiency softener, the linear speed of the sludge discharge system is 30min, the sludge discharge:
HCO3 -+OH+─→H2O
Ca2++CO3 2-─→CaCO3
Ca2++SO4 2-─→CaCO4
(3) The water produced by the high-efficiency softener enters a membrane filter for filtration, the doctor solution passes through a membrane filter element, clear solution penetrates through the membrane filter element and enters an upper cavity, solid in the liquid is completely intercepted on the surface of the membrane filter element to form a filter cake, the membrane has excellent non-adhesiveness and very small friction coefficient, an automatic execution system is added, instantaneous reverse flow in seconds forms reverse cleaning, the filter cake is completely removed from the surface of the filter element, the filter cake separated from the surface of the filter element is deposited at the bottom of the filter, and when a certain amount of the filter cake is reached, the filter cake is quickly discharged into a sludge dewatering system from the bottom;
(4) the water produced by the membrane filter enters hollow ultrafiltration, the material is PVDF membrane filaments with reinforcing ribs, the membrane filaments are allowed to freely swing in the membrane shell, the open structure is favorable for scrubbing air to enter each membrane filament, the intercepted solid is fully released, the water inlet pressure is more than 0.5Mpa, the water inlet suspended matter is 1 ~ 50mg/L, the COD is 10 ~ 100ppm, the effluent turbidity is 0.3NTU, and the SDI is less than 5;
(5) sterilizing the hollow ultrafiltration effluent by a high-pressure ozone device and a high-pressure ultraviolet device, and then feeding the hollow ultrafiltration effluent into an NF device, wherein the pressure of the high-pressure ozone device is more than PN1.6Mpa, a lamp tube in the high-pressure ultraviolet device is more than 100000 Pa, and the COD of the hollow ultrafiltration effluent is controlled to be within 50 ppm;
(6) the recovery rate of the NF device is more than 75 percent, when the NF device enters the NF device, the PH value of inlet water is controlled below 4, a scale inhibitor is added, the Ca hardness of the NF device is controlled to be 40mg/L, the pressure is 4.0Mpa, the desalination rate is more than 90 percent, due to the characteristic of the membrane, the NF device is connected with a direct current power supply to promote the separation of monovalent ions and divalent ions, the current of the NF device is 10A, under the action of the pressure and electrons, the monovalent ions and the divalent ions are completely separated, the divalent ions are arranged on the concentrated water side, and the monovalent ions are arranged on the water production side;
(7) adjusting the pH value of concentrated water generated by an NF device to 4, adjusting the pH value of the concentrated water to 10000 ~ 60000ppm, mainly containing magnesium sulfate solution, concentrating by a magnesium sulfate concentration device, wherein the recovery rate is more than 80%, enabling the produced water to enter a secondary RO device, enabling the concentrated water to contain more than 20000ppm magnesium sulfate and enter a magnesium sulfate evaporation crystallizer, stably controlling the operation to 70 ~ 90 ℃ and the operation pressure to be-0.1 Mpa, after the concentrated water is saturated, enabling the concentrated water to enter a refrigerated separator, separating calcium and magnesium, controlling the temperature to be 0 ~ 20 ℃ and washing the magnesium sulfate heptahydrate (102) by using secondary reverse osmosis produced water to ensure that the purity of the obtained magnesium sulfate heptahydrate (102) is 98%, wherein the magnesium sulfate concentration device is a membrane distillation device, and the magnesium sulfate evaporation crystallizer adopts an OSLO type and adopts titanium materials;
(8) the flue evaporative crystallization device can adopt two types, one type is flue direct injection, the other type is a bypass flue, the discharged mother liquor of the magnesium sulfate evaporative crystallizer and the sodium chloride crystallizer enters the flue evaporative crystallization device, a gas-liquid bidirectional flow nozzle is adopted to carry out circumferential tangential gas inlet, the gas directional pressure of the nozzle is 0.4 ~ 0.6Mpa, the gas quantity is 0.3 ~ 1Nm3/L water, the nozzle is made of PE, 10 mu m after atomization, 0.2t of a single nozzle is adopted, the density of the nozzle is 300%, the heated flue gas is 250 ~ 350 degrees, the outlet temperature is 100 ~ 345 degrees, the flue gas flow velocity in the flue evaporative crystallization is 5 ~ 10m/s, the bypass flue is provided with a bypass adjusting door which can be interlocked with the mother liquor, and is provided with a pressure side point, a flue flow measuring point and a temperature measuring point;
(9) the produced water of the NF device enters a sodium bed, the effluent of the sodium bed is provided with a hardness meter and a conductivity meter, the hardness is controlled to be 40mg/L, the conductivity is below 50000mg/L, the regeneration liquid adopts the concentrated water of the HIRO device, and the concentrated water is discharged into a raw water regulating reservoir after regeneration;
(10) adding a scale inhibitor into effluent of a sodium bed, adjusting the pH to 5, concentrating the effluent in a primary RO device, adjusting the pH of concentrated water to 5, feeding the concentrated water into a HIRO device, feeding the HIRO concentrated water into a sodium chloride crystallizer, and drying the obtained sodium chloride (103) to obtain sodium chloride not lower than the primary industrial salt standard, wherein the produced water of the primary RO device and the HIRO device enters a secondary RO, the effluent conductance is controlled to be 50ppm, the overall recovery rate of membrane concentration is controlled to be 70%, the pressure of the primary RO device is PN4.0Mpa ~ PN6.4Mpa, a high-pressure anti-pollution membrane is adopted, the flow channel is 45mil, the pressure of the HIRO device is PN16Mpa, a roll-type high-pressure wide-flow-channel anti-pollution membrane is adopted, the flow channel is 50mil, and the material;
(11) After the concentrated water of the HIRO concentrated water is electrolyzed by an electrolysis device according to needs, byproducts of sodium hydroxide (104), chlorine dioxide (105) and sodium hypochlorite (106) can be generated, and the waste liquid of the electrolysis device enters a sodium chloride crystallizer;
(12) the scale inhibitor is an inorganic composite scale inhibitor for preventing Ca, Mg, F and SiO 2;
(13) The high-efficiency adsorbent dosing device and the sodium sulfate dosing device are used for dosing dry powder;
(14) except for mother liquor discharge, evaporation is carried out, and the overall recovery rate of the system is more than 99%;
(15) the filtering precision of the filter element is 1 mu m;
(16) The water quality TDS of the desulfurization waste water is 8000 ~ 60000ppm, Mg2+ water is 500 ~ 10000ppm, Ca2+ is 100 ~ 10000ppm, SO 4 2-2000 ~ 20000ppm, Cl-is 1000 ~ 15000ppm, SiO2 is 10 ~ 500ppm, HCO 3-is 10 ~ 1000ppm, F-is 10 ~ 200ppm, SS is 30 ~ 20000ppm, COD is 30 ~ 300ppm, and the pH value is 5 ~ 9.
example 1
The reference data of the desulfurized wastewater are shown in the following table:
This example is used to illustrate the method for zero discharge of desulfurization wastewater resource provided by the present invention:
(1) adding coagulant aid into desulfurized wastewater (101) generated by a desulfurization system before passing through a high-pressure cyclone, wherein the addition amount is 1ppm, the pressure of the high-pressure cyclone is PN40, the internal flow rate is 3m/s, the retention time is 30min, the overflow particle size D50 of the high-pressure cyclone is less than 1.0 mu m, the solid content of effluent is less than 500ppm, and concentrated solution is discharged into the tail end of a vacuum belt conveyor and is separated from the underflow liquid of an original gypsum cyclone;
(2) The method comprises the following steps that water produced by a high-pressure cyclone enters a high-efficiency softener, 50ppm of calcium hydroxide and 80ppm of sodium hydroxide are respectively added into a front mixing tank of the high-efficiency softener, a PH meter is arranged at an outlet, the PH value is controlled to be about 9, 100ppm of sodium sulfate is added into a second front mixing tank, 1ppm of gypsum crystal seeds are added simultaneously to accelerate formation of CaCO 4, an HCO 3 - detector is arranged at the inlet of the front mixing tank and linked with calcium hydroxide and sodium hydroxide by adding medicines, an online Ca hardness monitor and an online Mg hardness monitor are arranged at the outlet of the second front mixing tank, the Ca hardness is controlled to be 40Mg/L, the suspended matter in effluent is 30ppm, if the hardness exceeds the standard, the system is linked and circulated, the effluent enters the previous stage, the front mixing tank stays for 10min, a reaction zone of the high-efficiency softener is added with 10ppm of high-efficiency composite inorganic adsorbent and 1.1 time of calcium ions, annular addition is adopted, a lifting mixing stirrer is adopted in the reaction zone, the velocity gradient is 50S -1, the height is 0.15m, the velocity of the frequency conversion motor is adopted to adjust the residence time, the residence time of the high-efficiency softener, the velocity converter stays for 15 min, the whole sludge discharge, the sludge discharge system rises, the sludge discharge rate;
(3) the produced water of the high-efficiency softener enters a membrane filter for filtration, the turbidity of the produced water is 5ppm, the produced water of the membrane filter enters hollow ultrafiltration, the water inlet pressure is more than 0.5Mpa, the COD is 30ppm, the turbidity of the produced water is 0.3NTU, and the SDI is less than 5;
(4) sterilizing the hollow ultrafiltration effluent by a high-pressure ozone device and a high-pressure ultraviolet device, and then feeding the hollow ultrafiltration effluent into an NF device, wherein the pressure of the high-pressure ozone device is more than PN1.6Mpa, a lamp tube in the high-pressure ultraviolet device is more than 100000 Pa, and the COD of the hollow ultrafiltration effluent is controlled to be within 50 ppm;
(5) when the wastewater enters an NF device, the recovery rate is controlled at 75 percent, the pH value is adjusted to 4 by adding acid, and simultaneously, an inorganic composite scale inhibitor for preventing Ca, Mg, F and SiO2 is added, and the adding amount is 3 ppm. Meanwhile, the Ca hardness is controlled to be 40mg/L, the pressure is 4.0Mpa, and the salt rejection rate is more than 90%. Meanwhile, the NF device is connected with a direct current power supply to promote the separation of monovalent ions and divalent ions, the current of the NF device is 10A, the monovalent ions and the divalent ions are completely separated under the action of pressure and electrons, the divalent ions are arranged on the concentrated water side, and the monovalent ions are arranged on the water production side;
(6) the method comprises the steps of adjusting the pH value of concentrated water generated by an NF device to 4, enabling the pH value of the concentrated water to be 30000ppm and mainly containing magnesium sulfate solution, concentrating the concentrated water through a magnesium sulfate concentration device, enabling the recovery rate to be 85%, enabling the produced water to enter a secondary RO device, enabling the concentrated water to be 200000ppm and enter a magnesium sulfate evaporation crystallizer, enabling the concentrated water to stably operate at 85 ℃ and the operating pressure to be-0.1 MPa, enabling the concentrated water to enter a freezing separator after being saturated in concentration, separating calcium and magnesium, controlling the temperature to be 0 ~ 20 ℃, and washing magnesium sulfate heptahydrate (102) through secondary reverse osmosis produced water to enable the purity of the obtained magnesium sulfate heptahydrate (102) to be 98%;
(7) the flue evaporation crystallization device of the embodiment adopts two types, namely flue direct injection and bypass flue; the discharged mother liquor of the magnesium sulfate evaporative crystallizer and the sodium chloride crystallizer enters a flue evaporative crystallization device, a gas-liquid bidirectional flow nozzle is adopted for circumferential tangential gas inlet, the gas directional pressure of the nozzle is 0.45Mpa, the gas amount is 0.3Nm3/L water, the nozzle is made of PE, the atomized mother liquor is 10 mu m, 0.2t of a single nozzle is adopted, the density of the nozzle is 300%, the heated flue gas is 350 ℃, the outlet temperature is 120 ℃, the flow velocity of the flue gas in the flue evaporative crystallization is 6m/s, a bypass flue is provided with a bypass adjusting door which can be interlocked with the mother liquor, and the bypass adjusting door is provided with a pressure side point, a flow measuring point and a temperature measuring point; directly spraying the flue into a straight flue in front of SCR, arranging nozzles according to a flue gas flow field and temperature to completely gasify the flue, and evaporating the flue to treat more than 120% of discharged mother liquor;
(8) the produced water of the NF device enters a sodium bed, the effluent of the sodium bed is provided with a hardness meter and a conductivity meter, the hardness is controlled to be 40mg/L, the conductivity is 10000mg/L, the regeneration liquid adopts the concentrated water of an HIRO device, and the regenerated water is discharged into a raw water regulating reservoir after being regenerated;
(9) adding a compound scale inhibitor into the effluent of the sodium bed, wherein the dosage is 0.5ppm, then adjusting the pH to 5, feeding the effluent into a first-stage RO device for concentration, adjusting the pH of concentrated water to 5, feeding the effluent into a HIRO device, feeding the HIRO concentrated water into a sodium chloride crystallizer, and drying the obtained sodium chloride (103) to obtain the sodium chloride with the purity of 99%; the overall recovery rate of membrane concentration is controlled to be 70 percent; the pressure of a primary RO device is PN4.0Mpa, a high-pressure anti-pollution membrane is adopted, a flow channel is 45mil, the pressure of a HIRO device is PN16Mpa, a roll-type high-pressure wide-flow-channel anti-pollution membrane is adopted, the flow channel is 50mil, and the material is PVDF;
(10) After the concentrated water of the 20% HIRO concentrated water is electrolyzed by the electrolysis device according to needs, byproducts of sodium hydroxide (104), chlorine dioxide (105) and sodium hypochlorite (106) can be generated, 20% waste liquid of the electrolysis device enters a sodium chloride crystallizer, the chlorine dioxide (105) and the sodium hypochlorite (106) are used for sterilization, and the sodium hydroxide is used for softening in the system.
In order to ensure the long-term stable operation of the process system, realize complete zero emission and utilize products, the method also comprises a relevant cleaning device, a dosing device, an electrical system and instrument control which are matched with each other, and the operation of the desulfurization wastewater recycling zero emission method is referred to.
reference throughout this specification to "one embodiment," "an embodiment," and so forth, means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment described generally throughout this application. The appearances of the same phrase in various places in the specification are not necessarily all referring to the same embodiment. Further, when a particular feature, structure, or characteristic is described in connection with any embodiment, it is submitted that it is within the scope of the invention to effect such feature, structure, or characteristic in connection with other embodiments.
Although the invention has been described herein with reference to a number of illustrative embodiments thereof, it should be understood that numerous other modifications and embodiments can be devised by those skilled in the art that will fall within the spirit and scope of the principles of this disclosure. More specifically, various variations and modifications are possible in the component parts and/or arrangements of the subject combination arrangement within the scope of the disclosure, the drawings and the appended claims. In addition to variations and modifications in the component parts and/or arrangements, other uses will also be apparent to those skilled in the art.
Claims (3)
1. a desulfurization wastewater resource zero-emission method comprises the following steps: the desulfurization wastewater enters an NF device after being softened and clarified, concentrated water of the NF device passes through a magnesium sulfate concentration device and then passes through a magnesium sulfate evaporation crystallizer and a freeze separator to generate magnesium sulfate heptahydrate, the produced water of the NF device passes through a first-stage RO device and a HIRO device and then enters a sodium chloride crystallizer to generate sodium chloride, the concentrated water of the HIRO device passes through an electrolysis device to generate sodium hydroxide, chlorine dioxide and sodium hypochlorite, and the waste liquid of the electrolysis device enters the sodium chloride crystallizer; the flue evaporation crystallization device evaporates and crystallizes mother liquor of the magnesium sulfate evaporation crystallizer and the sodium chloride crystallizer, and real zero emission is realized.
2. the method is characterized in that:
adding coagulant aid in front of the high-pressure cyclone, wherein the adding amount is 1 ~ 3ppm, the pressure of the high-pressure cyclone is more than PN40, the internal flow rate is 3m/s, the retention time is 30min, the overflow particle size D50 of the wastewater cyclone is less than 1.0 μm, the solid content is less than 5000ppm, and concentrated solution is discharged into the tail end of a vacuum belt conveyor and is separated from the underflow liquid of the original gypsum cyclone;
The rotation speed of a front mixing tank stirrer of the high-efficiency softener is more than 500rpm, the retention time is 5min, the linear speed of a flocculation tank stirrer of the high-efficiency softener is 5m/s, the variable frequency regulation is adopted, the retention time is more than 16min, the lifting amount is 15 ~ 20 times of water inflow, the retention time of a high-efficiency clarifier of the high-efficiency softener is more than 30min, and the clarification rising flow rate is 10 m/h;
calcium hydroxide and sodium hydroxide are respectively added into a front mixing tank of the high-efficiency softener, a PH meter is arranged at an outlet, the PH value is controlled to be about 9, sodium sulfate is added into a second front mixing tank, gypsum crystal seeds are simultaneously added to accelerate formation of CaCO 4, an HCO 3 - detector is arranged at an inlet of the front mixing tank and is linked with the addition of calcium hydroxide and sodium hydroxide, an online Ca hardness monitor and an online Mg hardness monitor are arranged at an outlet of the second front mixing tank, the Ca hardness is controlled to be 40Mg/L, the effluent suspended matter is less than 50ppm, the residence time of the front mixing tank is 10min, a high-efficiency composite inorganic adsorbent and sodium sulfate are added into a reaction zone of the high-efficiency softener, the addition of the high-efficiency composite inorganic adsorbent is 10 ~ 50ppm, the addition of the sodium sulfate is 1.05 times of CA ions, annular addition is adopted, a lifting mixing stirrer is adopted in the reaction zone, the linear speed is 5m/s, variable frequency regulation is adopted by a variable frequency motor, the residence time is 16min, the lifting amount is 15 ~ 20 times of inlet water, the high-efficiency clarifier of the whole high-efficiency softener is more than 30min, the rising residence time of the clarifier is 10 m/:
HCO3 -+OH+─→H2O
Ca2++CO3 2-─→CaCO3
Ca2++SO4 2-─→CaCO4
when the membrane filter filters, the desulfurization liquid passes through the membrane filter element, clear liquid penetrates through the membrane filter element and enters the upper cavity, solid in the liquid is completely intercepted on the surface of the membrane filter element to form a filter cake, because the membrane has excellent non-adhesiveness and a very small friction coefficient, and an automatic execution system is added, instantaneous reverse flow in seconds forms reverse cleaning, the filter cake is completely removed from the surface of the membrane filter element, the filter cake separated from the surface of the membrane filter element is deposited at the bottom of the filter, and when a certain amount of the filter cake is reached, the filter cake is quickly discharged from the bottom.
3. The hollow ultrafiltration membrane is made of PVDF membrane yarns with reinforcing ribs, the membrane yarns are allowed to swing freely in the membrane shell, the open structure of the hollow ultrafiltration membrane is favorable for scrubbing air and entering each membrane yarn, the intercepted solid is fully released, the water inlet pressure is more than 0.5Mpa, the water inlet suspended matter is 1 ~ 50mg/L, the COD is 10 ~ 100ppm, the effluent turbidity is 0.3NTU, and the SDI is less than 5;
the recovery rate of the NF device is more than 75 percent, when the NF device enters the NF device, the PH value of inlet water is controlled below 4, the Ca hardness is controlled to be 40mg/L, the pressure is 4.0Mpa, the desalination rate is more than 90 percent, due to the characteristics of the membrane, the NF device is connected with a direct current power supply to promote the separation of univalent ions and bivalent ions, the current of the NF device is 10A, the univalent ions and the bivalent ions are completely separated under the action of pressure and electrons, the bivalent ions are arranged on the concentrated water side, and the univalent ions are arranged on the water producing side;
Adjusting the pH value of concentrated water generated by an NF device to 4, adjusting the pH value of the concentrated water to 10000 ~ 60000ppm, mainly containing magnesium sulfate solution, concentrating by a magnesium sulfate concentration device, wherein the recovery rate is more than 80%, the produced water enters a secondary RO device, the concentrated water contains more than 200000ppm magnesium sulfate and enters a magnesium sulfate evaporation crystallizer, the operation stability of the concentrated water is controlled to 70 ~ 90 ℃, the operation pressure is-0.1 Mpa, the concentrated water enters a freezing separator after being saturated, calcium and magnesium are separated, the temperature is controlled to 0 ~ 20 ℃, and the magnesium sulfate heptahydrate is washed by secondary reverse osmosis produced water at the same time, so that the purity of the obtained magnesium sulfate heptahydrate is 98%, the magnesium sulfate concentration device is a membrane distillation device, and the magnesium sulfate evaporation crystallizer adopts an OSLO type and adopts a titanium material;
The flue evaporative crystallization device comprises two flue evaporative crystallization devices, one is flue direct injection, the other is a bypass flue, wherein discharged mother liquor of a magnesium sulfate evaporative crystallizer and a sodium chloride crystallizer enters the flue evaporative crystallization device, a gas-liquid bidirectional flow nozzle is adopted for circumferential tangential gas inlet, the gas directional pressure of the nozzle is 0.4 ~ 0.6.6 Mpa, the gas flow is 0.3 ~ 1Nm3/L water, the nozzle is made of PE, 10 mu m after atomization, 0.2t of a single nozzle is adopted, the density of the nozzle is 300%, the temperature of heated flue gas is 250 ~ 350 ℃, the outlet temperature is 100 ~ 345 ℃, the flow rate of the flue gas in flue evaporative crystallization is 5 ~ 10m/s, the bypass flue is provided with a bypass adjusting door which can be interlocked with the mother liquor, and a pressure side point, a flow rate measuring point and a temperature measuring point are arranged;
The effluent of the sodium bed is provided with a hardness meter and a conductivity meter, the hardness is controlled to be 40mg/L, the conductivity is less than 50000mg/L, and the regeneration liquid adopts concentrated water of a HIRO device;
adding a scale inhibitor into effluent of a sodium bed, adjusting the pH to 5, concentrating the effluent in a first-stage RO device, adjusting the pH of concentrated water to 5, feeding the concentrated water into a HIRO device, feeding the HIRO concentrated water into a sodium chloride crystallizer, and drying the obtained sodium chloride to obtain sodium chloride not lower than the standard of first-stage industrial salt;
The electrolysis device can generate byproducts of sodium hydroxide, chlorine dioxide and sodium hypochlorite after electrolysis according to needs, and waste liquid of the electrolysis device enters a sodium chloride crystallizer;
the scale inhibitor adopts inorganic composite scale inhibitors for preventing Ca, Mg, F and SiO2, and is added in front of an NF device, a primary RO device and a HIRO device at the same time, the pressure of the primary RO device is PN4.0Mpa ~ PN6.4Mpa, a high-pressure anti-pollution membrane is adopted, the flow channel is 45mil, the pressure of the HIRO device is PN16Mpa, a roll-type high-pressure wide-flow-channel anti-pollution membrane is adopted, the flow channel is 50mil, and the material is PVDF;
The high-efficiency adsorbent dosing device and the sodium sulfate dosing device are used for dosing dry powder;
Except for mother liquor discharge, evaporation is carried out, and the overall recovery rate of the system is more than 99%;
The filtering precision of the filter element is 1 mu m;
the water quality TDS of the desulfurization waste water is 8000 ~ 60000ppm, Mg2+ water is 500 ~ 10000ppm, Ca2+ is 100 ~ 10000ppm, SO 4 2-2000 ~ 20000ppm, Cl-is 1000 ~ 15000ppm, SiO2 is 10 ~ 500ppm, HCO 3-is 10 ~ 1000ppm, F-is 10 ~ 200ppm, SS is 30 ~ 20000ppm, COD is 30 ~ 300ppm, and the pH value is 5 ~ 9.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111533330A (en) * | 2020-06-05 | 2020-08-14 | 北京朗新明环保科技有限公司 | Industrial circulating water coupling softening crystallization treatment system and treatment method |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103382035A (en) * | 2013-08-01 | 2013-11-06 | 河北诺达化工设备有限公司 | Magnesium sulfate heptahydrate producing process with fully-continuous method |
| CN104805157A (en) * | 2015-05-28 | 2015-07-29 | 广西浦北制药厂 | Environment-friendly production method of trinosin |
| CN105858990A (en) * | 2016-06-15 | 2016-08-17 | 江苏海容热能环境工程有限公司 | Technology and device for preparing sodium hypochlorite solution with zero-emission saline solution of desulfurization waste water |
| CN107055579A (en) * | 2017-03-31 | 2017-08-18 | 中国神华能源股份有限公司 | The method that salt is reclaimed from desulfurization wastewater |
| CN107304090A (en) * | 2016-04-21 | 2017-10-31 | 广州市心德实业有限公司 | A kind of Resourceful treatment method for high-salinity wastewater of sodium chloride-containing and sodium sulphate |
| CN107640860A (en) * | 2017-10-09 | 2018-01-30 | 北京中科康仑环境科技研究院有限公司 | A kind of saliferous industrial wastewater desalination reuse technology of calcic magnesium ion, sulfate ion |
| CN107721033A (en) * | 2016-08-10 | 2018-02-23 | 通用电气公司 | The system and method for handling salt solution |
| CN107758962A (en) * | 2017-11-07 | 2018-03-06 | 博天环境工程（北京）有限公司 | A kind of system of the preparing magnesium sulfate from desulfurization wastewater |
-
2018
- 2018-05-30 CN CN201810537012.6A patent/CN110550792A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103382035A (en) * | 2013-08-01 | 2013-11-06 | 河北诺达化工设备有限公司 | Magnesium sulfate heptahydrate producing process with fully-continuous method |
| CN104805157A (en) * | 2015-05-28 | 2015-07-29 | 广西浦北制药厂 | Environment-friendly production method of trinosin |
| CN107304090A (en) * | 2016-04-21 | 2017-10-31 | 广州市心德实业有限公司 | A kind of Resourceful treatment method for high-salinity wastewater of sodium chloride-containing and sodium sulphate |
| CN105858990A (en) * | 2016-06-15 | 2016-08-17 | 江苏海容热能环境工程有限公司 | Technology and device for preparing sodium hypochlorite solution with zero-emission saline solution of desulfurization waste water |
| CN107721033A (en) * | 2016-08-10 | 2018-02-23 | 通用电气公司 | The system and method for handling salt solution |
| CN107055579A (en) * | 2017-03-31 | 2017-08-18 | 中国神华能源股份有限公司 | The method that salt is reclaimed from desulfurization wastewater |
| CN107640860A (en) * | 2017-10-09 | 2018-01-30 | 北京中科康仑环境科技研究院有限公司 | A kind of saliferous industrial wastewater desalination reuse technology of calcic magnesium ion, sulfate ion |
| CN107758962A (en) * | 2017-11-07 | 2018-03-06 | 博天环境工程（北京）有限公司 | A kind of system of the preparing magnesium sulfate from desulfurization wastewater |
Non-Patent Citations (1)
| Title |
|---|
| 祁鲁梁等: "《水处理工艺与运行管理实用手册》", 31 May 2002, 中国石化出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111533330A (en) * | 2020-06-05 | 2020-08-14 | 北京朗新明环保科技有限公司 | Industrial circulating water coupling softening crystallization treatment system and treatment method |
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