CN115038671A - Deep purification device and process for strong brine - Google Patents
Deep purification device and process for strong brine Download PDFInfo
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- CN115038671A CN115038671A CN202180006715.6A CN202180006715A CN115038671A CN 115038671 A CN115038671 A CN 115038671A CN 202180006715 A CN202180006715 A CN 202180006715A CN 115038671 A CN115038671 A CN 115038671A
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- 239000012267 brine Substances 0.000 title claims abstract description 76
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 76
- 238000000746 purification Methods 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 23
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- 239000002351 wastewater Substances 0.000 claims description 25
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 24
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- 238000001728 nano-filtration Methods 0.000 claims description 22
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- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims 4
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims 4
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- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims 1
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- 150000002500 ions Chemical class 0.000 claims 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims 1
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims 1
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- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
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- RSIJVJUOQBWMIM-UHFFFAOYSA-L sodium sulfate decahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.[Na+].[Na+].[O-]S([O-])(=O)=O RSIJVJUOQBWMIM-UHFFFAOYSA-L 0.000 description 2
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- 235000017166 Bambusa arundinacea Nutrition 0.000 description 1
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- 241001330002 Bambuseae Species 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 235000015334 Phyllostachys viridis Nutrition 0.000 description 1
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- CXKWCBBOMKCUKX-UHFFFAOYSA-M methylene blue Chemical compound [Cl-].C1=CC(N(C)C)=CC2=[S+]C3=CC(N(C)C)=CC=C3N=C21 CXKWCBBOMKCUKX-UHFFFAOYSA-M 0.000 description 1
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Images
Classifications
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- 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
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/16—Purification
-
- 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
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- 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
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- 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
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- 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
- C02F1/22—Treatment of water, waste water, or sewage by freezing
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- 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
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
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- 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
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- 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
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- 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
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- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
Abstract
The invention relates to a strong brine deep purification device and a process. The organic separation unit comprises an organic reaction tank and a membrane separation device; the organic reaction tank provides a mixed reaction space of strong brine and the combined medicament; the membrane separation device is a spiral-wound micro-filtration membrane and is used for removing organic components in the concentrated brine. The invention can remove the organic components before the salt separation of the concentrated brine by a simple and economic method aiming at the industrial wastewater treatment with high concentration and high organic matter content, TDS of 50000 mg/L-150000 mg/L and COD of more than or equal to 500mg/L, thereby allowing to obtain purer salt products, reducing the scale of a salt separation system and the investment operation cost and improving the economic benefit of the concentrated brine treatment.
Description
Technical Field
The invention relates to the field of purification and utilization of salt-containing wastewater resources, in particular to a purification device and a treatment process for separating salt and organic matters in high-concentration salt-containing wastewater.
Background
With the continuous development of economy, people put higher demands on good living environment. Because the energy structure and the water resource of China present the characteristic of 'reverse distribution', in the northwest region where coal and petroleum resources are rich, the problems of water resource shortage, serious water pollution, low water environment capacity and the like exist, so that the deep recycling of the production wastewater is necessary in the industrial fields of 'high water consumption and high energy consumption' such as coal chemical industry, medicine, coal-fired power plants and the like.
In the process of recycling the reclaimed water, the high-concentration salt-containing wastewater generated by concentration not only contains salts which can be recycled, such as chloride, sulfate, nitrate and the like, but also contains organic pollutants which have complex components and are difficult to treat. Before the salt separation treatment is carried out on the wastewater, organic matters in the wastewater need to be removed as much as possible, so that pure monovalent and divalent salt products with high utilization value can be obtained in the subsequent salt separation process.
At present, the removal mode of organic matters in the wastewater comprises mature means such as coagulation, biological oxidation, advanced oxidation and the like. However, the high concentration salt can inhibit the growth of microorganisms and even cause toxicity to the microorganisms, so that the biological oxidation technology is difficult to be applied in the high-salt wastewater treatment process; and the equipment investment cost and the operation and maintenance cost of advanced oxidation processes such as a Feton oxidation method, an electrocatalytic oxidation method, an ozone oxidation method and the like are high, and the industrial high-salinity wastewater with low added value and huge treatment amount is lack of cost advantage and is difficult to be widely applied. Coagulation is a widely used wastewater treatment process, but at present, the action mechanism of chemical coagulation is still not completely clear, and the coagulation effect is influenced by the components, concentration, water temperature, pH value, coagulant property, coagulation condition and the like of impurities in wastewater. The currently accepted coagulation mechanisms include: a compression double-electric layer theory, an adsorption bridging theory and a net capture theory.
Therefore, it is urgently needed to provide a wastewater treatment device and a wastewater treatment process for treating high-salinity wastewater in industries such as coal chemical industry and the like to obtain pure monovalent and divalent salts with high added values and realize zero discharge of wastewater.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a strong brine deep purification device and a process, which specifically comprise the following steps:
the utility model provides a strong brine degree of depth purification device, purification device includes former water tank, organic separation unit, one-level branch salt unit and second grade branch salt unit, and each unit is connected through pipeline and fluid pump.
The organic separation unit comprises an organic reaction tank and a membrane separation device; the raw water tank is used for receiving and storing strong brine to be purified and is connected with the organic reaction tank through a pipeline and a water inlet pump; the organic reaction tank provides a mixed reaction space of strong brine and the combined medicament; the water outlet of the organic reaction tank is connected with the membrane separation device through a pipeline and a water inlet pump of the membrane separation device, and the membrane separation device is a spiral-wound micro-filtration membrane and is used for removing organic components in the strong brine.
The organic separation unit also comprises a first intermediate water tank, a sludge dewatering device and a chemical cleaning device; the water inlet of the first intermediate water tank is communicated with the water outlet of the membrane separation device and is used for storing the strong brine from which the organic components are removed by the membrane separation device; the sludge dewatering device is connected with a sludge discharge port of the membrane separation device and is used for dewatering sludge which is intercepted by the membrane separation device and contains organic matters and combined medicaments; the chemical cleaning device is connected with the water inlet of the membrane separation device through a pipeline and is used for supplying chemical cleaning agent to the membrane separation device in the cleaning stage of the membrane separation device.
The first-stage salt separating unit comprises a cartridge filter, a first-stage salt separating device, a second middle water tank and a brine tank; the water outlet of the first intermediate water tank is connected with a cartridge filter through a pipeline and a first-level salt separation device lifting pump, and the water outlet of the cartridge filter is connected with the water inlet of the first-level salt separation device through a pipeline and a first-level salt separation device high-pressure pump so as to supply high-pressure strong brine to the first-level salt separation device; the first-stage salt separating device is a nanofiltration membrane; the water inlet of the security filter is connected with a scale inhibitor feeding device; the water inlet and outlet of the primary salt separating device are connected with a membrane cleaning device; the concentrated water (referred to as intercepted water) of the first salt separating device is connected with the water inlet of the second intermediate water tank through a pipeline; the produced water (referred to as permeated water) of the primary salt separation device is connected with the brine pond through a pipeline.
The first-stage salt separation device adopts a nanofiltration membrane made of one or a combination of polyamides, polysulfones and cellulose acetates.
The second-stage salt separating unit comprises a second-stage salt separating device and a mirabilite pool; the water outlet of the second intermediate water tank is connected with the water inlet of the secondary salt separation device through a pipeline and a lifting pump of the secondary salt separation device; the second-stage salt separation device is a freezing and crystallizing device which is used for freezing and crystallizing concentrated water (mainly containing divalent sodium sulfate) generated by the first-stage salt separation device to generate mirabilite (Na) 2 SO 4 ·10H 2 O crystal) is conveyed to a mirabilite pool by a conveying belt and a conveying pump, and mother liquor generated by a secondary salt separation device is conveyed to a raw water tank by a pipeline.
Preferably, a pretreatment unit is further included between the organic reaction tank and the raw water tank, and the pretreatment unit is used for removing total hardness and soluble silicon in the concentrated brine.
As shown in fig. 2, a method for purifying concentrated brine based on the concentrated brine advanced purification device is provided, which comprises the following steps:
s1, conveying strong brine wastewater to be treated to a raw water tank;
s2, conveying the wastewater in the raw water tank to an organic separation unit; the concentrated brine containing organic components from a raw water tank is firstly conveyed into an organic reaction tank, mixed with a combined medicament added into the organic reaction tank, subjected to coagulation and adsorption combined reaction, and then conveyed to an organic separation device consisting of a roll type microfiltration membrane; the organic components after reaction are intercepted by the roll-type microfiltration membrane so as to be removed from the concentrated brine;
s3, after the treatment of the organic separation unit, respectively conveying the produced water and sludge to a primary salt separation unit and a sludge dewatering device;
s4, respectively conveying the produced water and the concentrated water treated by the primary salt separating unit to a brine pond and a secondary salt separating unit; monovalent salt in the concentrated brine can penetrate through the nanofiltration membrane, and divalent salt is trapped by the nanofiltration membrane, so that the monovalent salt and the divalent salt in the concentrated brine are separated; conveying the monovalent salt penetrating through the nanofiltration membrane to a brine tank; the divalent salt trapped by the nanofiltration membrane is conveyed to a secondary salt separation unit;
s5, after the treatment of the secondary salt separation device, conveying the generated mirabilite to a mirabilite pool, and conveying the mother liquor to a raw water tank; the second-stage salt separating device is used for freezing and crystallizing the divalent salt solution generated by the first-stage salt separating device to generate sodium sulfate decahydrate crystals, namely mirabilite; and (3) conveying the mirabilite to a mirabilite pool, and conveying the mother liquor generated in the crystallization process to a raw water tank to be mixed with strong brine to be treated so as to improve the overall yield of the mirabilite.
The crystallization temperature of the secondary salt separation unit is-15 ℃ to 5 ℃.
Compared with the prior art, the invention can at least obtain the following beneficial effects:
the method firstly removes the organic components of the strong brine before the salt separation treatment of the strong brine, and effectively removes the organic components of the strong brine through the treatment mode of the microfiltration membrane and the combined medicament; through multiple groups of comparative experiments, the combination of the wood activated carbon powder and the polyferric coagulant is creatively found to obtain a better COD removal effect, and no flocculant is required to be added after industrial amplification application;
the invention discovers that when the polymeric aluminum ferric silicate coagulant is used independently, the polymeric aluminum ferric silicate coagulant has little effect on removing COD in the concentrated brine, and when the polymeric aluminum ferric silicate coagulant and the polymeric ferric silicate coagulant are compounded according to a certain proportion and then matched with the wood activated carbon powder, the removal rate of COD can be further greatly improved on the basis of only the wood activated carbon powder and the polymeric ferric combined medicament;
the organic separation unit can realize that the COD removal rate reaches more than 30% under the condition of a certain feeding amount ratio of the adsorbent to the coagulant, and the organic separation unit is further matched with subsequent nanofiltration and crystallization treatment, so that the total salt recovery rate in the strong salt industrial wastewater is more than or equal to 90%, and the COD removal rate is more than or equal to 50%;
aiming at the industrial wastewater treatment with high concentration and high organic matter content, wherein TDS is 50000 mg/L-150000 mg/L, COD is more than or equal to 500mg/L, the invention creatively discovers the combined medicament, and can remove the organic components before the salt separation of the concentrated brine by a simple and economic method, thereby allowing the acquisition of a relatively pure salt product, reducing the scale of a salt separation system and the investment operation cost, and improving the economic benefit of the concentrated brine treatment.
Drawings
FIG. 1 is a schematic view of the deep purification apparatus according to the present invention;
FIG. 2 is a flow diagram illustrating the purification of concentrated brine by the purification apparatus.
Detailed Description
As shown in figure 1, a deep purification device for concentrated brine is provided, which comprises a raw water tank (101), an organic separation unit, a primary salt separation unit and a secondary salt separation unit, wherein the units are connected through a pipeline and a liquid pump.
The above-mentioned
IncludedOrganic reaction tank (103)Andmembrane separation device (105)) (ii) a The raw water tank (101) is used for receiving and storing strong brine to be purified and is connected with the organic reaction tank (103) through a pipeline and a water inlet pump (102); the organic reaction tank (103) provides a mixed reaction space of concentrated brine and the combined medicament; the water outlet of the organic reaction tank (103) is connected with a membrane separation device (105) through a pipeline and a water inlet pump (104) of the membrane separation device, and the membrane separation device (105) is a roll-type microfiltration membrane which is used for removing organic components in concentrated brine.
The organic separation unit further comprises a first intermediate water tank (106), a sludge dewatering device (107) and a chemical cleaning device (108); the water inlet of the first intermediate water tank is communicated with the water outlet of the membrane separation device (105) and is used for storing the strong brine from which the organic components are removed by the membrane separation device (105); the sludge dewatering device (107) is connected with a sludge discharge port of the membrane separation device (105) and is used for dewatering sludge containing organic matters and combined agents intercepted by the membrane separation device (105); the chemical cleaning device (108) is connected with the water inlet of the membrane separation device through a pipeline and is used for supplying chemical cleaning agent to the membrane separation device (105) in the cleaning stage of the membrane separation device.
The primary salt separation unit comprises a cartridge filter (202), a primary salt separation device (204), a second intermediate water tank (205) and a brine tank (206); the water outlet of the first intermediate water tank (106) is connected with a cartridge filter (202) through a pipeline and a first-level salt separation device lifting pump (201), the water outlet of the cartridge filter (202) is connected with the water inlet of a first-level salt separation device (204) through a pipeline and a first-level salt separation device high-pressure pump (203) to supply high-pressure concentrated brine to the first-level salt separation device (204); the primary salt separating device (204) is a nanofiltration membrane; a water inlet of the cartridge filter (202) is connected with a scale inhibitor adding device (207); the water inlet and outlet of the primary salt separating device (204) are connected with a membrane cleaning device (208); the concentrated water (referred to as intercepted water) of the primary salt separating device (204) is connected with the water inlet of a second intermediate water tank (205) through a pipeline; the produced water (referred to as permeate water) of the primary salt separation device (204) is connected with the brine pool (206) through a pipeline.
The nanofiltration membrane adopted by the first-stage salt separating device (204) is made of one or the combination of polyamides, polysulfones and cellulose acetate.
The second-stage salt separating unit comprises a second-stage salt separating device (302) and a mirabilite pool (304); the water outlet of the second intermediate water tank (205) is connected with the water inlet of the second-stage salt separating device (302) through a pipeline and a second-stage salt separating device lifting pump (301); the second-stage salt separation device (302) is a freezing crystallization device, and is used for freezing and crystallizing concentrated water (mainly containing divalent sodium sulfate) generated by the first-stage salt separation device to generate mirabilite (Na) 2 SO 4 ·10H 2 O crystal) is sent to a mirabilite pool (304) through a conveyer belt and a transfer pump (303), and mother liquor generated by a secondary salt separation device (302) is transferred to a raw water tank (101) through a pipeline.
Preferably, a pretreatment unit is further included between the organic reaction tank (103) and the raw water tank (101), and the pretreatment unit is used for removing total hardness and soluble silicon in concentrated brine.
As shown in fig. 2, a method for purifying concentrated brine based on the concentrated brine advanced purification device is provided, which comprises the following steps:
s1, conveying strong brine wastewater to be treated to a raw water tank (101);
s2, conveying the wastewater in the raw water tank (101) to an organic separation unit; concentrated brine containing organic components from a raw water tank (101) is firstly conveyed into an organic reaction tank (103), mixed with a combined medicament added into the organic reaction tank (103) and subjected to coagulation and adsorption combined reaction, and then conveyed to an organic separation device (105) consisting of a roll type microfiltration membrane; the organic components after reaction are intercepted by the roll-type micro-filtration membrane, so that the organic components are removed from the concentrated brine;
s3, after being treated by the organic separation unit, the produced water and sludge are respectively conveyed to a primary salt separation unit and a sludge dewatering device (107);
s4, respectively conveying the produced water and the concentrated water treated by the primary salt separating unit to a brine pond (206) and a secondary salt separating unit; monovalent salt in the concentrated brine can penetrate through the nanofiltration membrane, and divalent salt is trapped by the nanofiltration membrane, so that the monovalent salt and the divalent salt in the concentrated brine are separated; the monovalent salt that permeates through the nanofiltration membrane is transported to a brine tank (206); the divalent salt trapped by the nanofiltration membrane is conveyed to a secondary salt separation unit;
s5, after the treatment of the second-stage desalting device (302), conveying the generated mirabilite to a mirabilite pool (304), and conveying the mother liquor to a raw water tank (101); the second-stage salt separating device (302) is used for freezing and crystallizing the divalent salt solution generated by the first-stage salt separating device (204) to generate sodium sulfate decahydrate crystals, namely mirabilite; and (3) conveying the mirabilite to a mirabilite pool (304), and conveying the mother liquor generated in the crystallization process to a raw water tank (101) to be mixed with the strong brine to be treated so as to improve the overall yield of the mirabilite.
Organic separation unit process screening experiment
The organic separation unit in the concentrated brine deep purification device is adopted to treat typical concentrated brine wastewater in coal chemical industry, and the treatment effects under different process conditions are inspected. The salt content of the concentrated salt wastewater is 5.1%, wherein the main salts are sodium sulfate and sodium chloride, sulfate radical 8250mg/L, chloride radical 23850mg/L, the total hardness is 10mg/L, and soluble silicon is 20 mg/L.
Firstly injecting coal chemical industry strong brine into a raw water tank (101) for temporary storage, and then removing the total hardness and soluble silicon in the strong brine through a pretreatment device; the pretreated strong brine is conveyed to an organic reaction tank (103).
Example 1
Adsorbent, single-component coagulant and microfiltration membrane filtration(pore diameter of the membrane: 0.3 μm)And (5) carrying out experiments.
Polyferric (namely PFS (polyferric sulfate) coagulant) and powdered activated carbon adsorbent are added into the organic reaction tank (103); the activated carbon powder adsorbent is as follows: TY-120 (woody charcoal for sugar, 200 mesh, methylene blue decolorizing power > 120ml/g, Shanghai activated carbon plant Co., Ltd.) or MZ-800 (coal charcoal, 200 mesh, iodine value: 800mg/g, Zhengzhou bamboo forest activated carbon development Co., Ltd.).
The COD removal rates before and after the reaction were examined according to the following conditions, respectively:
A. the adding amount is as follows: 500mg/L TY-120 powdered carbon and 250mg/L polyferric PFS; the COD of the inlet water is 1061.4mg/L, the COD of the outlet water is 813.4mg/L, and the removal rate of the COD is 23.4 percent;
B. the adding amount is as follows: MZ-800 powdered carbon 500mg/L, polyferric PFS-250 mg/L; the COD of the inlet water is 1061.4mg/L, the COD of the outlet water is 892.8mg/L, and the removal rate of the COD is 15.9 percent;
C. the adding amount is as follows: 750mg/L of TY-120 powdered carbon, 250mg/L of polyferric PFS, 952.3mg/L of COD in inlet water, 724.2mg/L of COD in outlet water and 24.9% of COD removal rate;
example 2
Adsorbent, single-component coagulant and microfiltration membrane filtration(pore diameter of membrane 0.1. mu.m)And (5) carrying out experiments.
The adding amount is as follows: 750mg/L of TY-120 powdered carbon, 250mg/L of polyferric PFS, 1126.9mg/L of COD in inlet water, 873mg/L of COD in outlet water and 26.3% of COD removal rate.
Example 3
Adsorbent and method of making same+ compounded coagulantAnd (3) performing microfiltration membrane filtration (membrane pore size is 0.3 mu m).
The adding amount is as follows: 500mg/L of TY-120 powdered carbon,poly iron PFS-50mg/L, poly aluminum ferric silicate50mg/L, inlet water COD is 248mg/L, outlet water COD is 156mg/L, and COD removal rate is 37%.
Comparative example 1
Adsorbent + microfiltration membrane filtration (membrane pore size 0.3 μm).
The adding amount is as follows: 750mg/L of TY-120 powdered carbon, 1539mg/L of COD in inlet water, 1325mg/L of COD in outlet water and 14.0% of COD removal rate.
Comparative example 2
Coagulant + microfiltration membrane filtration (membrane pore size 0.3 μm).
A. The adding amount is as follows: PFS-300mg/L, COD of inlet water is 153mg/L, COD of outlet water is 120mg/L, and removal rate of COD is 21.6%;
B. the polymeric aluminum ferric silicate is 300mg/L, the COD is 153mg/L, the effluent COD is 151mg/L, and the removal rate of the COD is 1.3 percent.
Separation experiment of deep purification device
Example 4
In this embodiment, the advanced purification apparatus is adopted to treat typical concentrated salt wastewater in coal chemical industry, that is, after the concentrated salt wastewater is treated by the organic separation unit, the concentrated salt wastewater is subjected to nanofiltration by the primary salt separation unit and crystallization by the secondary salt separation apparatus, and then the COD removal rate (referring to the COD removal rate of the COD in the brine pond compared with the raw water COD) and the total salt recovery rate before and after treatment are examined.
In this embodiment, the organic separation device uses a roll-type microfiltration membrane with a membrane pore size of 0.1 μm; the first-stage salt separation device adopts a nanofiltration membrane, and the water inlet pressure of the first-stage salt separation device is 6.5 MPa.
The water inflow of the strong salt wastewater in certain coal chemical industry is 40m 3 H, salt content 5.1% wt, main salts are sodium sulfate and sodium chloride; in raw water: 8250mg/L of sulfate radical, 23850mg/L of chloride radical, 979mg/L of COD, 10mg/L of total hardness and 20mg/L of soluble silicon.
The strong brine is pretreated to remove total hardness and soluble silicon and then enters an organic separation unit, and the adding amount is as follows:TY-120 750mg/L of powdered carbon, 250mg/L of polyferric PFS,after coagulation, adsorption and microfiltration membrane filtration, the product enters a first-stage salt separation unit through pressurization.
After being treated by a first-stage salt separation device, the salt-water ratio (as Cl) of the produced water - /SO 4 2- Mass ratio) of 66, and the retention rate of sulfate radicals of 96 percent; the main salt in the produced brine is sodium chloride, the salt content is 4%, the COD is 433mg/L, the retention rate of the COD is about 55%, and the total salt recovery rate is about 97%.
The retention effect of the organic matter of 1000Da is obvious; in addition, the organic separation unit has obvious removal effect on hydrophobic neutral organic matters, hydrophilic organic matters and hydrophobic basic organic matters, and the primary nanofiltration salt separation unit mainly has obvious interception effect on hydrophobic acidic organic matters. The organic separation unit and the first-stage salt separation unit are complementary in the aspects of the molecular weight grade and the organic property of the organic matter removal, and the organic separation unit and the first-stage salt separation unit can better remove the organic matter in the wastewater in a synergistic manner.
Part of hydrophobic acidic organic matters permeate the organic separation unit, are intercepted by the nano-filtration salt separation unit, flow into a freezing crystallization device of a secondary salt separation unit along with a divalent salt solution, and are still remained in mother liquor after freezing crystallization, and mirabilite is precipitated in a crystal form, so that the mirabilite is separated from the part of organic matters, and the generated mirabilite can be further used for producing high-purity sodium sulfate.
The relevant parameters of the above embodiment are shown in table 1:
TABLE 1
As can be seen from Table 1:
based on the A, B experimental results in example 1, the combined preparation of TY-120 and poly-iron PFS has higher COD removal rate than the combined preparation of MZ-800 and poly-iron PFS;
based on the experimental result of the item C in the example 1 and the experimental result of the comparative example 1, the TY-120 added powdered carbon and the polyferric combined medicament have higher COD removal rate than the TY-120 added powdered carbon alone;
based on the two experimental results of A, C in example 1 and A in comparative example 2, the added TY-120 powdered carbon and polyferric combined medicament has higher COD removal rate than that of singly added polyferric;
based on the two experimental results of A, B in the comparative example 2, the good COD removal rate can be obtained by adding the polyferric coagulant alone; the effect of adding the polyaluminum ferric silicate coagulant alone on removing COD in the concentrated brine is not obvious;
based on the experimental results of the examples 1-3 and the comparative example 2, although the effect of adding the polyaluminum ferric silicate alone on removing COD is not obvious, the polyaluminum ferric silicate is compounded with the polyferric according to a certain proportion and then matched with TY-120 powdered carbon, so that the removal rate of COD can be greatly improved;
based on the experimental results of the embodiment 4 and the embodiments 1 to 3, the removal rate of COD in the obtained brine can reach 55% after the organic separation unit treatment and the nano-filtration salt separation.
Further, the effect of the addition of different adsorbents TY-120 powdered carbon and coagulant polyferric PFS on the COD removal effect is examined, the COD of the inlet water is 1061.4mg/L, the result is shown in Table 2, the adsorbents and the polyferric PFS achieve good COD removal rate in a large addition proportion range, and especially under the condition that the weight ratio of the adsorbents to the coagulant is more than 3:1, the COD removal rate can reach more than 30%.
TABLE 2
The above description is only an example of the preferred embodiment of the present invention, and not a limitation to all possible embodiments of the present invention, and those skilled in the art can easily make various modifications, substitutions and alterations without departing from the spirit and scope of the present invention; the actual scope of the invention is subject to the limitations of the claims.
Claims (11)
1. The utility model provides a strong brine degree of depth purification device which characterized in that: comprises an organic separation unit, wherein the organic separation unit adopts a roll type microfiltration membrane, and the membrane aperture is less than or equal to 0.3 mu m; a combined medicament composed of an adsorbent and a coagulant is used in a matching way; the combined medicament is added into the concentrated saline on the upstream side of the rolled microfiltration membrane and is fully mixed and reacted with the concentrated saline.
2. The concentrated brine deep purification device according to claim 1, characterized in that: the adsorbent is activated carbon and/or activated coke, and the coagulant is one or more of polymeric aluminum ferric silicate, polymeric ferric chloride, polymeric ferric sulfate, polymeric aluminum chloride, polymeric aluminum sulfate and ferrous sulfate.
3. The concentrated brine deep purification device according to claim 2, characterized in that: the coagulant comprises polymeric ferric sulfate.
4. The concentrated brine deep purification device according to claim 2, characterized in that: the coagulant is a mixture of polymeric ferric sulfate and polymeric aluminum ferric silicate, and the mass ratio of the polymeric ferric sulfate to the polymeric aluminum ferric silicate is more than or equal to 1.
5. The concentrated brine deep purification device according to any one of claims 1 to 4, characterized in that: also comprises a primary salt separating unit and a secondary salt separating unit.
6. The concentrated brine deep purification device according to claim 5, characterized in that: the first-stage salt separation unit comprises a nanofiltration membrane and a high-pressure pump, and the high-pressure pump can provide water inlet pressure which is more than or equal to 4.1MPa to the nanofiltration membrane; the secondary salt fractionation unit comprises a crystallization device.
7. The concentrated brine deep purification device according to claim 6, characterized in that: the nanofiltration membrane is made of one or the combination of polyamides, polysulfones and cellulose acetate, and the rejection rate of the nanofiltration membrane on multivalent ions is more than or equal to 96 percent.
8. The concentrated brine deep purification device according to claim 5, characterized in that: the upstream of the organic separation unit also includes a pretreatment unit for removing the total hardness and soluble silicon of the concentrated brine.
9. A method of purifying concentrated brine using the purification apparatus of any one of claims 1 to 8, comprising the steps of:
s1, conveying strong brine wastewater to be treated to a raw water tank;
s2, conveying the wastewater in the raw water tank to an organic separation unit, adding a combined medicament consisting of an adsorbent and a coagulant into the wastewater, mixing and reacting, and filtering by using a spiral-wound microfiltration membrane.
10. The method of purifying a concentrated brine according to claim 9, further comprising the steps of:
s3, after being treated by the organic separation unit, the produced water and sludge are respectively conveyed to a primary salt separation unit and a sludge dewatering device;
s4, respectively conveying the produced water and the concentrated water treated by the primary salt separating unit to a brine pond and a secondary salt separating unit;
s5, after the treatment of the secondary salt separation device, the produced mirabilite is conveyed to a mirabilite pool, and the mother liquor is conveyed to a raw water tank.
11. The method of claim 10, wherein: the crystallization temperature of the secondary salt separation unit is-15 ℃ to 5 ℃.
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|---|---|---|---|---|
| CN115465929A (en) * | 2022-09-27 | 2022-12-13 | 湖南邦德博鑫环保科技有限公司 | High-salinity wastewater treatment process |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH09108692A (en) * | 1995-10-20 | 1997-04-28 | Ataka Kogyo Kk | Treatment of organic waste water and device therefor |
| CN105016530A (en) * | 2015-08-07 | 2015-11-04 | 沧州绿源水处理有限公司 | Comprehensive treatment process of waste water high in concentration and high in salinity |
| WO2020010678A1 (en) * | 2018-07-10 | 2020-01-16 | 中冶华天南京工程技术有限公司 | Novel material for in-situ decontamination of turbid river water and preparation method thereof |
| CN110734170A (en) * | 2019-10-13 | 2020-01-31 | 麦王环境技术股份有限公司 | deep purification device and treatment process for concentrated salt water |
| CN111517389A (en) * | 2020-05-14 | 2020-08-11 | 崔玉祥 | COD (chemical oxygen demand) remover and using method thereof |
| CN111807490A (en) * | 2020-07-16 | 2020-10-23 | 众意环保科技(大连)有限公司 | Combined medicament for removing COD (chemical oxygen demand) and decoloring coking wastewater advanced treatment and application |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU2003200855A1 (en) * | 2002-03-05 | 2003-09-25 | Qed Occtech Ltd | A Process and System for Reducing Arsenic Levels in Aqueous Solutions |
| AT501991B1 (en) * | 2005-06-10 | 2007-04-15 | Adler Herwig Dipl Ing | METHOD FOR THE TREATMENT OF WASTE FROM OLIVE OIL PRODUCTION |
| CN104355376A (en) * | 2014-10-20 | 2015-02-18 | 苏州富奇诺水治理设备有限公司 | Coagulant for industrial water pretreatment |
| CN110467251A (en) * | 2019-09-09 | 2019-11-19 | 上海电力大学 | A kind of composite water treatment agent and the preparation method and application thereof |
-
2021
- 2021-05-28 CN CN202180006715.6A patent/CN115038671A/en active Pending
- 2021-05-28 WO PCT/CN2021/096897 patent/WO2022246823A1/en unknown
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH09108692A (en) * | 1995-10-20 | 1997-04-28 | Ataka Kogyo Kk | Treatment of organic waste water and device therefor |
| CN105016530A (en) * | 2015-08-07 | 2015-11-04 | 沧州绿源水处理有限公司 | Comprehensive treatment process of waste water high in concentration and high in salinity |
| WO2020010678A1 (en) * | 2018-07-10 | 2020-01-16 | 中冶华天南京工程技术有限公司 | Novel material for in-situ decontamination of turbid river water and preparation method thereof |
| CN110734170A (en) * | 2019-10-13 | 2020-01-31 | 麦王环境技术股份有限公司 | deep purification device and treatment process for concentrated salt water |
| CN111517389A (en) * | 2020-05-14 | 2020-08-11 | 崔玉祥 | COD (chemical oxygen demand) remover and using method thereof |
| CN111807490A (en) * | 2020-07-16 | 2020-10-23 | 众意环保科技(大连)有限公司 | Combined medicament for removing COD (chemical oxygen demand) and decoloring coking wastewater advanced treatment and application |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115465929A (en) * | 2022-09-27 | 2022-12-13 | 湖南邦德博鑫环保科技有限公司 | High-salinity wastewater treatment process |
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