CN112875930A - Method for purifying high-salt and high-concentration wastewater by multi-stage membrane permeation method - Google Patents
Method for purifying high-salt and high-concentration wastewater by multi-stage membrane permeation method Download PDFInfo
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- 239000012528 membrane Substances 0.000 title claims abstract description 108
- 239000002351 wastewater Substances 0.000 title claims abstract description 99
- 238000000034 method Methods 0.000 title claims abstract description 44
- 238000002425 crystallisation Methods 0.000 claims abstract description 116
- 230000008025 crystallization Effects 0.000 claims abstract description 115
- 238000005189 flocculation Methods 0.000 claims abstract description 81
- 230000016615 flocculation Effects 0.000 claims abstract description 81
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 51
- 239000007788 liquid Substances 0.000 claims abstract description 38
- 238000000746 purification Methods 0.000 claims abstract description 29
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 27
- 230000007246 mechanism Effects 0.000 claims abstract description 25
- 239000012466 permeate Substances 0.000 claims abstract description 24
- 239000011780 sodium chloride Substances 0.000 claims abstract description 14
- 239000012982 microporous membrane Substances 0.000 claims description 25
- 238000005086 pumping Methods 0.000 claims description 25
- 239000013078 crystal Substances 0.000 claims description 24
- 238000001728 nano-filtration Methods 0.000 claims description 23
- 238000000108 ultra-filtration Methods 0.000 claims description 21
- 239000008213 purified water Substances 0.000 claims description 17
- 239000004576 sand Substances 0.000 claims description 16
- 238000001914 filtration Methods 0.000 claims description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 4
- 239000002910 solid waste Substances 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 2
- 230000008569 process Effects 0.000 abstract description 9
- 238000005374 membrane filtration Methods 0.000 abstract description 6
- 150000003839 salts Chemical class 0.000 abstract description 5
- 239000010865 sewage Substances 0.000 abstract description 3
- 239000002245 particle Substances 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 22
- 238000005188 flotation Methods 0.000 description 7
- 229920002401 polyacrylamide Polymers 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 5
- 239000000460 chlorine Substances 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 229910017053 inorganic salt Inorganic materials 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- -1 salt ions Chemical class 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000007832 Na2SO4 Substances 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- 238000011001 backwashing Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 239000013527 degreasing agent Substances 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- CSNNHWWHGAXBCP-UHFFFAOYSA-L magnesium sulphate Substances [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
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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
- 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
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- 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
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
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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
-
- 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
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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
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- 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
- C02F1/5281—Installations for water purification using chemical 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
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- 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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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/05—Conductivity or salinity
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- Engineering & Computer Science (AREA)
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to a method for purifying high-salinity high-concentration wastewater by a multi-stage membrane permeation method, belonging to the technical field of water treatment. The invention carries out flocculation purification in a flocculation purification mechanism, permeate liquid of the wastewater after the flocculation purification is collected by a multi-stage membrane filtration mechanism, and concentrated solution flows back to the flocculation purification mechanism to continue the flocculation purification step. According to the invention, after the early flocculation treatment, organic matters are removed in advance, so that the pressure of the subsequent membrane treatment is reduced, in the membrane treatment process, inorganic matters and macromolecular particles are continuously separated step by step to obtain saline wastewater with improved concentration, and salt is removed from the wastewater through crystallization, so that the sewage treatment is realized.
Description
Technical Field
The invention relates to a method, in particular to a method for purifying high-salt high-concentration wastewater by a multi-stage membrane permeation method, belonging to the technical field of water treatment.
Background
With the development of industry, the problems of environmental pollution and water resource shortage are becoming more serious. Therefore, it is very important to develop a novel water treatment technology for industrial wastewater treatment, recovery of pure water and valuable solute resources, and realization of near zero emission and resource recycling of wastewater. The high-salinity wastewater is always the key point of industrial wastewater treatment due to the characteristics of large discharge amount, high salinity, strong environmental destruction and the like. The high-concentration Na +, Mg2 +/Cl aqueous solution is typical high-salinity wastewater, the wastewater is mainly treated by firstly concentrating and then evaporating and crystallizing at present, the operation energy consumption is always high due to high evaporation and crystallization operation temperature and uncontrollable crystallization supersaturation degree in an evaporator, the controllability of the crystallization process is poor, the product purity is low, and a large amount of solid waste and hazardous waste byproducts are generated in the process treatment.
The membrane separation-crystallization technology is a novel water treatment and crystallization coupling separation technology, and can realize the synchronous recovery of pure water and valuable salt. Compared with the traditional reverse osmosis and multiple-effect evaporation technologies, the membrane distillation has a plurality of remarkable advantages. However, the membrane separation process tends to be prone to clogging, resulting in a reduction in separation efficiency and efficiency.
The invention discloses an invention patent named as a high-salt high-COD wastewater recycling zero-discharge system and a process in Chinese patent with publication number CN110526512A, publication number is 03/12/2019. The high-salt high-COD wastewater recycling zero-discharge process comprises the following steps: step one, removing COD, total nitrogen, SS and heavy metal ions from high-salt high-COD wastewater through pretreatment; step two, performing double-stage concentration on the pretreated wastewater to obtain a high-concentration Na2SO4 solution and a NaCl solution through RONFNFRO concentration; and step three, filtering the high-concentration Na2SO4 solution and the NaCl solution by using a high-pressure flat membrane, and evaporating and concentrating to obtain the crystalline salt with the purity of more than 99%. Although the process is progressive for treating the high-salinity wastewater layer by layer, the whole process has no wastewater discharge, can remove characteristic target pollutants, can ensure the water inlet requirement of the next reaction, and has the wastewater recovery rate close to 100 percent; however, the method adopts the way of concentrating and then evaporating for crystallization, so that the method still has the defects.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide the method for purifying the high-salinity high-concentration wastewater by the multistage membrane permeation method, which is convenient to operate, stable, reliable, good in sewage treatment and purification effect and good in applicability.
The technical scheme adopted by the invention for solving the problems is as follows: the method for purifying the high-salt and high-concentration wastewater by the multistage membrane permeation method comprises the step of flocculation purification in a flocculation purification mechanism, and is characterized in that: and collecting permeate of the wastewater subjected to flocculation purification after passing through a multi-stage membrane filtering mechanism, and refluxing the concentrated solution to a flocculation purification mechanism to continue to perform a flocculation purification step.
Preferably, the multistage membrane filtering mechanism comprises a crystallization tank, a crystallization residual liquid storage tank, a purified water storage tank, and a microporous membrane component, an ultrafiltration membrane component, a nanofiltration membrane component and an RO membrane component which are sequentially connected; the flocculation purification mechanism comprises a solid-liquid separator, an air flotation oil remover, a sand filter, a flocculation tank and a flocculation wastewater storage tank connected with the flocculation tank, the flocculation wastewater storage tank is connected with the water inlet end of the microporous membrane component, and concentrated solution outlets of the microporous membrane component, the ultrafiltration membrane component, the nanofiltration membrane component and the RO membrane component are respectively connected with the flocculation wastewater storage tank; the crystallization tank is connected with a permeate outlet of the nanofiltration membrane component, the crystallization tank is connected with a crystallization residual liquid storage tank, the crystallization residual liquid storage tank is connected with a water inlet end of the RO membrane component, and a permeate outlet of the RO membrane component is connected with a purified water storage tank; the discharge port of the solid-liquid separator is connected with the discharge port of the flocculation tank, the discharge port of the solid-liquid separator is connected with the air floatation oil remover, the discharge port of the air floatation oil remover is connected with the sand filter, and the discharge port of the sand filter is connected with the flocculation wastewater storage tank.
Preferably, the purification method comprises the following specific steps: after the wastewater enters a flocculation tank, adding a polyferric sulfate flocculant and PAM (polyacrylamide) into the flocculation tank, adding NaOH solution to adjust the pH of the wastewater to 7-9, stirring for 5-10min, pumping the wastewater into a solid-liquid separator for solid-liquid separation, treating the separated solid as solid waste, removing oil from the wastewater by an air floatation oil remover, filtering the deoiled wastewater by a sand filter, and storing the wastewater by a flocculation wastewater storage tank, wherein the weight ratios of the polyferric sulfate flocculant, the PAM and the wastewater in the flocculation tank are respectively 0.1-2 wt: 1 and 0.1-1 wt% o: 1; pumping wastewater in a flocculation wastewater storage tank into a water inlet end of a microporous membrane component by a pump, pumping concentrated solution of the microporous membrane component into the flocculation wastewater storage tank, pumping permeate into a water inlet end of an ultrafiltration membrane component by the pump, pumping concentrated solution of the ultrafiltration membrane component into the flocculation wastewater storage tank, pumping permeate into a water inlet end of a nanofiltration membrane component, pumping concentrated solution of the nanofiltration membrane component into the flocculation wastewater storage tank, pumping wastewater in a crystallization tank into a crystallization residual solution storage tank after the permeate enters a crystallization tank and stands for 5-24 hours, pumping wastewater in the crystallization residual solution storage tank into a water inlet end of an RO membrane component by the pump, pumping concentrated solution of the RO membrane component into the flocculation wastewater storage tank, and pumping the permeate into a purified water storage tank.
Preferably, a plurality of crystallization columns are arranged in the crystallization tank, a crystal blanking sleeve capable of reciprocating along the axial direction of the crystallization columns is sleeved on each crystallization column, and a discharging manhole is arranged at the bottom of each crystallization tank.
Preferably, the crystallization column is hollow, the bottom of the crystallization column is sealed, the top of the crystallization column is open, crystallization holes are densely distributed in the crystallization column, and NaCl and MgSO is filled in the crystallization column4The crystal blanking sleeve is annular, a gap is formed between the inner wall of the annular crystal blanking sleeve and the outer wall of the crystal column, and the crystal blanking sleeve is fixedly connected with a lifting rod.
Preferably, NaCl and MgSO are present in the crystallization column according to the invention4In a molar ratio of 1:1, and a plurality of crystallization columns are arranged in the crystallization tank in an annular array.
Preferably, after the liquid in the crystallization tank is completely filled into the storage tank for the residual crystallization liquid, the crystal discharging sleeve is extracted up and down, the crystal on the crystallization column is scraped from the crystallization column, and NaCl and MgSO (MgSO) are supplemented into the crystallization column4The discharge manhole is opened, and the crystal is taken out from the crystallizing tank.
Preferably, the filter diameters of the microporous membrane component, the ultrafiltration membrane component, the nanofiltration membrane component and the RO membrane component are respectively 1-10 μm, 10-100nm, 2-10nm and 0.5-2 nm; the pressures of the water inlet ends of the microporous membrane component, the ultrafiltration membrane component, the nanofiltration membrane component and the RO membrane component are respectively 0.2MPa, 0.5MPa, 2MPa and 5 MPa; the operation temperature is normal temperature.
Compared with the prior art, the invention has the following advantages and effects: after flocculation through the earlier stage, get rid of the organic matter in advance to reduced follow-up membrane treatment's pressure, among the membrane treatment process, continue to separate inorganic matter and macromolecular granule step by step, obtain the salt-containing waste water after the concentration improves, get rid of salt from waste water through the crystallization, thereby realize sewage treatment.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
FIG. 2 is a schematic structural view of a crystallizing tank according to an embodiment of the present invention.
FIG. 3 is a schematic view of the structure of a crystallization column in a crystallization tank according to an embodiment of the present invention.
FIG. 4 is a schematic structural diagram of a crystallization column according to an embodiment of the present invention.
In the figure: the device comprises a multistage membrane filtering mechanism Z, a microporous membrane component 1, an ultrafiltration membrane component 2, a nanofiltration membrane component 3, an RO membrane component 4, a flocculation purification mechanism 5, a flocculation tank 6, a flocculation wastewater storage tank 7, a crystallization tank 8, a crystallization residual liquid storage tank 9, a purified water storage tank 10, a crystallization column 11, a crystallized material discharging sleeve 12, a discharging manhole 13, a crystallization hole 14, a lifting rod 15, a solid-liquid separator 16, an air flotation oil remover 17 and a sand filter 18;
multistage membrane filtration mechanism Z: the system comprises a microporous membrane component 1, an ultrafiltration membrane component 2, a nanofiltration membrane component 3, an RO membrane component 4, a crystallization tank 8, a crystallization residual liquid storage tank 9 and a purified water storage tank 10;
flocculation purification mechanism 5: a flocculation tank 6, a flocculation wastewater storage tank 7, a solid-liquid separator 16, an air flotation oil remover 17 and a sand filter 18;
a crystallizing tank 8: the device comprises a crystallization column 11, a crystal blanking sleeve 12, a discharge manhole 13, a crystallization hole 14 and a lifting rod 15.
Detailed Description
The present invention will be described in further detail below by way of examples with reference to the accompanying drawings, which are illustrative of the present invention and are not to be construed as limiting the present invention.
Example 1.
Referring to fig. 1 to 4, the method for purifying high-salt and high-concentration wastewater by using multi-stage membrane filtration of this embodiment includes a step of performing flocculation purification in the flocculation purification mechanism 5, collecting permeate of the wastewater after the flocculation purification by using the multi-stage membrane filtration mechanism Z, and returning the concentrate to the flocculation purification mechanism 5 to continue the flocculation purification step.
The multistage membrane filtering mechanism Z of this embodiment includes micropore membrane module 1, milipore filter subassembly 2, receive filter membrane subassembly 3, crystallizer 8, crystallization residual liquid storage tank 9, RO membrane module 4 and the purified water storage tank 10 that connect gradually, receives filter membrane subassembly 3 permeate liquid outlet and connects crystallizer 8, and crystallizer 8 connects crystallization residual liquid storage tank 9, and crystallization residual liquid storage tank 9 connects the end of intaking of RO membrane module 4, and the permeate liquid outlet of RO membrane module 4 connects the purified water storage tank 10.
The flocculation purification mechanism 5 of this embodiment includes flocculation tank 6, air supporting degreaser 17, sand filter 18 and the flocculation waste water storage tank 7 that connects gradually, and the end of intaking of microporous membrane subassembly 1 is connected to the flocculation waste water storage tank 7, and the concentrated solution export of microporous membrane subassembly 1, milipore filter subassembly 2, receive filter membrane subassembly 3 and RO membrane subassembly 4 is connected flocculation waste water storage tank 7 respectively. The other scheme is that concentrated solution outlets of the microporous membrane component 1, the ultrafiltration membrane component 2, the nanofiltration membrane component 3 and the RO membrane component 4 are respectively connected with the sand filter 18.
In this embodiment, a discharge port of the flocculation tank 6 is connected with a solid-liquid separator 16, a discharge port of the solid-liquid separator 16 is connected with an air flotation oil remover 17, a discharge port of the air flotation oil remover 17 is connected with a sand filter 18, and a discharge port of the sand filter 18 is connected with a flocculation wastewater storage tank 7.
As shown in fig. 2 and fig. 3, a plurality of crystallization columns 11 are arranged in the crystallization tank 8 in this embodiment, a crystal blanking sleeve 12 capable of reciprocating along the axial direction of the crystallization columns 11 is sleeved on the crystallization columns 11, and a discharge manhole 13 is arranged at the bottom of the crystallization tank 8.
In this embodiment, the crystallization column 11 is hollow and has a sealed bottom and an open top, the crystallization column 11 is densely provided with crystallization holes 14, and the crystallization column 11 is filled with NaCl and MgSO4A mixture of (a).
Referring to fig. 2 and 4, the crystal blanking sleeve 12 is sleeved on the crystallization column 11, the crystal blanking sleeve 12 is annular, a gap is formed between the inner wall of the annular crystal blanking sleeve and the outer wall of the crystallization column 11, and the crystal blanking sleeve 12 is fixedly connected with a lifting rod 15. Wherein, crystallization column 11 and crystallizer 8 fixed connection, carry pull rod 15 and crystallizer 8 swing joint, can set up on crystallizer 8 a confession and carry pull rod 15 movable aperture can, both ends set up the location fixture block about the crystallization column 11, prevent that crystallization thing unloading cover 12 from droing or the roll-off from crystallization column 11, and the crystallization thing is handled as industrial by-product.
As shown in FIG. 3, a plurality of crystallization columns 11 are arranged in a ring-shaped array in the crystallization tank 8, so that the inorganic substance is more easily crystallized and the crystallization rate is increased.
NaCl and MgSO in the crystallization column 11 of this example4Is 1: 1. Of course, the skilled person can also adjust NaCl and MgSO as appropriate4The molar ratio of (A) to (B), however, in the present example, chlorine was maintainedThe ion and sulfate ion are 1:1, and the applicability to different waste water is better.
The specific method of the embodiment is as follows: after the wastewater enters the flocculation tank 6, adding a polyferric sulfate flocculant and PAM into the flocculation tank 6, adding NaOH solution to adjust the pH of the wastewater to 7-9, stirring for 5-10min, pumping into a solid-liquid separator 16 for solid-liquid separation, treating the separated solid as solid waste, removing oil from the wastewater in an air flotation oil remover 17, filtering the deoiled wastewater in a sand filter 18, and storing the deoiled wastewater in a flocculation wastewater storage tank 7, wherein the weight ratios of the polyferric sulfate flocculant, PAM and the wastewater in the flocculation tank 6 are respectively 0.1-2 wt: 1 and 0.1-1 wt% o: 1, preferably 0.5 wt: 1 and 0.2 wt% o: 1, pumping the wastewater in a flocculation wastewater storage tank 7 into a water inlet end of a microporous membrane component 1 by using a pump, pumping concentrated solution in the microporous membrane component 1 back into the flocculation wastewater storage tank 7, pumping permeate into a water inlet end of an ultrafiltration membrane component 2 by using a pump, pumping concentrated solution in the ultrafiltration membrane component 2 back into the flocculation wastewater storage tank 7, pumping permeate into a water inlet end of a nanofiltration membrane component 3 by using a pump, pumping concentrated solution in the nanofiltration membrane component 3 back into the flocculation wastewater storage tank 7, standing the permeate into a crystallization tank 8 for 5-24 hours, pumping the wastewater in the crystallization tank 8 into a crystallization residual solution storage tank 9, pumping the wastewater in the crystallization residual solution storage tank 9 into a water inlet end of an RO membrane component 4 by using a pump, pumping the concentrated solution in the RO membrane component 4 back into the flocculation wastewater storage tank 7, pumping the permeate into a purified water storage tank 10, wherein the water in the purified water storage tank 10 reaches a discharge standard and can be recycled, or directly discharged.
After the liquid in the crystallization tank 8 is completely injected into the residual crystallization liquid storage tank 9, the crystal blanking sleeve 12 is extracted up and down, the crystal on the crystallization column 11 is scraped from the crystallization column 11, and NaCl and MgSO are supplemented into the crystallization column 114The discharge manhole 13 is opened, and the crystallized product is taken out from the crystallizing tank 8.
The crystallization column 11 of the present example is different from the general crystallization, and NaCl and MgSO are filled in the crystallization column 11 in advance4Thereafter, crystal nuclei are produced, and the crystal pores 14 are generated as the crystal nuclei, thereby accelerating the rapid crystallization of the inorganic salt in the crystal pores 14 and allowing the crystallization processIs complete and sufficient.
In this embodiment, the filter diameters of the microporous membrane module 1, the ultrafiltration membrane module 2, the nanofiltration membrane module 3 and the RO membrane module 4 are 1-10 μm, 10-100nm, 2-10nm and 0.5-2nm, the pressures of the water inlet ends of the microporous membrane module 1, the ultrafiltration membrane module 2, the nanofiltration membrane module 3 and the RO membrane module 4 are 0.2MPa, 0.5MPa, 2MPa and 5MPa, respectively, and in this embodiment, different pumps can be configured according to the pressure required by the water inlet end.
The working principle of the embodiment is as follows: the wastewater often contains two kinds of impurities of organic matters and inorganic matters, and after passing through the flocculation purification mechanism 5, a large amount of organic matters are removed, so that the pressure of the multistage membrane filtration mechanism Z is reduced. The microporous membrane component 1, the ultrafiltration membrane component 2 and the nanofiltration membrane component 3 gradually remove macromolecular substances to relieve pressure for subsequent membrane filtration, so that the continuous working time of the membrane component is prolonged, the backwashing time is shortened, the membrane component is prevented from being blocked, and meanwhile, the relative separation of organic matters and inorganic matters is completed, thereby creating conditions for the completion of subsequent crystallization.
After crystallization in the crystallization tank 8, the inorganic salt is basically crystallized, the crystallized inorganic salt can be further treated as an industrial byproduct, and the crystallized water can be recycled as reclaimed water. The water is then treated by the RO membrane module 4 to obtain purified water. The purified water can be used as process water.
Practical application example 1:
cl in wastewater of a certain plant-、SO4 2-、Na+And Mg2+The concentration of the oil is 351.82mg/L, 542.33 mg/L, 164.12 mg/L and 213.65 mg/L respectively, the turbidity is 120NTU, the oil content is 12.1mg/L, and the emission standard is not reached.
By adopting the method of the embodiment 1, the weight ratios of the polyferric sulfate flocculant and PAM to the wastewater put in the flocculation tank 6 are respectively 0.6 wt: 1 and 0.2 wt% o: 1, 30NaOH is used for adjusting the pH value to 8.0, and Cl is added into the wastewater after the wastewater passes through a flocculation tank 6, an air flotation oil remover 17 and a sand filter 18-、SO4 2-、Na+And Mg2+The concentrations of (A) were 351.60 mg/L, 541.12 mg/L, 163.25 mg/L and 213.35 mg/L, respectively, turbidity was 20NTU, and oil content was 1.8 mg/L. The oil content and the turbidity are obviously improved, but salt ions are not seenAnd decreases.
In the permeate after passing through the microporous membrane component 1, the ultrafiltration membrane component 2 and the nanofiltration membrane component 3, Cl is contained-、SO4 2-、Na+And Mg2+The concentrations of (A) were 2.22g/L, 3.37g/L, 3.65g/L and 1.41g/L, respectively, turbidity was 4NTU, and oil content was 0.2 mg/L. Turbidity and oil content are further reduced, but salt ion concentration is increased in preparation for subsequent crystallization.
The permeate is put into a crystallizing tank 8, crystallized for 8hr, and then subjected to Cl-、SO4 2-、Na+And Mg2+The concentrations of (A) were 12.56mg/L, 8.21mg/L, 11.75mg/L and 2.32mg/L, respectively, turbidity was 4NTU, and oil content was 0.2 mg/L. The salt ion concentration is significantly reduced but the conductivity is still high. But has reached emission standards.
After passing through the RO membrane module 4, the water entering the purified water storage tank 10 has turbidity of 0.2 NTU, and other indexes are qualified according to the standard detection of purified water in Chinese pharmacopoeia 2015 edition, thereby reaching the standard of purified water.
By adopting the device, the multistage membrane filtering mechanism Z can continuously work for 7-10 days and then carry out backwashing for 12-24 hours, and the working continuity is strong.
And will be apparent to those skilled in the art from the foregoing description.
In addition, it should be noted that the specific embodiments described in the present specification may be different in the components, the shapes of the components, the names of the components, and the like, and the above description is only an illustration of the structure of the present invention. Equivalent or simple changes in the structure, characteristics and principles of the invention are included in the protection scope of the patent. Various modifications, additions and substitutions for the specific embodiments described may be made by those skilled in the art without departing from the scope of the invention as defined in the accompanying claims.
Claims (8)
1. A method for purifying high-salt high-concentration wastewater by a multi-stage membrane permeation method comprises the step of flocculation purification in a flocculation purification mechanism (5), and is characterized in that: and collecting the permeate of the wastewater after the flocculation purification through a multi-stage membrane filtering mechanism (Z), and refluxing the concentrated solution to a flocculation purification mechanism (5) to continue the flocculation purification step.
2. The method for purifying high-salinity high-concentration wastewater by the multi-stage membrane permeation method according to claim 1, characterized in that: the multistage membrane filtering mechanism (Z) comprises a crystallizing tank (8), a crystallizing residual liquid storage tank (9), a purified water storage tank (10), and a microporous membrane component (1), an ultrafiltration membrane component (2), a nanofiltration membrane component (3) and an RO membrane component (4) which are connected in sequence; the flocculation purification mechanism (5) comprises a solid-liquid separator (16), an air floatation oil remover (17), a sand filter (18), a flocculation tank (6) and a flocculation wastewater storage tank (7) connected with the flocculation tank (6), wherein the flocculation wastewater storage tank (7) is connected with the water inlet end of the microporous membrane component (1), and concentrated solution outlets of the microporous membrane component (1), the ultrafiltration membrane component (2), the nanofiltration membrane component (3) and the RO membrane component (4) are respectively connected with the flocculation wastewater storage tank (7); the crystallization tank (8) is connected with a permeate outlet of the nanofiltration membrane component (3), the crystallization tank (8) is connected with a crystallization residual liquid storage tank (9), the crystallization residual liquid storage tank (9) is connected with a water inlet end of the RO membrane component (4), and the permeate outlet of the RO membrane component (4) is connected with a purified water storage tank (10); the solid-liquid separator (16) is connected with the discharge port of the flocculation tank (6), the discharge port of the solid-liquid separator (16) is connected with the air floatation oil remover (17), the discharge port of the air floatation oil remover (17) is connected with the sand filter (18), and the discharge port of the sand filter (18) is connected with the flocculation wastewater storage tank (7).
3. The method for purifying high-salinity high-concentration wastewater by the multi-stage membrane permeation method according to claim 2, characterized in that: the purification comprises the following specific steps: after wastewater enters a flocculation tank (6), adding a polyferric sulfate flocculant and PAM into the flocculation tank (6), adding NaOH solution to adjust the pH value of the wastewater to 7-9, stirring for 5-10min, pumping into a solid-liquid separator (16) for solid-liquid separation, treating separated solids as solid waste, removing oil in an air floatation oil remover (17) by the wastewater, filtering the wastewater after oil removal in a sand filter (18), and storing in a flocculation wastewater storage tank (7), wherein the weight ratios of the polyferric sulfate flocculant and PAM to the wastewater in the flocculation tank (6) are respectively 0.1-2wt ‰:1 and 0.1-1 wt% o: 1; pumping the wastewater in the flocculation wastewater storage tank (7) into the water inlet end of the microporous membrane component (1) by a pump, refluxing the concentrated solution of the microporous membrane component (1) into the flocculation wastewater storage tank (7), the permeate is pumped into the water inlet end of the ultrafiltration membrane component (2) by a pump, the concentrated solution of the ultrafiltration membrane component (2) flows back into the flocculation wastewater storage tank (7), the permeate is pumped into the water inlet end of the nanofiltration membrane component (3) by a pump, the concentrated solution of the nanofiltration membrane component (3) flows back into the flocculation wastewater storage tank (7), allowing the permeate to enter a crystallizing tank (8) and standing for 5-24hr, introducing the wastewater in the crystallizing tank (8) into a crystallizing residual liquid storage tank (9), and pumping the wastewater in the crystallization residual liquid storage tank (9) into a water inlet end of the RO membrane assembly (4) by using a pump, refluxing the concentrated solution of the RO membrane assembly (4) into the flocculation wastewater storage tank (7), and feeding the permeate into the purified water storage tank (10).
4. The method for purifying high-salinity high-concentration wastewater by the multi-stage membrane permeation method according to claim 2, characterized in that: be equipped with a plurality of crystallization columns (11) in crystallizer (8), the cover is equipped with crystal unloading cover (12) that can follow crystallization column (11) axial reciprocating motion on this crystallization column (11), and crystallizer (8) bottom is equipped with ejection of compact manhole (13).
5. The method for purifying high-salinity high-concentration wastewater by the multi-stage membrane permeation method according to claim 4, characterized in that: the crystallization column (11) is hollow, the bottom of the crystallization column is sealed, the top of the crystallization column is open, crystallization holes (14) are densely distributed in the crystallization column (11), and NaCl and MgSO (MgSO) are filled in the crystallization column (11)4The mixture of (1), crystallization thing unloading cover (12) cover is established on crystallization post (11), and crystallization thing unloading cover (12) are annular and have the clearance between inner wall and crystallization post (11) outer wall, and crystallization thing unloading cover (12) is last to be linked firmly a lifting rod (15).
6. The method for purifying high-salinity high-concentration wastewater by the multi-stage membrane permeation method according to claim 4, characterized in that: NaCl and MgSO in the crystallization column (11)4In a molar ratio of 1:1, a plurality of crystallization columns (11) are arranged in a crystallization tank (8) in an annular array.
7. The method for purifying high-salinity high-concentration wastewater by the multi-stage membrane permeation method according to claim 4, characterized in that: after all the liquid in the crystallization tank (8) is injected into a crystallization residual liquid storage tank (9), a crystal material feeding sleeve (12) is extracted up and down, the crystal material on the crystallization column (11) is scraped from the crystallization column, and NaCl and MgSO (MgSO) are supplemented into the crystallization column (11)4The discharge manhole (13) is opened, and the crystal is taken out from the crystallizing tank (8).
8. The method for purifying high-salinity high-concentration wastewater by the multi-stage membrane permeation method according to claim 2, characterized in that: the filter diameters of the microporous membrane component (1), the ultrafiltration membrane component (2), the nanofiltration membrane component (3) and the RO membrane component (4) are respectively 1-10 μm, 10-100nm, 2-10nm and 0.5-2 nm; the pressures of the water inlet ends of the microporous membrane component (1), the ultrafiltration membrane component (2), the nanofiltration membrane component (3) and the RO membrane component (4) are respectively 0.2MPa, 0.5MPa, 2MPa and 5 MPa.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106517598A (en) * | 2016-12-28 | 2017-03-22 | 北京清大国华环境股份有限公司 | Treating method and treating device for zero discharging of desulfurization wastewater |
| CN214990744U (en) * | 2021-02-01 | 2021-12-03 | 浙江省机电设计研究院有限公司 | Multi-stage membrane permeation structure for wastewater purification |
-
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- 2021-02-01 CN CN202110135601.3A patent/CN112875930A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106517598A (en) * | 2016-12-28 | 2017-03-22 | 北京清大国华环境股份有限公司 | Treating method and treating device for zero discharging of desulfurization wastewater |
| CN214990744U (en) * | 2021-02-01 | 2021-12-03 | 浙江省机电设计研究院有限公司 | Multi-stage membrane permeation structure for wastewater purification |
Non-Patent Citations (2)
| Title |
|---|
| 丁启圣等: "《中国战略性新兴产业 新材料 高性能分离膜材料》", 31 December 2017, 冶金工业出版社 * |
| 段国波: "荷正电聚四氟乙烯复合纳滤膜的制备及表征", 《高分子材料科学与工程》 * |
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