CN112209547A - Concentration and reduction method for high-salinity high-organic matter aqueous solution - Google Patents
Concentration and reduction method for high-salinity high-organic matter aqueous solution Download PDFInfo
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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
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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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
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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
- C02F1/441—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
- C02F1/445—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by forward 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
- C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
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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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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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
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/08—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents
- C02F5/10—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents using organic substances
Abstract
A method for concentrating and reducing a high-salinity high-organic-matter aqueous solution comprises the following steps: (1) performing membrane concentration treatment on an aqueous solution to be treated, performing substance exchange on a stock solution on one side of a forward osmosis membrane and an extracting solution on the other side under the driving of osmotic pressure difference, introducing water in the aqueous solution into the extracting solution, concentrating the aqueous solution to obtain a concentrated solution, and diluting the extracting solution to obtain a diluted extracting solution; TDS <500,000ppm or/and COD <600,000ppm in the aqueous solution to be treated; (2) performing reverse osmosis treatment or membrane distillation treatment on the diluted extracting solution to regenerate the extracting solution and obtain produced water; and (3) introducing the regenerated extracting solution into the step (1) for recycling, and directly recycling the produced water. The invention reduces the concentration of the water solution through the forward osmosis membrane with low energy consumption and pollution resistance, finally realizes the zero discharge of the wastewater, reduces the treatment capacity of a subsequent evaporation device when being applied to the wastewater treatment process, and reduces the operation energy consumption of the system.
Description
Technical Field
The invention belongs to the technical field of water treatment concentration, and particularly relates to a concentration and reduction method of a high-salinity high-organic-matter aqueous solution.
Background
Water acts as a good solvent, dissolving a large number of different soluble inorganic salts, such as: sodium ion, chloride ion, calcium ion, magnesium ion, sulfate ion, etc., and many organic substances such as glucose, amino acids, etc. can be dissolved in water. Therefore, aqueous solutions in nature often contain multiple solutes, forming mixed solutions. Particularly, for multi-component wastewater with high salinity (TDS <500,000 ppm) and high organic content (COD <600,000 ppm), the difficulty of the concentration or purification treatment is higher than that of the single treatment of a dissolved substance, mainly because of the mutual interference of the dissolved substances.
The common wastewater treatment method at present is a process combining 'three-stage treatment' with a 'double-membrane method', specifically, a first stage removes suspended matters in a physicochemical mode, a second stage removes degradable water-soluble organic matters in a biochemical mode, a third stage performs advanced treatment sterilization, and then ultrafiltration, nanofiltration and reverse osmosis are performed to remove salt, and then strong brine (usually with the concentration of 2-7% and mass fraction) generated by reverse osmosis is reused through an evaporator and a crystallizer. The whole treatment process has long flow, multiple steps and high cost. In addition, because of the self-limitation of the reverse osmosis membrane, the salt concentration of the concentrated water is still far away from saturation, and the evaporation and concentration by adopting a thermal method consume a large amount of energy.
Disclosure of Invention
The invention aims to provide a concentration and reduction method of a high-salinity high-organic-matter aqueous solution, which is used for intercepting salinity and soluble organic matters in the aqueous solution and enabling clear water to pass through a membrane, so that the concentration and reduction method of the aqueous solution is realized, the water reuse rate is improved, and zero discharge of wastewater is realized.
In order to achieve the purpose, the technical scheme of the invention is as follows:
a method for concentrating and reducing a high-salinity high-organic-matter aqueous solution comprises the following steps:
1) membrane concentration treatment
Performing membrane concentration treatment on an aqueous solution to be treated, wherein the membrane concentration treatment is to perform forward osmosis by adopting a plate-type or roll-type forward osmosis membrane group, under the driving of osmotic pressure difference, performing material exchange on the aqueous solution on one side of the forward osmosis membrane and the extracting solution on the other side of the forward osmosis membrane, introducing water in the aqueous solution into the extracting solution, concentrating the aqueous solution to obtain a concentrated solution, and diluting the extracting solution to obtain a diluted extracting solution;
TDS <500,000ppm or/and COD <600,000ppm in the aqueous solution to be treated;
2) regeneration treatment of extract
Carrying out reverse osmosis treatment or membrane distillation treatment on the diluted extracting solution obtained in the step 1) to improve the concentration of the extracting solution so as to regenerate the extracting solution and obtain produced water, wherein TDS (total dissolved solids) in the produced water is less than 500ppm, and COD (chemical oxygen demand) in the produced water is less than 50 ppm; introducing the regenerated extracting solution into the step 1) for recycling;
the reverse osmosis treatment adopts a roll type multistage reverse osmosis membrane group, and the membrane distillation adopts a plate type low-temperature distillation membrane group.
Further, the method also comprises scale inhibition treatment before the membrane concentration treatment in the step 1), and the scale inhibition treatment method comprises the following steps: adjusting the pH value of the liquid to be treated and adding a scale inhibitor for scale inhibition treatment.
Preferably, the concentration of the scale inhibitor is 2-20 ppm.
In the step 2), the osmotic pressure difference is 70-600 psi;
in the step 2), the plate-type or roll-type forward osmosis membrane group adopts a plate-type or roll-type forward osmosis membrane element with modules connected in series, and the salt rejection rate of the plate-type or roll-type forward osmosis membrane element is more than or equal to 90%.
In the step 2), the operating conditions of forward osmosis are as follows: the water flux of the membrane is 2-18L/m2H, the lateral pressure of the aqueous solution is 5-15 psi, the lateral pressure of the extracting solution is 2-12 psi, and the operating temperature is 5-45 ℃. Preferably, the pressure difference DeltaP between the aqueous solution side and the extraction solution side is-5 psi ≦ DeltaP ≦ 10 psi.
Further, the extraction solution is a solution having a higher osmotic pressure than the aqueous solution to be treated, such as NaCl solution, MgCl2Solution, Na2SO4Solutions or MgSO4Solutions, and the like.
In the step 2), the multistage reverse osmosis membrane group adopts a mode of cascade connection between stages, the stage number is 1-5, if the stage number is 1, 1-20 reverse osmosis membrane elements are adopted in the 1 st stage, and the salt rejection rate of the reverse osmosis membrane elements is more than or equal to 95%; if the number of stages is more than or equal to 2, 1-20 reverse osmosis membrane elements are adopted in the 1 st stage, and the salt rejection rate of the reverse osmosis membrane elements is more than or equal to 95 percent; and 3-15 reverse osmosis membrane elements are adopted in the other stages, the salt rejection rate of the reverse osmosis membrane elements is 50-90%, and the salt rejection rates of the reverse osmosis membrane elements in the other stages are gradually decreased.
In the step 3), the operating conditions of the reverse osmosis treatment are as follows: membrane cartridgeThe amount of the organic solvent is 3 to 35L/m2H, the operating pressure is 100-1500 psi, and the operating temperature is 5-40 ℃.
In the step 2), the operation conditions of the membrane distillation treatment are as follows: the membrane flux is 5-16L/m2H, the absolute pressure of the vacuum side is 25-200 mbar, and the operating temperature is 50-70 ℃.
In the step 2), the plate-type low-temperature membrane distillation membrane group adopts a multi-group parallel connection mode, water vapor molecules can pass through the membrane distillation membrane, and salt and other soluble macromolecular organic matters cannot penetrate through the distillation membrane.
Before the membrane concentration treatment, scale inhibition treatment can be carried out for preventing scaling phenomenon, the scale inhibition treatment is conventional operation, whether scale inhibition treatment is carried out or not and the adding concentration of the scale inhibitor are adjusted according to the type, the concentration and the like of ions with scaling tendency in an aqueous solution.
In the step 1) membrane concentration treatment, under the driving of osmotic pressure difference, the aqueous solution and the extracting solution are subjected to material exchange, water in the aqueous solution enters the extracting solution, a concentrated solution and the diluted extracting solution are obtained, and the concentration multiple of the aqueous solution is 2-50 times. Step 2), TDS in the produced water obtained by reverse osmosis treatment or membrane distillation treatment is less than 500ppm, COD is less than 50ppm, the produced water exceeds the standard of tap water, reaches the standard of direct use, and can be directly used as factory production water and the like; the regenerated extracting solution obtained in the step 2) can be introduced into the step 1) for cyclic utilization, so that the water reuse rate is improved, and zero discharge of wastewater is realized.
In the invention, the reduction method provided by the invention can be applied to concentration treatment as long as the water quality of the liquid to be treated meets TDS <500,000ppm or/and COD <600,000ppm, for example, the method is applicable to concentration treatment of lithium carbonate wastewater, landfill leachate, electroplating wastewater, chemical wastewater, coking wastewater, electroplating wastewater, medical wastewater, food medical wastewater, oilfield reinjection water, oilfield produced liquid, metallurgical wastewater, mine acid wastewater, power plant desulfurization wastewater or boiler external drainage and the like. In addition, the invention is also suitable for fruit juice concentration, Chinese and western medicine concentration, antibiotic concentration, sucrose and stevioside concentration, milk and other dairy product concentration and the like, in the application, because the stock solution contains a large amount of water, in order to save the transportation cost or obtain solute therein, the water is often distilled out by a heating method, but because the heating consumes a lot of energy, and the heating often destroys the performance of the stock solution, for example, the heating of the fruit juice destroys the nutrition cost and the fragrance therein, the method provided by the invention can selectively remove the water in the stock solution at normal temperature, thereby realizing the concentration with low energy consumption and no raw material loss.
The invention has the beneficial effects that:
aiming at the water quality characteristics of the high-salinity high-organic-matter aqueous solution, the forward osmosis membrane treatment is used as a core technology, the salt and soluble organic matters in the water can be intercepted by utilizing the forward osmosis, clear water passes through the membrane, the aqueous solution is concentrated, and the concentration multiple can reach 2-50 times, so that the method for reducing the aqueous solution is realized.
The diluted extract generated by the membrane concentration treatment in the concentration and reduction method provided by the invention can be regenerated through reverse osmosis treatment or membrane distillation treatment, and then enters the membrane concentration treatment for recycling, and meanwhile, the produced water obtained by the reverse osmosis treatment or the membrane distillation treatment can be directly used as factory production water and the like, so that the recycling rate of the whole factory water is improved, and zero discharge of wastewater is realized.
The reduction treatment method is applied to a wastewater treatment process, the membrane concentration treatment is used as a first-stage concentration unit to carry out reduction treatment on the wastewater, the evaporation treatment capacity of subsequent evaporation is greatly reduced, and the stable operation of an evaporation system is ensured. The membrane concentration treatment process can utilize the characteristics of positive osmosis, capability of intercepting solute and high organic matter resistance to concentrate mixed wastewater, thereby reducing the complexity of the treatment process and reducing the treatment cost.
Detailed Description
The present invention is further illustrated by the following examples, which are not intended to limit the scope of the invention.
Example 1
The ingredients of the wastewater generated by the concentrated water collecting tank of the coking wastewater reverse osmosis device workshop of an enterprise are shown in table 1, and the wastewater is subjected to reduction treatment, which comprises the following steps:
(1) and (3) enabling the wastewater to enter a water inlet adjusting tank, adding hydrochloric acid to adjust the pH value to 4-5, and adding 0.5ppm of an inorganic scaling and scale inhibitor (polyacrylic acid).
(2) Membrane concentration
The wastewater after the scale inhibition treatment is lifted to a forward osmosis system by a lift pump to perform a material exchange reaction with a NaCl solution with the concentration of 7 percent, the outlet pressure of the lift pump is 5.8psi, the inlet water operation temperature is 15 ℃, and the forward osmosis flux is 8.2L/m2H, obtaining a concentrated solution (the concentration multiple is 5) and a diluted extracting solution (the concentration is reduced from 7% to 3.2%), wherein the water quality of the concentrated solution is shown in a table 1.
The forward osmosis system adopts plate type forward osmosis membrane groups, the membrane groups adopt plate type forward osmosis membrane elements with modules connected in series, each membrane group comprises 10 membrane elements, the total number of the membrane groups is two, the pressure difference between two sides of the membrane is maintained to be less than 10psi, and the salt rejection rate of the forward osmosis membrane is more than or equal to 90%.
(3) Regeneration treatment of extract
The extracting solution regeneration device adopts a mode of connecting multi-stage reverse osmosis membrane groups in series, the stage number is 3, the 1 st stage adopts 8 sea freshwater reverse osmosis membrane elements, the salt rejection rate is 99%, and the operating pressure is 600-; the 2 nd stage adopts 3 reverse osmosis membranes with low salt rejection rate, the salt rejection rate is 90 percent, and the operating pressure is 800-; the 3 rd level adopts 1 reverse osmosis membrane with lower salt rejection rate, the salt rejection rate is 80 percent, and the operating pressure is 1000-1200 psi; the membrane flux is 3-20L/m2H, the operation temperature is 5-40 ℃.
The concentration of the diluted extracting solution is recovered from 3.2% to 7% after regeneration treatment, the extracting solution is led into the step (1) for recycling, meanwhile, reverse osmosis membrane is used for separating the original wastewater to produce usable produced water with the conductivity of about 100us/cm, and the quality of the produced water is shown in table 2.
(4) Preheating the concentrated solution to 80 deg.C, evaporating in mechanical compression evaporator to obtain condensed water and residue, and delivering the residue for treatment.
TABLE 1
| Index of water quality | Unit of | Waste water | Concentrated solution | Recycled water |
| pH | 8.9 | 8.5 | 7.3 | |
| Electrical conductivity of | us/cm | 13000 | 57000 | 100 |
| CODcr | mg/l | 336 | 2300 | 10 |
| TDS | mg/l | 9800 | 88000 | 150 |
| SO4 2- | mg/l | 2200 | 16800 | 5 |
| Ca2+ | mg/l | 21 | 67 | <0.1 |
| Mg2+ | mg/l | 7.9 | 29 | <0.1 |
| Chloride compound | mg/l | 2730 | 27800 | 43 |
| F- | mg/l | 3 | 11.2 | Not detected out |
| Al3+ | mg/l | 1.4 | 7.2 | Not detected out |
| Total nitrogen | mg/l | 116 | 715 | 0.5 |
Comparative example 1
The main components of the reverse osmosis concentrated water produced in the membrane method recycling process of the coking wastewater of certain steel enterprises are shown in the table 1. The reverse osmosis concentrated water is directly used for flue evaporation treatment, and is not subjected to reduction treatment, so that the problem that the emission of pollutants such as VOCs at a flue gas outlet exceeds standard is caused, the relevant emission standard is not met, and the resource utilization difficulty of fly ash residues is improved.
Example 2
The reverse osmosis concentrated water components of the coking wastewater advanced treatment unit of a certain enterprise are shown in a table 2.
(1) And (3) enabling the wastewater to enter a water inlet adjusting tank, adding hydrochloric acid to adjust the pH value to 4-5, and adding 1.5ppm of an inorganic scale-forming and scale-inhibiting agent (polyacrylic acid).
(2) Membrane concentration
The pre-adjusted wastewater enters a lift pump and is lifted to a forward osmosis system to perform material exchange reaction with 10% NaCl solution, the outlet pressure of the lift pump is 7.6psi, the inlet water operation temperature is 20 ℃, and the forward osmosis flux is 11.3L/m2H, obtaining a concentrated solution (the concentration multiple is 8) and a diluted extracting solution (the concentration is reduced from 10% to 4.6%), wherein the water quality of the concentrated solution is shown in a table 2.
The forward osmosis system adopts plate type forward osmosis membrane groups, the membrane groups adopt single-stage series plate type forward osmosis membrane elements, each membrane group comprises 10 membrane elements, the total number of the membrane groups is 1, the pressure difference between two sides of the membrane is maintained to be less than 10psi, and the salt rejection rate of the forward osmosis membrane is more than or equal to 90%.
(3) Regeneration treatment of extract
The diluted extracting solution is subjected to steam heat exchange to 65 ℃, and then is lifted to a membrane distillation system, wherein the membrane distillation membrane flux is 5-16L/m2H, absolute pressure on vacuum side 55mbar, recovery of extract concentration from 4.6% to 10% after membrane distillation treatment, introduction into step (1) for circulationAnd (3) separating the raw wastewater to produce the directly usable produced water with the conductivity of about 25us/cm, wherein the quality of the produced water is shown in Table 2.
(4) And (4) further exchanging heat of the concentrated solution to 80 ℃, entering a mechanical compression evaporator for evaporation to obtain condensed water and residues, and sending the residues out for treatment.
TABLE 2
| Index of water quality | Unit of | Reverse osmosis concentrate | Concentrated solution | Recycled water |
| pH | 8.1 | 8.0 | 7.5 | |
| Electrical conductivity of | us/cm | 7000 | 62000 | 25 |
| CODcr | mg/l | 127 | 579 | 5 |
| TDS | mg/l | 5700 | 47000 | 15 |
| SO4 2- | mg/l | 860 | 4700 | 3 |
| Ca2+ | mg/l | 30 | 115 | <0.1 |
| Mg2+ | mg/l | 4 | 21 | <0.1 |
| Chloride compound | mg/l | 1280 | 13900 | 15 |
| F- | mg/l | 6 | 35 | Not detected out |
| Al3+ | mg/l | 0.6 | 10.2 | Not detected out |
| Total nitrogen | mg/l | 75 | 482 | 0.3 |
Comparative example 2
The main components of the reverse osmosis concentrated water of the advanced treatment unit of the coking wastewater of a certain enterprise are shown in the table 2. The water directly enters an evaporation system without being concentrated by a forward osmosis membrane, simultaneously, the water yield of reverse osmosis of the original treatment system is reduced to 47% from 60% of the design due to the scaling problem, the operation pressure is improved by 23%, the discharged concentrated water is increased, the evaporation system cannot stably operate, and the operation cost per ton of water is up to 165 yuan/ton.
Example 3
Fresh orange juice is produced in a certain fruit juice processing factory, the sugar content is about 10 percent, the fresh orange juice needs to be transported to a consumption place from a place of origin, the transportation cost is 120 yuan/ton, the fruit juice is concentrated and then transported by adopting the method, so that the transportation cost is saved to the maximum extent, and the method specifically comprises the following steps:
(1) membrane concentration
The fresh orange juice is lifted to a forward osmosis system by a lift pump to perform material exchange reaction with 10 percent NaCl solution, the outlet pressure of the lift pump is 10.6psi, the inlet water operation temperature is 20 ℃, and the forward osmosis flux is 14.4L/m2H, to obtain a concentrated solution (concentration factor 5) and a diluted extract (concentration reduced from 10% to 5%).
The forward osmosis system adopts a plate type forward osmosis membrane group, the membrane group adopts a single-stage series plate type forward osmosis membrane element, each membrane group comprises 9 membrane elements, the total number of the membrane groups is 3, the pressure difference between two sides of the membrane is maintained to be less than 10psi, and the salt rejection rate of the forward osmosis membrane is more than or equal to 90%.
(2) Regeneration treatment of extract
The extracting solution regenerating device adopts a mode of connecting multi-stage reverse osmosis membrane groups in series, the stage number is 3, the 1 st stage adopts 8 reverse osmosis membrane elements, the salt rejection rate is 99%, the 2 nd stage adopts 3 reverse osmosis membranes with low salt rejection rate, the salt rejection rate is 90%, the 3 rd stage adopts 1 reverse osmosis membrane with lower salt rejection rate, and the salt rejection rate is 80%.
And (3) recovering the concentration of the NaCl solution from 5% to 10% after reverse osmosis treatment, introducing the NaCl solution into the step (1) for recycling, and simultaneously, directly using the separated produced water as factory production water and the like.
The fresh orange juice of the enterprise adopts a heating, evaporating and concentrating mode, and the processing cost is about 80 yuan per ton of juice. The concentrated juice treated by the method has the operation cost of only 20 yuan/ton, the sugar content of the concentrated juice reaches 50-60%, the comprehensive cost is reduced by 70%, heating is not needed in the concentration process, the nutrient components and the taste in the juice are not damaged, and the reduction degree is high.
Example 4
The invention relates to a method for concentrating and transporting fresh milk, which is used for transporting fresh milk from a milk source place to a consumption place, wherein the fresh milk in a dairy processing plant has a protein content of 2-2.5 g/100g, and the transportation cost is 120 yuan/ton, and the method for concentrating and transporting the fresh milk saves the transportation cost to the maximum extent, and specifically comprises the following steps:
(1) membrane concentration
The fresh milk is lifted to a forward osmosis system by a lift pump to perform substance exchange reaction with a NaCl solution with 14 percent concentration, the outlet pressure of the lift pump is 9.6psi, the inlet water operation temperature is 20 ℃, and the forward osmosis flux is 12.4L/m2H, to obtain a concentrated solution (concentration factor 9) and a diluted extract (concentration reduced from 14% to 3.5%).
The forward osmosis system adopts a plate type forward osmosis membrane group, the membrane group adopts a single-stage series plate type forward osmosis membrane element, each membrane group comprises 8 membrane elements, the total number of the membrane groups is 2, the pressure difference between two sides of the membrane is maintained to be less than 10psi, and the salt rejection rate of the forward osmosis membrane is more than or equal to 90%.
(2) Regeneration treatment of extract
The extracting solution regenerating device adopts a mode of connecting multi-stage reverse osmosis membrane groups in series, the stage number is 3, the 1 st stage adopts 8 sea fresh reverse osmosis membranes, the salt rejection rate is 99%, the 2 nd stage adopts 3 reverse osmosis membranes with low salt rejection rate, the salt rejection rate is 90%, the 3 rd stage adopts 1 reverse osmosis membrane with lower salt rejection rate, and the salt rejection rate is 80%.
And (3) after reverse osmosis treatment, recovering the concentration of the NaCl solution from 3.5% to 14%, introducing the NaCl solution into the step (1) for recycling, and simultaneously, directly using the separated produced water as factory production water and the like.
The concentrated fresh milk treated by the method has the operation cost of only 20 yuan/ton, the protein content after concentration reaches 40g/100g of fresh milk, the comprehensive cost is reduced by 75 percent, the concentration process does not need heating, nutrient substances in the original milk are not damaged, and the reduction degree is high.
Claims (10)
1. A method for concentrating and reducing a high-salinity high-organic-matter aqueous solution comprises the following steps:
1) membrane concentration
Performing membrane concentration treatment on an aqueous solution to be treated, wherein the membrane concentration treatment is to perform forward osmosis by adopting a plate-type or roll-type forward osmosis membrane group, under the driving of osmotic pressure difference, performing material exchange on the aqueous solution on one side of the forward osmosis membrane and the extracting solution on the other side of the forward osmosis membrane, introducing water in the aqueous solution into the extracting solution, concentrating the aqueous solution to obtain a concentrated solution, and diluting the extracting solution to obtain a diluted extracting solution;
TDS <500,000ppm or/and COD <600,000ppm in the aqueous solution to be treated;
2) regeneration of extract
Performing reverse osmosis treatment or membrane distillation treatment on the diluted extracting solution obtained in the step 1) to regenerate the extracting solution and obtain produced water, wherein TDS in the produced water is less than 500ppm, and COD in the produced water is less than 50 ppm; introducing the regenerated extracting solution into the step 1) for recycling.
2. The method for concentrating and reducing the high-salinity high-organic-matter aqueous solution according to claim 1, further comprising a scale inhibition treatment before the membrane concentration treatment in step 1), wherein the scale inhibition treatment method comprises: adjusting the pH value of the liquid to be treated and adding a scale inhibitor for scale inhibition treatment.
3. The method for concentrating and reducing a high-salinity high-organic matter aqueous solution according to claim 2, wherein the concentration of the scale inhibitor is 2-20 ppm.
4. The method for concentrating and reducing the high-salt and high-organic water solution according to claim 1, wherein the osmotic pressure difference in step 1) is 70-600 psi.
5. The method for concentrating and reducing the high-salinity high-organic-matter aqueous solution according to claim 1, wherein in the step 1), the plate-type or roll-type forward osmosis membrane module adopts a plate-type or roll-type forward osmosis membrane element with modules connected in series, and the salt rejection rate of the plate-type or roll-type forward osmosis membrane element is more than or equal to 90%.
6. The method for concentrating and reducing the high-salt and high-organic water solution according to claim 1, wherein the forward osmosis is performed under the following operating conditions in step 1): the water flux of the membrane is 2-18L/m2H, the lateral pressure of the aqueous solution is 5-15 psi, the lateral pressure of the extracting solution is 2-12 psi, and the operating temperature is 5-45 ℃.
7. The method according to claim 6, wherein the pressure difference Δ P between the aqueous solution side and the extraction solution side is-5 psi ≦ Δ P ≦ 10 psi.
8. The method for concentrating and reducing the high-salinity high-organic-matter aqueous solution according to claim 1, wherein in the step 2), the reverse osmosis treatment adopts a roll type multi-stage reverse osmosis membrane group, the multi-stage reverse osmosis membrane group adopts a mode of cascade connection, and the number of stages is 1-5;
if the number of the stages is 1, 1-20 reverse osmosis membrane elements are adopted in the 1 st stage, and the salt rejection rate of the reverse osmosis membrane elements is more than or equal to 95 percent;
if the number of stages is more than or equal to 2, 1-20 reverse osmosis membrane elements are adopted in the 1 st stage, and the salt rejection rate of the reverse osmosis membrane elements is more than or equal to 95 percent; and 3-15 reverse osmosis membrane elements are adopted in the other stages, the salt rejection rate of the reverse osmosis membrane elements is 50-90%, and the salt rejection rates of the reverse osmosis membrane elements in the other stages are gradually decreased.
9. The method for concentrating and reducing the high-salinity high-organic-matter aqueous solution according to claim 1, wherein in the step 2), the reverse osmosis treatment is performed under the following operating conditions: the membrane flux is 3-35L/m2H, the operating pressure is 100-1500 psi, and the operating temperature is 5-40 ℃.
10. The method for concentrating and reducing the high-salt and high-organic aqueous solution according to claim 1, wherein the membrane distillation process is performed under the following conditions in step 2): the membrane flux is 5-16L/m2H, the absolute pressure of the vacuum side is 25-200 mbar, and the operating temperature is 30-80 ℃.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102745776A (en) * | 2012-07-03 | 2012-10-24 | 上海中科高等研究院 | Method and apparatus for treatment of concentrated reverse osmosis drainage through coupled forward osmosis and reverse osmosis |
| CN103073146A (en) * | 2013-02-06 | 2013-05-01 | 上海中科高等研究院 | Waste water treatment method and device based on forward osmosis and membrane distillation |
| JP2015150553A (en) * | 2014-02-19 | 2015-08-24 | 株式会社ササクラ | Fresh water generation device and fresh water generation method |
| CN105923704A (en) * | 2016-04-29 | 2016-09-07 | 北京新源国能科技集团股份有限公司 | Forward osmosis draw fluid recycling method, wastewater treatment method and treatment device |
| CN107098530A (en) * | 2017-05-02 | 2017-08-29 | 山东博润工业技术股份有限公司 | A kind of positive osmosis treatment system of chloro alcali wastewater and handling process |
| CN107585936A (en) * | 2017-09-22 | 2018-01-16 | 北京万邦达环保技术股份有限公司 | The Zero-discharge treating process and device of a kind of high-salt wastewater |
| WO2019087867A1 (en) * | 2017-10-30 | 2019-05-09 | 東洋紡株式会社 | Seawater desalination method and seawater desalination system |
-
2019
- 2019-07-10 CN CN201910618143.1A patent/CN112209547A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102745776A (en) * | 2012-07-03 | 2012-10-24 | 上海中科高等研究院 | Method and apparatus for treatment of concentrated reverse osmosis drainage through coupled forward osmosis and reverse osmosis |
| CN103073146A (en) * | 2013-02-06 | 2013-05-01 | 上海中科高等研究院 | Waste water treatment method and device based on forward osmosis and membrane distillation |
| JP2015150553A (en) * | 2014-02-19 | 2015-08-24 | 株式会社ササクラ | Fresh water generation device and fresh water generation method |
| CN105923704A (en) * | 2016-04-29 | 2016-09-07 | 北京新源国能科技集团股份有限公司 | Forward osmosis draw fluid recycling method, wastewater treatment method and treatment device |
| CN107098530A (en) * | 2017-05-02 | 2017-08-29 | 山东博润工业技术股份有限公司 | A kind of positive osmosis treatment system of chloro alcali wastewater and handling process |
| CN107585936A (en) * | 2017-09-22 | 2018-01-16 | 北京万邦达环保技术股份有限公司 | The Zero-discharge treating process and device of a kind of high-salt wastewater |
| WO2019087867A1 (en) * | 2017-10-30 | 2019-05-09 | 東洋紡株式会社 | Seawater desalination method and seawater desalination system |
Non-Patent Citations (1)
| Title |
|---|
| 赵文玉 等主编: "《工业水处理技术》", 31 May 2019, pages: 166 * |
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