KR20170023237A - System for producing reusable water and concentrated sewage from waste water and method using the same - Google Patents
System for producing reusable water and concentrated sewage from waste water and method using the same Download PDFInfo
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- KR20170023237A KR20170023237A KR1020150116618A KR20150116618A KR20170023237A KR 20170023237 A KR20170023237 A KR 20170023237A KR 1020150116618 A KR1020150116618 A KR 1020150116618A KR 20150116618 A KR20150116618 A KR 20150116618A KR 20170023237 A KR20170023237 A KR 20170023237A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 121
- 229910001868 water Inorganic materials 0.000 title claims abstract description 120
- 239000010865 sewage Substances 0.000 title claims abstract description 82
- 238000000034 method Methods 0.000 title claims description 44
- 239000002351 wastewater Substances 0.000 title description 6
- 239000000243 solution Substances 0.000 claims abstract description 173
- 230000006698 induction Effects 0.000 claims abstract description 96
- 238000009292 forward osmosis Methods 0.000 claims abstract description 55
- 230000001939 inductive effect Effects 0.000 claims abstract description 35
- 238000012546 transfer Methods 0.000 claims abstract description 15
- 238000007599 discharging Methods 0.000 claims abstract description 4
- 229910052602 gypsum Inorganic materials 0.000 claims abstract description 4
- 239000010440 gypsum Substances 0.000 claims abstract description 4
- 230000008595 infiltration Effects 0.000 claims abstract 2
- 238000001764 infiltration Methods 0.000 claims abstract 2
- 239000012527 feed solution Substances 0.000 claims description 65
- 230000003204 osmotic effect Effects 0.000 claims description 45
- 239000012528 membrane Substances 0.000 claims description 40
- 239000000203 mixture Substances 0.000 claims description 30
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 16
- 239000013505 freshwater Substances 0.000 claims description 14
- 239000006228 supernatant Substances 0.000 claims description 12
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 10
- 239000011591 potassium Substances 0.000 claims description 10
- 229910052700 potassium Inorganic materials 0.000 claims description 10
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 9
- 229910052698 phosphorus Inorganic materials 0.000 claims description 9
- 239000011574 phosphorus Substances 0.000 claims description 9
- 101100283604 Caenorhabditis elegans pigk-1 gene Proteins 0.000 claims description 5
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- 230000008569 process Effects 0.000 description 31
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- 230000001965 increasing effect Effects 0.000 description 10
- 229920002284 Cellulose triacetate Polymers 0.000 description 9
- NNLVGZFZQQXQNW-ADJNRHBOSA-N [(2r,3r,4s,5r,6s)-4,5-diacetyloxy-3-[(2s,3r,4s,5r,6r)-3,4,5-triacetyloxy-6-(acetyloxymethyl)oxan-2-yl]oxy-6-[(2r,3r,4s,5r,6s)-4,5,6-triacetyloxy-2-(acetyloxymethyl)oxan-3-yl]oxyoxan-2-yl]methyl acetate Chemical compound O([C@@H]1O[C@@H]([C@H]([C@H](OC(C)=O)[C@H]1OC(C)=O)O[C@H]1[C@@H]([C@@H](OC(C)=O)[C@H](OC(C)=O)[C@@H](COC(C)=O)O1)OC(C)=O)COC(=O)C)[C@@H]1[C@@H](COC(C)=O)O[C@@H](OC(C)=O)[C@H](OC(C)=O)[C@H]1OC(C)=O NNLVGZFZQQXQNW-ADJNRHBOSA-N 0.000 description 9
- 230000008859 change Effects 0.000 description 9
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 238000001223 reverse osmosis Methods 0.000 description 7
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- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
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- 238000005259 measurement Methods 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
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- 239000000498 cooling water Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 239000008367 deionised water Substances 0.000 description 1
- 229910021641 deionized water Inorganic materials 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
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Images
Classifications
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D35/00—Filtering devices having features not specifically covered by groups B01D24/00 - B01D33/00, or for applications not specifically covered by groups B01D24/00 - B01D33/00; Auxiliary devices for filtration; Filter housing constructions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/002—Forward osmosis or direct osmosis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/002—Forward osmosis or direct osmosis
- B01D61/005—Osmotic agents; Draw solutions
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological 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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
Landscapes
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention relates to a method for producing an aqueous solution containing a water-soluble organic solvent, which is connected to a front end or a rear end of a primary settling tank for primary infiltration of influent water flowing through a gypsum of a sewage treatment plant, module; A first supply pipe connected to a first end of the forward osmosis module to supply a supply solution, a first discharge pipe connected to a second end of the forward osmosis module, A second supply pipe connected to the third end of the forward osmosis module for supplying the induction solution, a second discharge pipe connected to the fourth end of the forward osmosis module for discharging the induction solution, And the diluted induction solution passing through the inducing solution transfer section is usable as reusing water. The present invention provides a system for producing concentrated sewage and reusing water from sewage water.
Description
The present invention relates to a system for producing concentrated sewage and reused water having a reduced treatment amount from sewage using a fresh water desalination system using a fertilizer composition as an induction solution, and a method using the same.
About two-thirds of the world's water demand is used as agricultural water, and reuse of agriculture water is the most important part in the sewage reuse field. In many countries, efforts are being made to treat domestic sewage and reuse as irrigation water. It is known that only 67 cases of reuse report of agricultural wastewater from sewage treatment have been reported recently.
As a result of the empirical experiment on the feasibility of reuse of agricultural wastewater in sewage treatment water, reuse of sewage wastewater as irrigation water has resulted in a remarkable improvement in the water quality improvement effect, including the effect of increasing the organic matter removal rate to 60% It was shown.
However, since the chloride content of sewage-treated water is high, it is difficult to use it directly as agriculture water, so that the re-use rate of agriculture water is low. Currently, the method currently used for removing chloride from sewage- (Reverse Osmosis). However, the reverse osmosis process requires a considerably high pressure since osmotic pressure is greatly generated. As a result, sewage treatment reuse using the reverse osmosis process requires a lot of installation and operation costs, which is difficult to apply in practice.
On the other hand, the forward osmosis process (FO) shown in Fig. 1 (B) is a technique for producing fresh water (reclaimed water) using the difference in osmotic pressure between the feed solution and the induction solution with the membrane therebetween, And it is considered that it is a new technology that can replace the reverse osmosis process in the future.
Currently, most of the pure osmosis technology is being developed as an alternative to water shortage by producing fresh water from raw water (seawater or nautical), and studies to treat sewage using pure osmosis technology are at an early stage .
As shown in Korean Patent Publication No. 10-1286044, the biggest problem in practical application of the positive osmosis technology is that an additional step of separating the derivatized solute from the diluted induction solution is required in order to continuously produce the production water.
In addition, in Korea, rainfall is intensively generated, and when the inflow of sewage water exceeds the capacity of the sewage system during rainfall, the overflow sewage water is overflowed from the sewage tank, It is a fact that it is released. Furthermore, as the water area and the solid load of the secondary settling tank increase, problems such as settling sludge flooding may occur. To cope with this problem, a storage tank is installed to temporarily store the sewage water generated in the sewage treatment plant, However, since the amount of overflow is large, the capacity of the storage tank becomes large, and there arises a problem of burdening site, construction cost, etc. for installing the storage tank.
In order to solve the above-mentioned problem, the present invention can reduce the amount of treated sewage water by concentrating the sewage water, produce reused water without further process for separating the induced solute from the diluted induction solution, Can be used as a fertilizer (fertilizer) in the fertilizer (water) of the fertilizer without any separate separation process. Therefore, it is possible to reduce the energy cost as compared with the reverse osmosis process, And a system for producing reused water from sewage that can protect groundwater and a method using the same.
In addition, the present invention aims to prepare an inducer which can be used in the production of reusable water from sewage on the basis of the composition of mixed fertilizer and use it as an inducing solution.
The present invention relates to a method of separating an inflow water flowing through a gill in a sewage treatment plant, which is connected to a front end or a rear end of a primary settling tank for primarily performing a settling process, A forward osmosis module; A first supply pipe connected to a first end of the forward osmosis module to supply a supply solution, a first discharge pipe connected to a second end of the forward osmosis module, A second supply pipe connected to the third end of the forward osmosis module for supplying the induction solution, a second discharge pipe connected to the fourth end of the forward osmosis module for discharging the induction solution, And the diluted induction solution passing through the inducing solution transfer section is usable as reusing water. The present invention provides a system for producing concentrated sewage and reusing water from sewage water.
The present invention provides a method for producing concentrated water from sewage, comprising the steps of: (a) countercurrently supplying the feed solution and the induction solution; (b) moving the fresh water contained in the feed solution through the forward osmosis membrane to the induction solution transfer section by the positive osmotic pressure phenomenon by the difference in concentration between the supplied feed solution and the induction solution; And (c) moving the concentrated feed solution to a treatment tank of the next step, wherein the removed fresh water is excluded, wherein the diluted induction solution is used as reclaimed water. Thereby producing concentrated sewage and reused water.
The system for producing concentrated sewage and reused water from the sewage according to the present invention reduces the amount of treated water by concentrating the sewage. By using the mixed fertilizer as the induction solution, the produced reused water does not need a separate separation step, Because it can be used as a fertilizer, it can save energy costs and protect the soil and groundwater with eco-friendly process.
1 is a process diagram showing a conventional reverse osmosis process and a normal osmosis process.
FIG. 2 is a process diagram showing a conventional normal osmosis process and a normal osmosis process according to the present invention.
3 is a diagram showing a typical sewage treatment system.
4 illustrates a system for producing reused water from sewage according to an embodiment of the present invention.
5 illustrates a system for producing reused water from sewage according to another embodiment of the present invention.
FIG. 6 is a graph showing changes in osmotic pressure according to concentration of an induction solution according to an embodiment of the present invention.
7 is a graph showing the osmotic pressure of each induction solution according to an embodiment of the present invention.
8 is a graph showing the osmotic pressure of the individual components, the sum of the individual components, and the osmotic pressure of the mixed fertilizer in the induction solution of the embodiment of the present invention.
9 is a graph showing a comparison between the osmotic pressure of the individual component and the osmotic pressure of the mixed fertilizer according to the concentration change of the mixed fertilizer in the induction solution of the embodiment of the present invention.
10 is a graph showing the pH of the induction solution according to an embodiment of the present invention.
11 is a graph showing the change in water permeation flux versus inductive solution when the supply solution of the embodiment of the present invention is FS-1.
FIG. 12 is a graph showing changes in water permeation flux versus induced solution for a supply solution of FS-2 according to an embodiment of the present invention. FIG.
FIG. 13 is a graph showing changes in water permeation flux versus inductive solution when the supply solution of the embodiment of the present invention is FS-3. FIG.
FIG. 14 is a graph comparing changes in water permeation flux of each of the inductive solutions when the supply solution of one embodiment of the present invention is FS-2 and FS-3.
15 is a graph showing an average water permeation flux according to an induction solution according to an embodiment of the present invention.
16 is a graph showing the average water permeation flux according to the supply solution according to one embodiment of the present invention.
FIG. 17 is a graph showing changes in the concentration factor according to the feed solution FS-1 of one embodiment of the present invention. FIG.
18 is a graph showing the change of the concentration factor according to the feed solution FS-2 of one embodiment of the present invention.
19 is a graph showing changes in the concentration factor according to the feed solution FS-3 of one embodiment of the present invention.
FIG. 20 is a graph showing the change in the concentration factor for each feed solution in one embodiment of the present invention. FIG.
FIG. 21 is a graph showing the change in the concentration factor of the induction solution according to one embodiment of the present invention. FIG.
Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. Prior to this, terms and words used in the present specification and claims should not be construed as limited to ordinary or dictionary terms, and the inventor should appropriately interpret the concepts of the terms appropriately It should be construed in accordance with the meaning and concept consistent with the technical idea of the present invention based on the principle that it can be defined.
Therefore, the embodiments described in this specification and the configurations shown in the drawings are merely the most preferred embodiments of the present invention and do not represent all the technical ideas of the present invention. Therefore, It is to be understood that equivalents and modifications are possible.
Hereinafter, as shown in the brief description of the drawings, a system for producing concentrated sewage and reused water from the sewage of the present invention will be described in detail with reference to FIGS. 1 to 21 and embodiments.
The present invention relates to a system for producing concentrated sewage and reused water from wastewater using a forward osmosis process with mixed fertilizer as an inducing solution.
Here, the reuse water means the treated water usually treated in the sewage treatment facility. The reusable water can be divided into the number of contents and the water for off-site water. The water in the intestines includes washing water, cooling water, cleaning water, drinking water, dilution water, intestinal water and other water. , Off-site other water, and off-site waterworks.
In addition, a forward osmosis (FO) process refers to a process in which a solute is melted at a concentration higher than the concentration of the feed solution solute on one side of the semipermeable membrane through which the solute can not pass, thereby inducing a higher osmotic pressure than the feed solution, 2B is a process diagram showing a process of extracting fresh water in a feed solution to the induction solution by using a forward osmosis membrane from a feed solution, and FIG. 2B is a flow chart showing a process of extracting fresh water from a feed solution to an induction solution through a semipermeable membrane. have.
4 to 5, the system for producing concentrated sewage and reused water from the sewage of the present invention is characterized in that the system for producing concentrated sewage and reused water from the sewage treatment plant includes a
In particular, the
More specifically, the forward osmosis process is performed in the
Herein, the constant
In addition, the
Here, the
In addition, the feed solution is characterized in that one of the influent or effluent of the primary clarifier (10) is used.
Here, when the
In addition, the induction solution as a solute, NH 4 NO 3, NH 4
More specifically, the induction solution solute includes a fertilizer composition, more preferably NH 4 NO 3 , KCl, (NH 4 ) 2 HPO 4 and a mixed fertilizer prepared by mixing the same, Can be used.
The mixed fertilizer (Blend) was prepared by mixing NH 4 NO 3 , (NH 4 ) 2 HPO 4 and KCl in the weight ratio w of nitrogen (N): phosphorus (P 2 O 5 ): potassium (K 2 O) / w%) is from 21:15 to 18:15 to 18, but is not limited thereto.
The NH 4 NO 3 , (NH 4 ) 2 HPO 4 and KCl have a weight ratio (w / w%) of nitrogen (N): phosphorus (P): potassium (K) of 21: 6 to 8: .
As an example, it can be used as an induction solution by preparing mixed fertilizer that can be used in a system for producing recycled water from sewage, based on mixed fertilizer composition mainly used in Jeju Island. The most commonly used fertilizer composition in Jeju is mixed fertilizer with a ratio of nitrogen (N): phosphorus (P 2 O 5 ): potassium (K 2 O) 21:17:17 (w / w%)
The nitrogen (N), phosphorus (P 2 O 5 ), and potassium (K 2 O) are nutrients that require relatively large amounts of crops among various essential elements required for growing crops and are likely to be scarce in the soil. Element. In particular, in the present invention, by using NH 4 NO 3 , (NH 4 ) 2 HPO 4 and KCl as an inducing solution, the ratio of nitrogen, phosphorus, and potassium can be independently controlled. For example, the weight ratio (w / w%) of nitrogen (N), phosphorus (P 2 O 5 ), and potassium (K 2 O) is adjusted by mixing NH 4 NO 3 , (NH 4 ) 2 HPO 4 , (N: P: K = 21.0: 7.4: 14.1), which is prepared so as to be 21:17:17 by weight, can be used as an inducing solution, but the present invention is not limited thereto.
Here, the concentration of the inducing solution solute of the present invention is higher than the concentration of the supplying solution.
The
3, the
The
The
The inductive solution supplied from the inductive
5, when the
The
Here, the
The inductive solution supplied from the inductive
In this case, the induction solution passing through the
Particularly, in the present invention, the
Here, the counterflow refers to a case where the direction of flow of two fluids is opposite in the case of heat transfer or material transfer between two fluids. In particular, in the present invention, the countercurrent flow of the feed solution and the inducing solution is higher than that of the cocurrent flow by making the osmotic pressure difference larger than that flowing in parallel, so that the feed solution and the inducing solution flow countercurrently.
In the system for producing concentrated sewage and reused water from the sewage according to the present invention having the above-described structure, the following process proceeds.
A method for producing concentrated sewage and reused water from sewage of the present invention comprises the steps of: (a) supplying the feed solution and the induction solution countercurrently; (b) moving the fresh water contained in the feed solution through the forward osmosis membrane to the induction solution transfer section by the positive osmotic pressure phenomenon by the difference in concentration between the supplied feed solution and the induction solution; And (c) moving the concentrated supply solution to a treatment tank of the next step by removing the moved fresh water, wherein the diluted induction solution containing the transferred fresh water is used as reusing water; .
More specifically, when the feed solution supplied from the front end 11 or the
At this time, the supply solution supplied through the
In particular, in the case of the
As the forward osmosis process by the positive osmotic action proceeds, the sewage is concentrated and produced by the solute such as the salt that has not passed through the
More specifically, when the feed solution passes through the
Where f c is the concentration of the feed solution, V o is the initial volume of the feed solution, and V t is the volume of the feed solution after t hours.
Therefore, as the concentration factor becomes larger, the volume reduction rate becomes larger, so that the treated water amount of the sewage decreases.
On the other hand, fresh water in the sewage having passed through the
When the
When the
In addition, the effluent of the
BEST MODE FOR CARRYING OUT THE INVENTION Hereinafter, the present invention will be described in detail with reference to the following examples. However, the following examples are intended to illustrate the contents of the present invention, but the scope of the present invention is not limited to the following examples. Embodiments of the present invention are provided to more fully describe the present invention to those skilled in the art.
Examples were carried out in order to realize a positive osmosis process system using fertilizer as an inducing solution, which is used in the present invention.
A positive osmosis module was prepared to implement the system of the present invention. In this case, the forward osmosis module is a channel of a forward osmosis module having a feed solution (FS) and a draw solution (DS) of 110 mm (L) x 36 mm (W) Respectively.
The FO membrane was installed such that the activated layer was upward and the porous layer was downward so that the feed solution flowed to the top surface of the osmosis membrane and the induction solution flowed to the bottom of the osmosis membrane.
The osmosis membrane used in the embodiment of the present invention is a cellulose triacetate (CTA) flat membrane (OsMemTM CTA-ES) manufactured by HTI, and the membrane area is 3,960 mm 2 . Table 1 shows the properties of the membranes used in this example.
The feed solution was supplied to the positive osmosis module using a diaphragm pump (DWP-62163A, Moterbank, KOREA) and the induction solution was supplied using a gear pump (WT3000-1JA, Baoding Longer Precision Pump Co., Ltd., China) . A constant temperature chamber (M20, LAUDA, Germany) was used to keep the temperature of the forward osmosis module constant and the operation temperature was kept constant at 25 ± 1 ° C.
In addition, the system operation was performed by supplying 2 L each of the supply solution and the induction solution to the PE supply solution tank and the induction solution tank, respectively, and supplying them to the forward osmosis module using a pump. Both the feed solution and the induction solution were allowed to flow countercurrently at a constant flow rate of 500 ml / min, and the solution passed through the forward osmosis module was circulated to the feed solution and the induction solution tank, respectively. Table 2 shows the operating conditions of this embodiment.
In this embodiment, a feed solution and an inducing solution were prepared. The supernatant (hereinafter referred to as FS-1) and the effluent from the primary clarifier were left for 30 minutes. The supernatant (hereinafter referred to as FS-2) and the primary clarifier effluent (Hereinafter referred to as " FS-3 ") was used.
NH 4 NO 3 , (NH 4 ) 2 HPO 4 , KCl and mixed fertilizer were used as induction solutions. The mixed fertilizer at a rate such as fertilizer (21-17-17), the most widely used in Jeju, NH 4 NO 3, (NH 4) 2
The induction solution was prepared by dissolving a single fertilizer or mixed fertilizer in deionized water. The concentration of the inducing solution was adjusted to 2 mol / LH 2 O. NH 4 NO 3 , (NH 4 ) 2 HPO 4 and KCl used in this example were all reagents (Samchun co. Korea) having a purity of 99% or more.
The most important factor in the cleansing process is the osmotic pressure difference between the inducing solution and the feed solution. That is, the greater the difference in osmotic pressure between the feed solution and the induction solution, the greater the water permeation flux. Also, since the membrane used in the positive osmosis process has a different pH range depending on the material, it may cause deformation of the osmosis membrane when using the inducing solution and the supplying solution.
Therefore, osmotic pressure and pH of the derivatized solution were measured in this example. Here, the osmotic pressure and pH of the derivatized solution were calculated using Stream Analyzer 3.2 (OLI Systems Inc., Morris Plains, NJ, USA).
In this example, 1) measurement of the osmotic pressure change according to the concentration change of the induction solution, 2) osmotic pressure measurement of the induction solution of 2mol / L H2O concentration, 3) individual components for the mixed fertilizer of 2mol Blend / L H2O, Osmotic pressure of mixed fertilizer, 4) comparison of osmotic pressure of individual component osmotic pressure and osmotic pressure of mixed fertilizer according to concentration of mixed fertilizer, and pH of induction solution.
1) Measurement of osmotic pressure change according to concentration of induction solution
First, the osmotic pressure according to the concentration change of each induction solution used in the present invention was measured and shown in FIG.
As a result, it was found that the osmotic pressure was increased as the concentration of the inducing solution was increased.
2) Osmotic pressure measurement of induction solution of 2mol / LH 2 O concentration
Figure 7 shows the osmotic pressure of the inductive solution when the concentration of the inductive solution was all kept constant at 2 mol / L H2O.
As a result, NH 4 NO 3, (NH 4) 2
3) Osmotic pressure measurement of individual components, individual components and mixed fertilizers for 2mol Blend / LH 2 O mixed fertilizer
When the mixed fertilizer was 2 mol Blend / LH 2 O, the osmotic pressure of the individual components constituting the mixed fertilizer was compared with the osmotic pressure of the three component osmotic pressure sum (Sum) and the mixed fertilizer (Blend).
As shown in FIG. 8, osmotic pressures of NH 3 NO 3 of 0.92 mol / L, (NH 4 ) 2 HPO 4 of 0.43 mol / L and KCl of 0.65 mol / L were 28.9 atm, 21.4 atm and 29.3 atm, The Sum is 79.6 atm. However, the osmotic pressure of 2 mol / LH 2 O mixed fertilizer containing 0.92 mol of NH 4 NO 3 , 0.43 mol of (NH 4 ) 2 HPO 4 and 0.65 mol of KCl was found to be less than 79.6 atm and 65.4 atm.
This is because in the case of mixed fertilizers, the osmotic pressure is reduced by the interaction between the dissolved ions.
4) Comparison of osmotic pressure and osmotic pressure of mixed fertilizer according to concentration of mixed fertilizer
FIG. 9 shows the comparison of the sum of the osmotic pressures according to the concentration of the mixed fertilizer and the sum of the three individual component osmotic pressures constituting the mixed fertilizer.
As a result, the osmotic pressure of the mixed fertilizer was lower than the sum of the osmotic pressure of the three components, as in the case of the 2 mol / LH 2 O mixed fertilizer. These differences increased with increasing concentration of mixed fertilizer. This is because in the case of mixed fertilizers, the osmotic pressure is reduced by the interaction between the dissolved ions. These differences also increased with increasing concentration of mixed fertilizer.
5) pH of induction solution
FIG. 10 shows the calculated pH when the concentration of NH 4 NO 3 , (NH 4 ) 2 HPO 4 , KCl and Blend was 2 mol / LH 2 O. FIG.
As a result, the pHs of NH 4 NO 3 , (NH 4 ) 2 HPO 4 , KCl and Blend were 4.9, 7.7, 6.9 and 7.7, respectively. As shown in Example 1, 3 to 8, all were within the pH tolerance range of the CTA-ES which is the positive osmosis membrane used in the examples.
In this example, when the system according to the present invention was installed at the front of the primary clarifier of the sewage treatment plant and the influent water from the primary clarifier of the Jeju sewage treatment plant was used as the feed solution, 2 mol / LH 2 O concentration was measured for each induction solution.
FIG. 11 is a graph showing changes in water permeation flux according to the operation time for each induction solution prepared at the concentration of 2 mol / LH 2 O according to the influent of the primary settling water (feed solution: FS-1).
As a result, regardless of the type of inducing solution, the water permeation flux decreased with operating time, and the permeate fluxes of KCl and NH 4 NO 3 were almost similar. Blend, (NH 4 ) 2 HPO 4 , respectively.
In this embodiment, when the system according to the present invention is installed at the rear end of the primary clarifier of the sewage treatment plant and the effluent and effluent filtrate from the primary clarifier of the Jeju sewage treatment plant are used as the feed solution, the induction solution prepared in Example 2 is used And the water permeate flux of each inducing solution having a concentration of 2 mol / LH 2 O was measured.
12 is a graph showing changes in water permeation flux according to the operation time of each induction solution prepared at the concentration of 2 mol / LH 2 O according to the primary clarifier effluent (feed solution: FS-2).
As a result, water fluxes were decreased according to the operating time regardless of the type of induction solution. The order of KCl> NH 4 NO 3 >Blend> (NH 4 ) 2 HPO 4 was obtained.
Next, FIG. 13 is a graph showing changes in water permeation flux according to the operation time of each induction solution prepared at the concentration of 2 mol / LH 2 O according to the filtrate of the primary clarifier effluent (feed solution: FS-3).
FIG. 14 is a graph comparing the graphs of FS-2 and FS-3 by induction solution.
As a result, water fluxes were decreased according to the operating time regardless of the type of induction solution. The order of KCl> NH 4 NO 3 >Blend> (NH 4 ) 2 HPO 4 was obtained. In addition, when the feed solution was FS-3, it was found that the water flux was relatively high relative to FS-2.
In this Example, the average permeation flux was calculated after conducting the forward osmosis test as in Example 4 and Example 5 for 24 hours, and the average water permeation flux and the water permeability per feed solution (FS-1, FS-2 and FS-3) 15 and 16 show the average water permeation flux per inductive solution.
The supernatant (FS-1) and the effluent of the primary clarifier were left to stand for 30 minutes. The supernatant (FS-2) and the primary clarifier effluent were set to 1 The filtrate (FS-3) passed through a ㎛ cartridge filter and NH 4 NO 3 , (NH 4 ) 2 HPO 4 , KCl and Blend of 2 mol / LH 2 O were used as induction solutions, respectively.
As a result, regardless of the type of the induction solution, the average value of the permeate flux was in the order of FS-3>FS-2> FS-1. In addition, the average water permeation flux for each inducing solution was in the order of KCl> NH 4 NO 3 >Blend> (NH 4 ) 2 HPO 4 . This tendency was more pronounced when the quality of the feed solution was relatively good, such as FS-3.
The average water permeation flux values according to the feed solution and the induction solution are shown in Table 3.
As described above in the above embodiment, using the experimental apparatus and the operating conditions, the feed solution and the induction solution are FS-2 and Blend, respectively, the operation time is 24 hr / day, and the membrane module is (OsMemTM CTA-ES) And the theoretical production amount of reused water was calculated when the membrane area was 16.5 m 2 .
As a result, it was found that FS-2 and Blend were used as a feed solution and an induction solution, and 3.5 m 3 / day was produced when the membrane area was 16.5 m 2 .
As a result, the components of the reclaimed water produced in the above reaction are about 21:17:17 by weight ratio of nitrogen (N 2 ): phosphorus (P 2 O 5 ): potassium (K 2 O) Is the composition ratio of the most used fertilizer in Jeju Island. Therefore, if the reused water produced in the above is diluted, it can be used as agricultural water or the like.
In this example, when the system according to the present invention was installed at the front of the primary clarifier of the sewage treatment plant and the influent water from the primary clarifier of the Jeju sewage treatment plant was used as the feed solution, 2 mol / LH 2 O solution was measured by the concentration factor induced with a concentration of.
FIG. 17 is a graph showing changes in the concentration factor depending on the operation time of each induction solution prepared at the concentration of 2 mol / LH 2 O according to the influent of the primary clarifier (feed solution: FS-1).
As a result, the concentration factors were continuously increased with the operation time, and the concentration factors of KCl and NH 4 NO 3 were almost similar, followed by Blend, (NH 4 ) 2 HPO 4 .
In this embodiment, when the system according to the present invention is installed at the rear end of the primary clarifier of the sewage treatment plant and the effluent and effluent filtrate from the primary clarifier of the Jeju sewage treatment plant are used as the feed solution, the induction solution prepared in Example 2 is used The concentrations of inducible solutions with concentrations of 2 mol / LH 2 O were measured.
First, FIG. 18 is a graph showing changes in concentration factors according to the operation time of each induction solution prepared at a concentration of 2 mol / LH 2 O according to the primary clarifier effluent (feed solution: FS-2).
As a result, according to the operating time factor concentration was continuously increased, KCl> NH 4 NO 3> Blend> (NH 4) appeared in the order of 2 HPO 4.
Next, FIG. 19 is a graph showing changes in the concentration factor depending on the operation time of each induction solution prepared at the concentration of 2 mol / LH 2 O according to the filtrate of the primary clarifier effluent (feed solution: FS-3).
As a result, the concentration factors were continuously increased, followed by KCl> NH 4 NO 3 >Blend> (NH 4 ) 2 HPO 4 .
In this example, the average concentration factors of FS-1, FS-2 and FS-3 were calculated and the concentration factor and the concentration of each solution The average concentration factors are shown in FIGS. 20 and 21. FIG.
The supernatant (FS-1) and the effluent of the primary clarifier were left to stand for 30 minutes. The supernatant (FS-2) and the primary clarifier effluent were set to 1 The filtrate (FS-3) passed through a ㎛ cartridge filter and NH 4 NO 3 , (NH 4 ) 2 HPO 4 , KCl and Blend of 2 mol / LH 2 O were used as induction solutions, respectively.
As a result, the mean value of the concentration factor increases in the order of FS-3> FS-2> FS-1, which is the same trend as the water permeation flux, because the concentration factor depends on the water permeation flux.
In addition, the average concentration factors for each inducing solution were KCl> NH 4 NO 3 >Blend> (NH 4 ) 2 HPO 4 . This tendency was more pronounced when the quality of the feed solution was relatively good, such as FS-3.
The mean concentration factor values for the feed and induction solutions are shown in Table 4.
As described above in the above examples, theoretical values of the volume reduction rate when the supply solution and the induction solution are FS-2 and KCl, respectively, were calculated according to Equation (2) using experimental equipment and operating conditions.
As a result, using a FS-2 and KCl in the feed solution and the solution was derived, f c is was found that obtaining a volume reduction rate of 51.7% when 2.07 days.
In conclusion, based on the above example, it can be seen that by using the system of the present invention, the sewage can be concentrated and the sewage treatment amount transferred to the next treatment tank is reduced by 50% or more.
100: positive osmosis module
101: first end 102: second end
103: Third end 104: Fourth end
110: osmosis membrane
120: feed solution transfer section 130: induction solution transfer section
210: first supply pipe 220: first discharge pipe
300: induction solution supply tank
310: second supply pipe 320: second discharge pipe
Claims (8)
A first supply pipe connected to a first end of the forward osmosis module to supply a supply solution, a first discharge pipe connected to a second end of the forward osmosis module,
A second supply pipe connected to the third end of the forward osmosis module for supplying the induction solution, a second discharge pipe connected to the fourth end of the forward osmosis module for discharging the induction solution, / RTI >
Characterized in that the amount of treated water in the downstream is reduced by the concentrated feed solution passing through the feed solution transfer section.
Wherein the feed solution is one of an influent or an effluent of the primary clarifier.
The induction solution as a solute, NH 4 NO 3, NH 4 H 2 PO 4, (NH 4) 2 HPO 4, NH 4 HCO 3, (NH 4) 2 SO 4, Ca (NO 3) 2, K 2 S 2 O 3 , KCl, KHCO 3 , KNO 3 , and NH 4 Cl. The system for producing concentrated sewage and reused water from sewage is characterized in that it comprises at least one solute selected from the group consisting of K 2 O 3 , KCl, KHCO 3 , KNO 3 and NH 4 Cl.
The weight ratio (w / w%) of nitrogen (N 2 ): phosphorus (P 2 O 5 ): potassium (K 2 O) was determined using NH 4 NO 3 , KCl and (NH 4 ) 2 HPO 4 A system for producing concentrated sewage and reused water from sewage characterized by being able to produce and use a mixture of 21:15 to 18: 15 to 18.
Wherein the first supply pipe, the second supply pipe, the first discharge pipe, and the second discharge pipe each include at least one pump, respectively, for producing concentrated sewage and reusing water from the sewage.
(a) countercurrently feeding the feed solution and the inducing solution;
(b) moving the fresh water contained in the feed solution through the forward osmosis membrane to the induction solution transfer section by the positive osmotic pressure phenomenon by the difference in concentration between the supplied feed solution and the induction solution; And
(c) moving the concentrated supply solution to the treatment tank of the next step by removing the moved fresh water, using the diluted induction solution containing the transferred fresh water as reused water; ≪ / RTI > wherein the concentrated water is recycled.
Wherein the feed solution is a supernatant liquid in which the influent water of the primary clarifier is allowed to stand for 20 to 40 minutes, thereby producing concentrated sewage and reusing water having reduced treated water from the sewage.
Wherein the feed solution is one of a supernatant obtained by allowing the effluent of the primary clarifier to stand for 20 to 40 minutes or an effluent of the primary clarifier passing through a 0.5 to 2 mu m cartridge filter. ≪ / RTI >
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115108606A (en) * | 2021-03-17 | 2022-09-27 | 南京理工大学 | With NH 4 NO 3 Method for concentrating forward osmosis brine for drawing electrolyte |
| US11502322B1 (en) | 2022-05-09 | 2022-11-15 | Rahul S Nana | Reverse electrodialysis cell with heat pump |
| US11502323B1 (en) | 2022-05-09 | 2022-11-15 | Rahul S Nana | Reverse electrodialysis cell and methods of use thereof |
| US11855324B1 (en) | 2022-11-15 | 2023-12-26 | Rahul S. Nana | Reverse electrodialysis or pressure-retarded osmosis cell with heat pump |
| US12040517B2 (en) | 2022-11-15 | 2024-07-16 | Rahul S. Nana | Reverse electrodialysis or pressure-retarded osmosis cell and methods of use thereof |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101286044B1 (en) | 2012-11-30 | 2013-07-15 | 한국과학기술연구원 | Plants for advanced treatment of wastewater and method for treating wastewater using thereof |
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2015
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101286044B1 (en) | 2012-11-30 | 2013-07-15 | 한국과학기술연구원 | Plants for advanced treatment of wastewater and method for treating wastewater using thereof |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115108606A (en) * | 2021-03-17 | 2022-09-27 | 南京理工大学 | With NH 4 NO 3 Method for concentrating forward osmosis brine for drawing electrolyte |
| US11502322B1 (en) | 2022-05-09 | 2022-11-15 | Rahul S Nana | Reverse electrodialysis cell with heat pump |
| US11502323B1 (en) | 2022-05-09 | 2022-11-15 | Rahul S Nana | Reverse electrodialysis cell and methods of use thereof |
| US11563229B1 (en) | 2022-05-09 | 2023-01-24 | Rahul S Nana | Reverse electrodialysis cell with heat pump |
| US11611099B1 (en) | 2022-05-09 | 2023-03-21 | Rahul S Nana | Reverse electrodialysis cell and methods of use thereof |
| US11699803B1 (en) | 2022-05-09 | 2023-07-11 | Rahul S Nana | Reverse electrodialysis cell with heat pump |
| US12107308B2 (en) | 2022-05-09 | 2024-10-01 | Rahul S Nana | Reverse electrodialysis cell and methods of use thereof |
| US11855324B1 (en) | 2022-11-15 | 2023-12-26 | Rahul S. Nana | Reverse electrodialysis or pressure-retarded osmosis cell with heat pump |
| US12040517B2 (en) | 2022-11-15 | 2024-07-16 | Rahul S. Nana | Reverse electrodialysis or pressure-retarded osmosis cell and methods of use thereof |
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