KR20170109332A - Measurement method and apparatus for forward osmosis membrane fouling pollution index - Google Patents

Abstract

According to an embodiment of the present invention, a device to predict the pollution of a forward osmosis membrane includes: a membrane pollution simulating part including a forward osmosis separation membrane and simulating the pollution of a forward osmosis separation membrane during a forward osmosis process; an inflow water supply part connected with the membrane pollution simulating part to provide primary inflow water during the forward osmosis process while providing secondary inflow water, which is faster than the primary inflow water, during a washing process; an inducing solution supply part connected with the membrane pollution simulating part to supply an inducing solution, of which the concentration is higher than the primary inflow water, during the forward osmosis process; and a membrane pollution predicting part calculating a forward osmosis membrane pollution index (OFI) by measuring the penetration rate of the primary inflow water, which penetrates the forward osmosis separation membrane, in accordance with how long the forward osmosis process is performed, and predicting the pollution of the forward osmosis separation membrane from the forward osmosis membrane pollution index. The inducing solution supply part accelerates the formation of an adhesive layer by controlling a molar concentration while providing the inducing solution to the membrane pollution simulating part. The membrane pollution simulating part advisably simulates the pollution of the forward osmosis separation membrane through the adhesive layer, which is formed by accumulating organic matter of the primary inflow water on the surface of the forward osmosis separation membrane, during a procedure in which the primary inflow water flows into a space, which stores the inducing solution, due to osmosis by the difference in concentration between the inducing solution and the primary inflow water.

Description

[0001] The present invention relates to a method for predicting a fouling pollution in a forward osmosis membrane,

The present invention relates to a device for predicting the osmosis membrane fouling and a method for predicting the fouling of the osmosis membrane. More particularly, the present invention relates to a method for predicting the contamination of a forward osmosis membrane produced by a seawater desalination process, a filtration process, a dewatering process, And more particularly, to a forward osmosis membrane fouling predicting apparatus and a forward osmosis membrane fouling predicting method capable of predicting and predicting a forward osmosis membrane fouling.

The seawater desalination process or water reuse process based on membrane filtration technology is considered as the ideal solution to solve the future water shortage problem. Reflecting this, the membrane filtration process, which has been developed rapidly in recent decades, has not only secured new water resources such as seawater desalination (RO / NF), sewage treatment and water reuse (MF / UF, MBR) (FO).

The dual reverse osmosis process is being used more rapidly due to the better quality of produced water than conventional water treatment. However, since the reverse osmosis process uses a high pressure as a driving force for membrane separation, it requires not only a large amount of electric power but also irreversible membrane fouling, which requires chemical washing or pretreatment of influent water. .

From this point of view, the forward osmosis process is attracting attention as a next-generation water treatment technology capable of overcoming the limitations of existing processes and replacing its role in areas where reverse osmosis is mainly used. The most important advantage of the positive osmosis process is that the osmotic pressure difference between the semi-permeable membrane without pressure is used as the driving force for the production of the treated water. Due to the operational characteristics of the osmosis process, In addition, since the problem of membrane contamination due to pressure is relatively small, the replacement cycle and the cleaning cycle of the membrane can be largely increased, so that the maintenance cost and the convenience of the operator can be improved. Which has advantages in terms of cleaning.

Therefore, related studies have been actively carried out for commercialization of the positive osmosis process which has great economic and environmental advantages. Among the various research fields, in particular, the development of a pure osmosis membrane (hereinafter referred to as a "osmosis membrane" Interest is very high.

Since the forward osmosis process operates in a non-pressurized manner, it exhibits a different membrane contamination mechanism than reverse osmosis. In the case of the normal osmosis operation using only the osmotic pressure difference between the influent and the induction solution, a loose and dispersed membrane contaminant layer was observed, and reverse osmosis membrane contamination, which is irreversibly affected by osmotic pressure and mechanical pressure, The membrane contamination layer generated by the reverse osmosis shows reversibility that is recovered above a certain level through physical washing.

Currently, there exist membrane fouling measurement methods and devices for pressurized membranes (MF, UF, NF, RO), but there are no measurement methods and devices that accurately simulate the membrane fouling phenomena.

The membrane membrane fouling measurement method is performed in the push operation mode of the reverse osmosis process. The reverse osmosis process uses a silt density index (SDI) to measure the membrane contamination of membranes in reverse osmosis processes. Here, the SDI (silt density index) is a universal index used as a manufacturer's quality assurance and operating standard in the reverse osmosis membrane. The membrane contamination index (SDI) in the conventional reverse osmosis process is measured by an SDI index measuring instrument.

SDI index measurement equipment is simple and easy to handle. However, it is difficult to predict the membrane contamination of the reverse osmosis process by using MF membrane with pores instead of reverse osmosis membrane (RO) The actual reverse osmosis process proceeds to a cross-flow, and the SDI index measurement proceeds to DEAD-END-TEST, There was a problem that the exponential test conditions were different.

Although the reverse osmosis process can predict the membrane contamination of the reverse osmosis membrane using the SDI index measurement equipment, the reverse osmosis process can predict the membrane contamination of the reverse osmosis membrane, And it is difficult to simulate the normal osmosis process because it does not reflect the actual osmosis operating conditions. In addition, there is no equipment for measuring the membrane contamination index of the positive osmosis membrane.

Therefore, it has been studied whether the application of the membrane contamination index (SDI) of the reverse osmosis process is suitable for measuring the membrane contamination in the forward osmosis process. In order to investigate whether the membrane contamination index of the reverse osmosis process, SDI, can indicate the membrane contamination of the osmosis membrane, the second treatment water of the sewage was used as a feed water and the seawater was used as a draw solution Experiment 1, in which an osmotic membrane was operated, was carried out.

Secondary clarifier effluent from the copper sewage treatment plant (A ² O process) was used for the sewage water treated as influent, and artificial seawater using NaCl 0.6 M (TDS 35,000 mg / L) Respectively. HITE's product of triacetyl cellulose (CTA, cellulose triacetate) was used as the positive osmosis membrane and SW30HR-380 product of DOW filmtec company was used as the reverse osmosis membrane.

As the experimental conditions, the operating temperature was set at 25 ° C. and the recovery rate of the whole process was 50%. When the experiment is conducted under these conditions, the dilution ratio of the purified osmosis treated water and the seawater is 0.7: 1 (purified osmosis treated water: seawater). SESW and MFSW experiments were carried out by dilution with seawater at the same dilution ratio.

The SDI value according to dilution of the raw water and seawater derived by such an experiment is as shown in FIG. 5A. The SDI value according to the dilution of the raw water and the seawater is a result of evaluating how much the raw water has the membrane contamination potential.

In FIG. 5A, SE is sewage secondary treated water, SESW is untreated sewage secondary treated water diluted in seawater, and MFSW uses MF (Millipore, polypropylene, 0.45 mu m) to treat sewage secondary treated water After filtration, it is diluted in seawater. FOSW is diluted with seawater by using the osmotic dilution effect by the secondary osmosis membrane.

In FIG. 5A, the SDI value of SE is 6.42 ± 0.5, which is much higher than the SDI 3 recommended for operating a reverse osmosis membrane.

Although the SDI values of SESW and MFSW were also diluted to 6.11 ± 0.48 and 5.04 ± 0.33, respectively, the SDI value still showed a value of 3 or more, indicating a membrane contamination potential which is difficult to use for the reverse osmosis membrane. The preprocessing cost may be incurred during operation.

However, in the case of FOSW diluted with seawater by using the osmotic dilution effect of the secondary treatment water of sewage water, the SDI value of FOSW is 1.28 ± 0.12, which is the only membrane contamination potential suitable for the recommended level of SDI 3 or lower .

Also, through the above experiment, it can be seen that the SDI, which is a membrane contamination index of the conventional reverse osmosis process, is used to measure the membrane fouling of the positive osmosis membrane, but not to the membrane. In addition, it was confirmed that the osmotic dilution method of diluting the production water treated with the forward osmosis (FO) with the secondary treatment water (SE) of the sewage water was the best method in terms of membrane contamination. At the same time, It can be concluded that water treatment is possible through the above-mentioned water-based normal osmosis membrane. Accordingly, it is required to develop a technology capable of calculating the film contamination index in the forward osmosis process which can simulate membrane fouling of the forward osmosis membrane and predict membrane fouling from the osmosis membrane.

Meanwhile, Korean Patent No. 10-1560524 discloses an apparatus and method for real-time membrane contamination monitoring in a cleansing vessel.

The present invention relates to a device for predicting and predicting the contamination of a forward osmosis membrane produced by a seawater desalination process, a filtration process, a dewatering process, and a concentration process using a forward osmosis method, And a method for predicting contamination.

In the present invention, the membrane contamination of the positive osmosis membrane used in the positive osmosis process is simulated by using the positive osmosis membrane which is reflected on the environmental factors applied in the field and is actually used, An apparatus for predicting membrane fouling in a forward osmosis membrane, which can estimate the membrane fouling of the forward osmosis membrane from the ortho-osmosis membrane fouling index (OFI) by calculating the osmosis membrane fouling index (OFI) based on measured membrane fouling data, And a method for predicting membrane fouling.

In the present invention, the positive osmosis film contamination index (OFI) due to the membrane contamination of the positive osmosis membrane is calculated in the positive osmosis process by reflecting all advantages and disadvantages of the apparatus for measuring the membrane contamination index (SDI) of the conventional reverse osmosis process, Which is capable of predicting membrane fouling of the forward osmosis membrane in the process of the present invention.

An apparatus for predicting a normal osmosis membrane fouling according to an embodiment of the present invention includes a membrane contamination simulator having a normal osmosis membrane and simulating membrane contamination of the osmosis membrane in a normal osmosis process; An influent supply unit connected to the membrane contamination simulator to provide a primary influent in the forward osmosis process and a secondary influent having a flow rate greater than the primary influent in the washing process; An induction solution supply unit connected to the membrane contamination simulation unit to supply an induction solution having a concentration higher than that of the primary influent water in the forward osmosis process; (OFI) is measured by measuring the water permeation amount of the first influent passing through the positive osmosis membrane according to the elapsed time of the operation of the osmosis process, and the osmosis membrane membrane fouling index (OFI) Wherein the induction solution supply part accelerates the formation of the adherent layer by providing the induction solution to the membrane contamination simulation part while adjusting the molar concentration, and the membrane contamination simulation part is provided with a first influent water During the flow of water in the first influent water through the positive osmotic membrane to the space containing the induction solution by the osmotic pressure due to the difference in concentration between the induction solutions, the organic matter of the first influent water is accumulated on the surface of the positive osmotic membrane It is preferable to simulate membrane contamination of the positive osmosis membrane.

In one embodiment of the present invention, the film fouling predicting unit predicts the membrane fouling with the elapse of the operating time. The membrane fouling predicting unit predicts the membrane permeation amount of the first influent water passing through the positive osmosis membrane at the beginning of the positive osmosis membrane, The permeation amount (J1) and the third water permeation amount (J3), which is the water permeation amount of the first influent passing through the positive osmosis membrane in the positive osmosis process after the adhesion layer of the positive osmosis membrane is removed by the washing process, It is preferable that the film contamination index (OFI) is calculated by the recovery rate of the third water permeation amount (J3) relative to the first water permeation amount (J1).

In one embodiment of the present invention, the film fouling predicting unit determines that the membrane fouling predicting unit is in the range of greater than the threshold reversibility (Rc) and less than 1 (Rc <OFI < (Rc) is the number of the first influent after the washing process with respect to the water permeation amount of the first influent before the washing process in which the membrane contamination of the positive osmosis membrane can not be recovered only by the physical washing with the second influent. It is preferable that the recovery rate of the permeation amount is.

In one embodiment of the present invention, in the film fouling predicting portion, the water permeation amount of the first influent water passing through the positive osmosis membrane is gradually converged to be lower than the first water permeation amount J1 by the adhesive layer formed on the surface of the positive osmosis membrane When the second water permeation amount J2 is measured, the influent water supply unit supplies the second influent water to the membrane contamination simulation unit at the time when the second water permeation amount J2 is measured, and the induction solution supply unit supplies the second water inflow water It is preferred that the layer be washed to remove the adhesive layer.

In one embodiment of the present invention, a TDS controller is connected to the inductive solution supply, and the TDS controller adjusts the total dissolved solids (TDS) of the inductive solution provided to the membrane contamination simulator, It is preferable to adjust the first water permeation amount due to the difference in TDS.

On the other hand, a method for predicting membrane fouling in a forward osmosis membrane process using a forward osmosis membrane fouling predicting apparatus includes the steps of (A) predicting a primary osmosis membrane fouling The osmosis process is performed by the osmotic pressure due to the difference in the concentration of the induction solution in the influent and the induction solution. The membrane contamination of the osmosis membrane by the adherent layer formed by accumulating the organic matter of the first influent water on the surface of the osmosis membrane is simulated step; (B) providing a second influent water to the membrane contamination simulator at the influent supply portion to clean the positive osmosis membrane by the second influent; And (C) the water permeation amount of the primary influent passing through the positive osmosis membrane is measured according to the elapsed operation time and the number of operation of the positive osmosis process, and the positive osmosis membrane contamination index (OFI) is calculated from the equation (1) It is preferable to include the step of predicting membrane contamination of the positive osmosis membrane from the osmotic membrane pollution index (OFI).

..........................식(1)

.......................... Equation (1)

Wherein J1 is a first water permeation amount which is the water permeation amount of the first influent passing through the positive osmosis membrane at the beginning of the positive osmosis membrane before the adherent layer is formed in the positive osmosis membrane, And the third water permeation amount which is the water permeation amount of the first influent water passing through the positive osmosis membrane in the forward osmosis process after being removed by the second osmosis membrane.

According to an embodiment of the present invention, the step (B) may further include, in accordance with passage of the operation time of the forward osmosis process, a water permeation amount of the first influent water passing through the osmosis membrane is gradually At the time of converging to the second water permeation amount (J2, J1 > J2), the cleansing of the normal osmosis membrane by the second influent water proceeds and the membrane layer of the normal osmosis membrane is recovered .

According to an embodiment of the present invention, the step (C) includes: (C1) predicting that when the normal osmosis membrane fouling index (OFI) is calculated to be greater than 1 (1 <OFI) Stopping the operation of the process; (C2) If the normal osmosis membrane pollution index (OFI) is calculated as 1 (OFI = 1), the operation of the forward osmosis process is continued by predicting that the forward osmosis membrane is not contaminated; (C3) Predict membrane fouling in the positive osmosis membrane when the positive osmosis membrane fouling index (OFI) is greater than the critical reversibility (Rc) and less than 1 (Rc <OFI <1) B) washing step; (Rc > OFI), it is predicted that the positively osmosis membrane can not recover the membrane contamination only by physical washing with the second influent water, and if (C4) the positive osmosis membrane contamination index (OFI) is smaller than the critical reversibility (Rc) (Rc) is a step of repeatedly performing the positive osmosis process and the washing process to perform physical washing only with the second influent water to perform the positive osmosis membrane in the membrane that can not be contamination of the recovered state, that the recovery ratio of the three primary transmission amount of influent can _{(after washing} J) after the process for the primary transmission amount of inlet water can be pre-washing step (J _{before washing)} is preferred.

In one embodiment of the present invention, in step (A), it is preferred that the derivatization solution is supplied to the membrane contamination simulator with a controlled molar concentration to accelerate the formation of the adherent layer.

In one embodiment of the present invention, in the step (A), the total dissolved solids (TDS) of the derivatized solution provided by the TDS controller to the membrane contamination simulator are controlled, and the first water permeation amount is controlled by the first influent water It is preferred to be controlled by the difference between the TDS and the TDS of the derivatized solution.

The present invention can simulate the membrane contamination of the positive osmosis membrane in a short period of time by shortening the time of membrane fouling by the positive osmosis process using the reversible and high concentration inductive solution of the positive osmosis membrane by utilizing the actually used osmosis membrane.

The present invention can calculate the ortho-osmosis membrane fouling index (OFI) by reflecting the water permeation amount measured in the membrane fouling-impregnated osmosis membrane and the characteristics of the osmosis membrane, and the osmosis membrane membrane fouling index (OFI) Membrane contamination of the membrane can be predicted.

FIG. 1 schematically shows a configuration of an apparatus for predicting a normal osmosis membrane fouling according to an embodiment of the present invention. Referring to FIG.
FIG. 2 is a graph showing the operation time-membrane fouling reversibility according to the molar concentration change of the induction solution.
FIG. 3 is a graph illustrating a water permeation amount according to time with respect to time before and after physical cleaning according to an embodiment of the present invention.
4 schematically illustrates a flow diagram of a method for predicting a normal osmosis membrane fouling according to an embodiment of the present invention.
FIG. 5A shows the results of SDI according to the raw water and sea water dilution method in Experiment 1. FIG.
FIG. 5B is a graph showing the water permeation amount and membrane fouling reversibility of the positive osmosis membrane according to the pressure or reduced pressure conditions in Experiment 2. FIG.
FIG. 5C is a graph of membrane fouling reversibility according to the number of times of operation under the conditions of pressurization and osmotic pressure in Experiment 3. FIG.
5D is a graph of SDI and TDS for four sewage treatment plants.
FIG. 5E is a graph showing the water fluxes of four sewage treatment plant secondary treatment water according to the operation time under the same TDS (250 mg / L) condition.
Figure 5f shows a graph of membrane fouling reversibility for the number of runs of four sewage treatment plants.
Figure 5g is a graph of the concentration of organics in the secondary treated water for four sewage treatment plants.
5H is a graph showing the concentration of four types of organic substances attached to the positive osmosis membrane according to the washing cycle.
FIG. 5I is a graph showing the membrane fouling reversibility of the positive osmosis membrane according to the flow rate, which is a physical washing condition, according to the driving cycle.

Hereinafter, an apparatus for predicting a normal osmosis membrane fouling and a method for predicting a normal osmosis membrane fouling according to a preferred embodiment of the present invention will be described with reference to the accompanying drawings.

As described in the Background of the Invention, according to the conclusion that SDI, which is a membrane contamination index of the conventional reverse osmosis process, can not be used for membrane contamination of the osmosis membrane, the present invention simulates the contamination of the osmosis membrane, This study was conducted to develop and analyze the membrane fouling of the forward osmosis membranes.

As shown in FIG. 1, the apparatus for predicting the normal osmosis membrane fouling according to an embodiment of the present invention is a component for simulating a normal osmosis process and measuring a normal osmosis membrane fouling index, An induction solution supply unit 120, a membrane contamination simulation unit 130, and a membrane contamination prediction unit 140.

First, the membrane contamination simulation of the normal osmosis membrane 131 by the normal osmosis process is performed by the influent supply portion 110, the induction solution supply portion 120 and the membrane contamination simulation portion 130.

The influent supply portion 110 is connected to the membrane contamination simulator 130. The inflow water supply unit 110 includes an inflow water storage tank 111, a first inflow water pipe 112, a first pump 113 and a second inflow water pipe 114.

The inflow water storage tank 111 is a tank in which inflow water is stored. The influent water is treated in the seawater desalination process, filtration process, dehydration process, and concentration process using the forward osmosis process.

The first inflow water pipe 112 connects the inflow water storage tank 111 and the first inlet 132a of the membrane contamination simulating unit 130. Here, the inflow water flowing through the first inflow water pipe 112 is moved from the inflow water storage tank 111 to the membrane contamination simulator 130. A first pump 113 is connected to the first inflow water pipe 112 for smooth flow of inflow water flowing through the first inflow water pipe 112. The first pump 113 sucks inflow water stored in the inflow water storage tank 111 and supplies the inflow water to the membrane contamination simulator 130.

The second inflow water pipe 114 connects the inflow water storage tank 111 and the first outlet 132b of the membrane contamination simulator 130. The influent water flowing through the second inflow water pipe 114 is concentrated water concentrated by the forward osmosis process with the induction solution in the membrane contamination simulator 130. The influent water flowing through the second inflow water pipe 114 flows from the membrane contamination simulator 130 into the inflow water storage tank 111 .

In the present embodiment, for convenience of explanation, the inflow water supplied in the forward osmosis process will be referred to as a 'primary inflow water', and the inflow water supplied in the cleaning process will be referred to as a 'secondary inflow water'. Here, the second influent water has a higher flow velocity than the first influent water. In this example, the primary influent is circulated along the arrow F1 during the forward osmosis process and the secondary influent circulates along the arrow F2 during the washing process.

The induction solution supply part 120 is for providing an induction solution during the positive osmosis process. The inducing solution supply portion may be provided to the membrane contamination simulator 130 while controlling the molar concentration of the inducing solution to accelerate the formation of the adhesion layer.

The induction solution supply unit 120 includes an induction solution storage tank 121, a first induction solution tube 122, a second pump 123, a second induction solution tube 124 and a TDS controller 125.

The induction solution storage tank 121 is a tank storing the induction solution. The induction solution has a higher concentration than the primary influent.

The first induction solution tube 122 connects the induction solution storage tank 121 and the second outlet 133b of the membrane contamination simulator 130. [ Here, the induction solution flowing through the first induction solution pipe 122 is transferred from the membrane contamination simulator 130 to the induction solution storage tank 121. Here, the induction solution flowing through the first induction solution pipe 122 is diluted by the positive infiltration process with the primary influent in the membrane contamination simulator 130.

A second pump 123 is connected to the first induction solution tube 122 for smooth flow of the induction solution flowing through the first induction solution tube 122. The second pump 123 sucks the inductive solution discharged from the membrane contamination simulator 130 and supplies it to the inductive solution storage tank 121.

The second induction solution tube 124 connects the induction solution storage tank 121 and the second inlet 133a of the membrane contamination simulator 130. Here, the induction solution flowing through the second induction solution tube 124 is a substance having a higher concentration than the first influent water.

The TDS controller 125 is connected to the inductive solution storage tank 121. The TDS controller 125 regulates the total dissolved solids (TDS) of the inductive solution provided to the membrane contamination simulator 130. The TDS controller 125 can adjust the TDS of the inductive solution to adjust the first water permeation amount. Here, the first water permeation amount is due to the difference between the TDS of the primary influent and the TDS of the derivatizing solution. The first water permeation amount J1 is the water permeation amount of the first influent water passing through the positive osmosis membrane 131 at the beginning of the normal osmosis process before the adherent layer is formed in the normal osmosis membrane 131. [

The membrane contamination simulation unit 130 is for performing a normal osmosis process and simulating membrane contamination of the osmosis membrane 131 by a repetitive positive osmosis process. The membrane contamination simulation unit 130 includes a first space 132 and a second space 133 separated by the osmosis membrane 131.

The membrane contamination simulation unit 130 has a first inlet 132a and a first outlet 132b at a portion where the first space 132 is provided. A first inlet water pipe 112 is connected to the first inlet 132a and a second inlet water pipe 114 is connected to the first outlet pipe 132b.

The first space 132 is a space in which inflow water circulating through the inflow water supply unit 110 is stored. In the forward osmosis process, the primary inflow water flows along the arrow F1 along the direction of arrow F1 from the inflow water storage tank 111 to the first inflow water pipe 112 to the first space 132 of the membrane contamination simulation unit 130, (114) -> the inflow water storage tank (111).

The membrane contamination simulation unit 130 is provided with a second inlet 133a and a second outlet 133b at a portion where the second space 133 is provided. A second induction solution tube 124 is connected to the second inlet 133a and a first induction solution tube 122 is connected to the second outlet 133b. The second space 133 is a space in which the induction solution circulating in the induction solution supply unit 120 is stored.

The induction solution circulates through the induction solution supply part 120 and the membrane contamination simulator 130 along F3. Specifically, the induction solution is introduced into the induction solution storage tank 121, the second induction solution tube 124, the second space 133 of the membrane contamination simulation unit 130, and the first induction solution tube 122) - > induction solution storage tank (121). At this time, the circulating direction F3 of the inducing solution is opposite to the circulating direction F1 of the primary influent.

The primary influent water is cross-flowed in a state separated from the induction solution by the positive osmosis membrane 131 and the osmotic pressure on the osmosis membrane 131 due to the difference in concentration between the primary influent and the induction solution The low-concentration primary influent water is transferred to the high-concentration induction solution.

In this process, as the water of the primary influent water moves from the first space 132 to the second space 133, an organic substance in the primary influent water accumulates on the surface of the forward osmosis membrane 131 to form an adherent layer . The positive osmosis membrane (131) is contaminated by the adherent layer.

As shown in Fig. 2, the rate of formation of the adhesion layer in the positive osmosis membrane 131 varies depending on the molar concentration of the derivatized solution. FIG. 2 is a graph showing the operation time-membrane fouling reversibility according to the molar concentration change of the induction solution. Here, membrane fouling reversibility refers to the recovery ability of the positive osmosis membrane 131 due to physical cleaning.

The operation time according to the molar concentration change of the induction solution - the membrane contamination reversibility graph shows that the recovery rate of the purified osmosis membrane 131 was recovered before and after the washing process, as the cleansing process and the cleansing process were repeatedly performed in a cycle of 5 minutes to 10 minutes Is the result value.

Referring to FIG. 2, when washing is carried out after driving for about 20 to 30 minutes at a molar concentration with 3 M of the induction solution, sufficient experimental results can be obtained that the critical reversibility (Rc) is reached. This is in accordance with the graph of FIG. 5F, which is consistent with the membrane contamination reversibility which was repeated 5 times using the inductive solution of the seawater condition.

Referring to FIG. 2, the membrane contamination reversibility of the positive osmosis membrane 131 is converged to 75% over time in the case of performing a positive osmosis process using a 2M induction solution, while using an induction solution of 3M or more It can be seen that when the forward osmosis process is carried out, it converges to about 60%. In other words, the concentration of 2M did not show enough experimental results. Although 4M can shorten the time, 3M is the most economical considering the cost of chemicals and equipment corrosion.

2, it can be seen that the membrane contamination reversibility of the osmosis membrane separation membrane 131 decreases sharply as the molar concentration of the derivatization solution increases. Accordingly, it can be seen that the higher the molar concentration of the derivatizing solution, the faster the adhesion layer adhered to the positive osmosis membrane separation membrane 131 is.

When the positive osmosis membrane separation membrane 131 is membrane-contaminated by the above-described normal osmosis process, the positive osmosis membrane 131 that is contaminated with membranes is washed by the secondary influent water to recover membrane contamination of the normal osmosis membrane separation membrane 131.

The second inflow water flows along the arrow F2 from the inflow water storage tank 111 to the first inflow water pipe 112 to the first space 132 of the membrane contamination simulator 130 to the second inflow water pipe 114) -> circulates the inflow water storage tank 111. Here, the circulating direction F2 of the second influent water is the same as the circulating direction F1 of the first influent water.

The second influent has a higher flow rate than the first influent. The secondary inflow water circulates through the inflow water supply unit 110 and the membrane contamination simulator 130 at a high flow rate to clean the osmosis membrane 131.

The second influent water is supplied to the membrane contamination simulator 130 at the time when the second water permeation amount J2 is measured. When the secondary inflow water circulates through the membrane contamination simulation unit 130, the supply of the induction solution to the membrane contamination simulation unit 130 of the induction solution supply unit 120 is stopped.

As shown in FIG. 3, the second water permeation amount J2 is set such that the water permeation amount of the primary influent water passing through the osmosis membrane 131 by the adhesive layer formed on the surface of the osmosis membrane separation membrane 131, And the water permeability is constantly converged.

Hereinafter, a film contamination predicting unit 140 for predicting film contamination of the positive osmosis membrane 131 by measuring a positive osmosis film contamination index (OFI) will be described.

The membrane contamination predicting unit 140 estimates the amount of permeation of the first influent water passing through the osmosis membrane 131 by the first water permeation amount J1 and the second water permeation amount J2, The membrane permeation amount J3 is measured, and the osmosis membrane membrane fouling index (OFI) is calculated therefrom. The film fouling of the osmosis membrane separation membrane 131 is predicted from the osmosis membrane membrane fouling index (OFI).

The first water permeation amount J1 is the water permeation amount of the first influent water passing through the positive osmosis membrane 131 at the beginning of the positive osmosis process before the adherent layer is formed on the positive osmosis membrane 131. [

As described above, the second water permeation amount J2 is set such that the water permeation amount of the first influent water passing through the osmosis membrane 131 by the adhesive layer formed on the surface of the osmosis membrane 131 is constantly converged Is the permeation amount.

The third water permeation amount J3 is the water permeation amount of the first influent water passing through the osmosis membrane 131 in the forward osmosis process after the adherent layer of the osmosis membrane separation membrane 131 is removed by the washing process.

The normal osmosis film contamination index (OFI) is calculated from the first water permeation amount (J1) and the third water permeation amount (J3). The normal osmosis membrane contamination index (OFI) is the recovery rate of the third water permeation amount (J3) to the first water permeation amount (J1).

The positive osmosis membrane fouling index (OFI) is determined by washing the positive osmosis membrane (131) membrane-contaminated by the adherent layer with the secondary influent, passing through the positive osmosis membrane (131) Is an index of how much the third water permeation amount J3 of the influent water is recovered in comparison with the first water permeation amount J1 at the beginning of the normal osmosis process.

The film contamination predicting unit 140 predicts that the positive osmosis membrane 131 is film-contaminated when the positive osmosis film contamination index (OFI) is greater than the critical reversibility Rc and smaller than 1 (Rc <OFI <1). Here, the critical reversibility Rc is reversibility of the membrane contamination in the state where the membrane contamination of the osmosis membrane 131 is not recoverable only by physical washing with the second influent water according to repetitive execution of the cleansing process and the cleansing process.

The critical reversibility (Rc) is a constant convergence of membrane contamination reversibility with time. As described above, the membrane fouling reversibility is a recovery capability of the purified osmosis membrane 131 due to physical cleaning, and is a recovery rate of the water permeation amount of the first influent water after the washing process with respect to the water permeation amount of the first influent water before the washing process.

Hereinafter, with reference to FIG. 4, a description will be made of a method for predicting the fouling of the osmosis membrane according to an embodiment of the present invention. The method for predicting the normal osmosis membrane fouling is a method for predicting the membrane fouling in the forward osmosis process using the apparatus for predicting the osmosis membrane fouling (100).

First, actual operating conditions considering variables are applied to simulate film contamination of the forward osmosis membrane 131 by the forward osmosis process in the membrane contamination simulator 130 (S1). That is, by the osmotic pressure due to the difference in concentration of the primary influent water of the inflow water supply unit 110 supplied to the membrane contamination simulation unit 130 of the apparatus for predicting the normal osmosis membrane fouling and the concentration of the inductive solution in the induction solution supply unit 120, As the osmosis process is performed, membrane contamination of the osmosis membrane 131 by the adherent layer formed by accumulating the organic matter of the first influent water is simulated on the surface of the osmosis membrane 131.

At this time, the induction solution may be supplied to the membrane contamination simulator 130 with a controlled molar concentration to accelerate the formation of the adhesion layer. Then, the TDS controller 125 controls the total dissolved solids (TDS) of the derivatized solution supplied to the membrane contamination simulator 130. The first water permeation amount is controlled by the difference between the TDS of the primary influent and the TDS of the derivatizing solution. Here, the first water permeation amount is the water permeation amount of the first influent water passing through the positive osmosis membrane 131 at the beginning of the positive osmosis process before the adherent layer is formed in the positive osmosis membrane 131.

Thereafter, the membrane contamination predicting unit 140 measures the permeation amount of the primary influent water passing through the osmosis membrane 131 in accordance with the elapsed operation time and the number of operation times of the normal osmosis process in the membrane contamination simulator 130 , From which a normal osmosis membrane contamination index (OFI) is calculated (S2). It is desirable that the ortho-osmotic membrane contamination index (OFI) is greater than the critical reversibility (Rc).

The normal osmosis membrane contamination index (OFI) is calculated by equation (1).

..........................식(1)

.......................... Equation (1)

In the formula (1), J1 is the first water permeation amount, and J3 is the number of the first influent water passing through the forward osmosis membrane 131 in the forward osmosis process after the adhesion layer of the osmosis membrane separation membrane 131 is removed by the washing process Which is the water permeation amount of the water.

Then, the film contamination predicting unit 140 predicts whether or not the film of the positive osmosis separating membrane 131 is contaminated from the positively osmosis membrane film contamination index (OFI).

If the positive osmosis film contamination index (OFI) is calculated to be greater than 1 (1 <OFI), the film fouling predicting unit 140 predicts that the positive osmosis membrane 131 is damaged (S3). In the case where the normal osmosis membrane separation membrane 131 is damaged, the normal osmosis process in the membrane contamination simulator 130 is stopped.

Next, when the ortho-osmosis membrane fouling index (OFI) is calculated as 1 (OFI = 1), the membrane fouling predicting unit 140 predicts that the osmosis membrane separation membrane 131 is not contaminated (S4). In this case, the forward osmosis process in the membrane contamination simulator 130 is continued.

The film fouling predicting unit 140 predicts that the osmosis membrane separation membrane 131 is in a state of being contaminated with membranes (Rc <OFI <1) when the ortho-osmosis membrane fouling index (OFI) is larger than the critical reversibility (Rc) At this time, cleaning of the positive osmosis membrane 131 is performed (S5). This is to recover the membrane contamination of the normal permeable membrane as the adherent layer is removed from the positive osmotic permeable membrane 131 by washing the positive osmotic membrane 131 with the second influent.

During the washing of the osmosis membrane (131), the operation of the osmosis process is stopped. In the inflow water supply unit 110, the second inflow water is supplied to the membrane contamination simulation unit 130, and the positive osmosis separation membrane 131 is cleaned by the second inflow water. The washing water passes through the forward osmosis membrane separation membrane 131, and the water permeation amount of the first influent water gradually decreases from the first water permeation amount J1 by the adhesive layer as the operation time of the forward osmosis process progresses. J2, J1 > J2).

The critical reversibility (Rc) is determined by repeating the positive osmosis process and the washing process. In this state, it is impossible to recover the membrane contamination of the osmosis membrane (131) only by physical washing with the second influent water. Is the recovery rate of the water permeation amount (after the J _washing ) of the first influent water after the washing process with respect to the permeation amount (before the J _washing ), and is calculated by the equation (2).

............................식 (2)

............................ Equation (2)

The critical reversibility (Rc) is the membrane contamination reversibility (R) in a state where the membrane contamination of the osmosis membrane (131) can not be recovered only by physical washing with the second influent according to repetitive performance of the cleansing process and the washing process. The membrane contamination reversibility (R) is calculated by equation (2).

The critical reversibility (Rc) is a constant convergence of membrane contamination reversibility with time. As described above, the membrane fouling reversibility is a recovery capability of the purified osmosis membrane 131 due to physical cleaning, and is a recovery rate of the water permeation amount of the first influent water after the washing process with respect to the water permeation amount of the first influent water before the washing process.

The water permeation amount ( _before J _cleaning ) of the first influent water before the washing process corresponds to the first water permeation amount J1 described above, and the water permeation amount (after J _cleaning ) of the first influent water after the washing process is the third water permeation amount J3).

However, the water permeation amount ( _{before the} J _cleaning ) of the first influent water before the cleaning process applied to the critical reversibility can be maintained even when the number of times of operation of the positive osmosis process is increased because the adhered layer stacked on the positive osmosis membrane 131 is not removed by physical washing The first water permeation amount is the water permeation amount before the washing operation in the initial operation of the normal osmosis process and the measured water permeation amount values are different from each other.

The water permeation amount ( _{after cleaning} J) of the first influent water after the washing process applied to the critical reversibility is such that the adhesive layer deposited on the osmosis membrane 131 is not removed by physical washing so that even if the number of operation of the osmosis membrane process is increased, While the third water permeation amount is a water permeation amount when the adhesion layer is removed from the osmosis membrane separation membrane 131 by washing.

On the other hand, if the positive osmosis membrane fouling index (OFI) is smaller than the critical reversibility (Rc) (Rc> OFI), it is predicted that the positive osmosis membrane separation membrane 131 can not recover the membrane fouling by physical washing with the second influent water , The operation of the normal osmosis process is stopped, and a pretreatment process such as chemical cleaning is performed (S6).

The present invention can measure and predict the membrane fouling of the forward osmosis membrane by simulating the osmosis membrane fouling and developing the osmosis membrane fouling index reflecting variables by environmental factors applied in the field.

The present invention can more precisely measure and predict the contamination phenomenon of the forward osmosis membrane caused by the seawater desalination process, the filtration process, the dehydration process, and the concentration process using the forward osmosis process.

Hereinafter, an experimental result on why the membrane contamination simulation of the positive osmosis membrane is performed by the osmotic pressure in the membrane contamination simulator, an experiment applied to derive the formula for calculating the positive osmosis membrane contamination index (OFI) .

As described in the Background of the Invention, it can be concluded that existing membrane contamination indexes can not be used for membrane contamination of the positive osmosis membrane and that a new method of simulating the osmosis membrane membrane contamination is needed, Experiment 2 was carried out.

There is a method of simulating the membrane contamination by pressurization, decompression, and osmotic pressure as a method of simulating the membrane contamination of the membrane. Experiment 2 simulates membrane contamination in the osmosis membrane under pressurized or reduced pressure conditions.

In Experiment 2, the membrane contamination simulation method using the reduced pressure condition simulates membrane contamination by reducing the pressure to about 1 bar by using a vacuum pump in the absence of osmotic pressure without the use of a draw solution. The membrane contamination simulation method using the pressurized condition simulates membrane contamination by applying a pressure of 1 bar to 9 bar to the positive osmosis membrane using a pump in the same manner as the reverse osmosis membrane operation mode.

FIG. 5B is a graph showing the water permeation amount and reversibility of the positive osmosis membrane according to the pressure or reduced pressure conditions in Experiment 2. FIG.

The membrane fouling reversibility was calculated by Eq. (2).

............................식 (2)

............................ Equation (2)

J is the flux of _water at 8.54 cm / s for 70 hours of operation. After washing for 10 minutes, the flow rate is increased by 3 times to 25.62 cm / s after J _{washing and} 8.54 cm / s And is the flux measured during operation.

Referring to FIG. 5B, it can be seen from the experimental results of the reduced pressure condition that the flux is hardly generated in the quasi-osmosis membrane, and the fouling layer is formed on the surface of the membrane because the water flux is very low. The membrane fouling reversibility was measured close to 100%. According to these results, it can be concluded that when the membrane contamination is simulated by the decompression method, the operation of the osmosis membrane is difficult and the membrane contamination can not occur.

Referring to FIG. 5B, the experimental result of the pressurization condition shows that a very small flux of about 1 LMH is generated at a pressure of 1 bar, and a flux of 7 LMH is obtained at a pressure of 7 bar. .

The results show that the recovery capability of the membrane by physical washing can be expressed as membrane fouling reversibility. According to the results in Fig. 1b, membrane at 7 bar, which is the condition for obtaining the initial flux, Fouling reversibility was observed to be about 50%.

Then, Experiment 3 was conducted to verify whether the pressurized condition sufficiently reflected the film contamination phenomenon under the condition of the normal osmosis, and the results of Experiment 3 are shown in Fig. 5C.

In Experiment 3, the pressurizing condition is a case where a pressure of 7 bar is applied to the positive osmosis membrane, and the condition using osmotic pressure is an induction solution having higher osmotic pressure than the influent water flowing into the apparatus. The first permeation amount was 7 LMH, the operation time was 70 minutes, and the physical washing with 3 times flow rate was performed without changing the membrane for 10 minutes under the conditions using the pressurization condition and the osmotic pressure.

FIG. 5C is a graph of membrane fouling reversibility according to the operating cycle under the conditions using the pressurizing condition and the osmotic pressure.

Referring to FIG. 5C, it can be seen that the reverse osmosis membrane operated under the pressurized condition has a reversibility of 50% from the first operation. On the other hand, the osmotic pressure-driven forward osmosis membrane exhibits nearly 100% reversibility in the first operation, and has a fouling reversibility of 80% even after four repetitions of operation. That is, it can be seen that the positive osmosis membrane operated by osmotic pressure has higher reversibility than the positive osmosis membrane at the pressurized condition even when the number of operation is increased.

According to the above experimental results, when the osmosis membrane is operated under the conditions of decompression and pressurization, when the osmosis membrane is operated under the depressurization type, there is a difficulty in operating the osmosis process due to insufficient driving force. It can be concluded that it is difficult to simulate the high membrane fouling reversibility of the positive osmosis membranes because the membrane pollution layer is consolidated when the membrane is operated, and the membrane recovery ability, which is one of the characteristics of the positive osmosis membrane, does not appear. Thus, it can be concluded that osmotic pressure should be used to simulate membrane contamination of the positive osmosis membrane.

Therefore, Experiment 4 was carried out to determine what factor influences membrane fouling index in the forward osmosis process when osmotic pressure is used to simulate membrane fouling of the osmosis membrane.

For the experiment 4, the sewage secondary treatment water of four sewage treatment plants (Jungang, Tancheon, Nanji, Copper) near Seoul was collected. This is to ensure the representativeness of the raw water used by selecting a small- and medium-sized sewage treatment plant from a sewage treatment plant having a very large capacity.

Table 1 shows the results of water quality analysis of the secondary treated water in four sewage treatment plants.

Sewage treatment plant Processing method Processing capacity
(M ³ / d) BOD COD SS T-N T-P Jungang A ² O + aggregation 159 5.7 ± 0.1 12.4 ± 0.3 7.6 ± 0.4 9.3 ± 0.6 0.18 + 0.02 Tancheon MLE + aggregation 90 5.4 ± 0.3 10.9 ± 0.5 9.4 ± 0.6 7.3 ± 0.7 0.15 + 0.08 Nanji MLE + aggregation 86 6.8 ± 0.2 13.4 ± 0.5 4.7 ± 0.5 8.3 ± 0.2 0.17 ± 0.05 Copper A ² O + aggregation 11 4.6 ± 0.2 10.4 ± 0.4 6.3 ± 0.5 7.4 ± 0.5 0.12 ± 0.05

In Table 1, MLE is the Modified Ludzack Ettinger process and A ² O is the Anaerobic-Anoxic-Aerobic process.

Since the initial water permeation amount is determined by the TDS difference between the feed water and the draw soultion in the forward osmosis process, the secondary treatment water of the four sewage treatment plants is subjected to the same concentration ( TDS 250 mg / L) was diluted with DI water (Deionized water) to conduct experiment 4.

The pure osmotic membrane used in this experiment was a PA membrane made by Toray Co., Ltd. The draw solution was filtered with 0.45 ㎛ PP membrane after collecting seawater from the sea in Hangdong, Jung-gu, Incheon (TDS 31,900 ± 200 mg / L ).

The raw water to be used was diluted with DI water to an SDI of 5.5 and then subjected to a forward osmosis membrane experiment. This experiment was carried out in order to observe the difference between flux and reversiblity in the case that the membrane contamination index is the same but the characteristics of the foulant existing in the raw water are different.

In Experiment 4, TDS and SDI were measured to evaluate membrane contamination potential of the raw water to be used. Referring to FIG. 5D, all the secondary treated water of the four sewage treatment plants were observed to have a SDI of 6 or more and a TDS of 280 mg / L or more. 5D is a graph of SDI and TDS for four sewage treatment plants.

Referring to FIG. 5E, when the initial water permeation amount was adjusted to about 25 LMH under the same osmotic pressure condition, it was difficult to observe the membrane pollution tendency only by the water flux. In the case of the forward osmosis membrane, there is no trend of membrane fouling in a short-term operation. Therefore, it is necessary to analyze membrane fouling tendency by long-term operation. Here, FIG. 5E is a graph showing the water fluxes of four sewage treatment plant secondary treatment water according to the operation time under the same TDS (250 mg / L) condition.

However, the prediction of membrane fouling through long-term observation is difficult to apply in the field where membrane pollution is required immediately and it is unnecessary to predict after membrane pollution has already progressed. Therefore, the newly developed osmosis membrane membrane pollution index is artificially high A method of accelerating membrane contamination by generating osmotic pressure and shortening the measurement time should be applied. In the present invention, as described above, a high concentration of the induction solution is used in order to shorten the time for measuring the contamination of the membrane.

Referring to FIG. 5F, after repeated physical washing (flow rate 3 times, 10 minutes) and repeated 10 times without membrane replacement, membrane fouling reversibility decreased to 55% at maximum, and even though the same SDI value And shows different membrane fouling reversibility for each water source. Figure 5f shows a graph of membrane fouling reversibility for the number of runs of four sewage treatment plants.

It can be seen from the graph shown in FIG. 5F that the membrane contamination index used in the conventional reverse osmosis process can not be utilized. Therefore, it is derived that the characteristics of the foulant in the raw water, that is, the factor causing the reversibility difference of the osmosis membrane, should be reflected in the osmosis membrane membrane fouling index, so that accurate membrane contamination simulation can be performed.

On the other hand, referring to FIG. 5F, it can be seen that the recovery rate of membrane fouling reversibility is the lowest, and the minimum recovery rate is close to that of the other sewage treatment plants in the Tancheon sewage treatment plant.

Therefore, the surface of the forward osmosis membrane tested with the secondary treated water of the Tancheon sewage treatment plant, which showed the lowest fouling reversibility, was examined at each washing cycle, and then the organics forming the fouling layer The analysis was performed with LC-OCD, and the results of the experiments performed are shown in Figure 5g. Figure 5g is a graph of the concentration of organics in the secondary treated water for four sewage treatment plants.

Referring to FIG. 5G, the organic matter distribution of the secondary treated water in the four sewage treatment plants exists at a similar ratio, and all of them are based on biological treatment, humics are the largest proportion, and trace amounts of biopolymers biopolymers) are also present.

Referring to FIG. 5H, it can be observed that all four organic materials such as biopolymers, humics, building blocks, and low MW neutrals are easily removed from the surface of the positive osmosis membrane by physical washing. However, it can be observed that the material accumulates on the surface of the osmotic membrane at a slight amount during each washing cycle. In particular, the amount of biopolymers and humics is observed from the third washing.

As for the tendency of the organic substances accumulated on the surface of the positive osmosis membrane, it can be seen that the biopolymers remain most on the surface of the osmosis membrane. In general, biopolymers based on proteins or polysaccharides are known to be difficult to remove by physical washing due to the nature of sticky substances.

Of course, irreversible membrane contaminants, such as biopolymers, will degrade the performance of the positively osmotic membrane, which should be reflected in the positively charged osmosis membrane fouling index.

Although it is best to measure the concentration of the substance present in the raw water, this method has limitations in application to the field in situ and the measurement time is very long, which makes it difficult to cope with the instantaneous membrane contamination .

Therefore, by measuring the fouling reversibility of membrane osmosis membranes through physical washing in the same way as above, indirectly measuring the amount of irreversible membrane contaminants such as biopolymers present in the raw water And the membrane contamination index which can give the signal of pretreatment strength to the pretreatment process is considered as the most reasonable method.

In order to reflect membrane fouling reversibility in the development of the membrane fouling index of the forward osmosis membrane, it is essential to analyze the effect of the physical washing conditions on membrane fouling reversibility. FIG. 5I is a graph showing the results of the fouling reversibility of the membrane osmosis membrane according to the operating cycle according to the physical washing condition.

After the positive osmosis process is carried out at a flow rate of 8.54 cm / s for 70 hours, the physical washing of the positive osmosis membrane is carried out for 10 minutes. At this time, the flow rates of the physical cleaning are performed at operation cycles of 17.08 cm / s, 25.62 cm / s, 34.16 cm / s, and 42.70 cm / s.

Referring to FIG. 5I, when the forward osmosis membrane is washed to 25.62 cm / s or less, the fouling layer of the osmosis membrane is not sufficiently removed from the osmosis membrane, resulting in a low membrane fouling reversibility Able to know.

5f and 5i show that the membrane fouling reversibility of the membrane of the forward osmosis membrane converges in the fifth to sixth cycles as the operation is repeated. From this, it can be deduced that the state in which the cleansing osmosis membrane can no longer be recovered by physical washing can be set as a 'critical reversibility', and the contamination of the cleansing osmosis membrane can be predicted from membrane contamination reversibility.

The positive osmosis membrane contamination index (OFI) is an index of the membrane contamination of the positive osmosis membrane. It is determined whether the permeation amount of the influent water passing through the osmosis membrane exceeds the critical reversibility (Rc) Can be derived.

It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the spirit or scope of the inventions. It will be apparent to those of ordinary skill in the art.

100: Fixed osmosis membrane fouling prediction device
110: Inflow water supply unit 111: Influent storage tank
112: first influent water pipe 113: first pump
114: second influent water tube 120: induction solution supply part
121: induction solution storage tank 122: first induction solution tube
123: second pump 124; The second induction solution tube
125: TDS controller 130: membrane contamination simulating part
131: positive osmosis membrane 140: membrane fouling predicting unit

Claims (10)

A membrane contamination simulator having a positive osmosis membrane and simulating membrane contamination of the osmosis membrane during a normal osmosis process;
An inflow water supply unit connected to the membrane contamination simulating unit to provide a primary inflow water during the normal infiltration process and provide a secondary inflow water having a flow rate higher than the flow rate of the primary inflow water during the washing process;
An induction solution supply unit connected to the membrane contamination simulating unit to supply an induction solution having a concentration higher than that of the first influent water in the forward osmosis process; And
Wherein the water permeation amount of the first influent water passing through the osmosis membrane is measured according to the elapsed time of the operation of the forward osmosis membrane process to calculate the osmosis membrane membrane fouling index (OFI) A membrane contamination predicting unit for predicting membrane contamination of the positive osmosis membrane,
The induction solution supply part supplies the induction solution to the membrane contamination simulator while adjusting the molar concentration to accelerate the formation of the adhesion layer,
Wherein the membrane contamination simulator is configured to cause the water in the first influent water to flow into the space containing the induction solution through the positive osmosis membrane by osmotic pressure due to a difference in concentration between the first influent water and the induction solution during the forward osmosis process , And the membrane contamination of the positive osmosis membrane is simulated by an adhesive layer formed by accumulating the organic matter of the primary influent water on the surface of the positive osmosis membrane.
The method according to claim 1,
Wherein the film fouling predicting unit predicts,
A first water permeation amount (J1), which is a water permeation amount of the first influent water passing through the positive osmosis membrane at the initial stage of the normal osmosis process before the adhering layer is formed in the positive osmosis membrane,
The third water permeation amount (J3), which is the water permeation amount of the first influent water passing through the positive osmosis membrane in the forward osmosis process after the adhered layer of the positive osmosis membrane is removed by the washing process, is measured,
Wherein the normal osmosis membrane fouling index (OFI) is calculated by a recovery rate of the third water permeation amount (J3) with respect to the first water permeation amount (J1).
The apparatus according to claim 2,
The membrane contamination of the positive osmosis membrane is predicted when the ortho-osmosis membrane fouling index (OFI) is in a range (Rc <OFI <1) which is greater than the critical reversibility (Rc)
Wherein the critical reversibility (Rc) is a ratio of a water permeation amount of the first influent water before the washing process to a water influent amount of the first influent water after the washing process in a state where the membrane contamination of the positive osmosis membrane is not recoverable only by physical washing with the second influent water Permeation amount of the permeable membrane is predicted.
3. The method of claim 2,
Wherein the membrane permeation predicting unit predicts that the permeation amount of water of the first influent water passing through the positive osmosis membrane by the adhering layer formed on the surface of the normal osmosis membrane becomes gradually smaller than the first water permeation amount When the water permeation amount J2 is measured,
The inflow water supply unit supplies the second influent water to the membrane contamination simulator at the time when the second water permeation amount J2 is measured so that the positive osmosis membrane is washed by the second influent water to remove the adhesion layer Wherein the first and second sensors are configured to detect the concentration of the osmosis agent.
3. The method of claim 2,
A TDS controller is connected to the inductive solution supply unit,
The TDS controller controls the first water permeation amount due to the difference between the TDS of the first influent water and the TDS of the induction solution by controlling the total dissolved solids (TDS) of the induction solution provided to the membrane contamination simulator Wherein said means for predicting the concentration of the osmosis membrane comprises:
A method for predicting membrane fouling in a forward osmosis process using the apparatus for predicting a forward osmosis membrane foul of claim 1,
(A) the forward osmosis process is performed by the osmotic pressure due to the difference in concentration of the primary influent water supplied to the influent water supply portion supplied to the membrane contamination simulating portion of the forward osmosis membrane fouling predicting device and the concentration of the inductive solution in the induction solution supply portion, A step of simulating membrane contamination of the positive osmosis membrane by an adherent layer formed by accumulating organic matter on the surface of the positive osmosis membrane;
(B) providing a second influent water to the membrane contamination simulator at the influent water supply unit to clean the osmosis membrane by the second influent water; And
(C) The water permeation amount of the first influent water passing through the positive osmosis membrane is measured according to the elapsed operation time and the number of operation of the positive osmosis process, and the positive osmosis membrane fouling index (OFI) is calculated from the equation (1) , And predicting membrane fouling of the positive osmosis membrane from the positive osmosis membrane fouling index (OFI).

.......................... Equation (1)
Wherein J1 is a first water permeation amount which is the water permeation amount of the first influent water passing through the positive osmosis membrane at the beginning of the positive osmosis membrane before the adherent layer is formed in the positive osmosis membrane, Is the third water permeation amount which is the water permeation amount of the first influent water passing through the positive osmosis membrane in the forward osmosis process after the adhered layer of the adhesive layer is removed by the washing process.

7. The method of claim 6, wherein step (B)
According to the elapse of the driving time of the forward osmosis process,
The water permeation amount of the first influent water passing through the positive osmosis membrane is gradually decreased by the adhering layer from the first water permeation amount J1, and at the time when the second water permeation amount J2, J1> J2 converges, Wherein the cleaning of the positive osmosis membrane by the influent of water proceeds and the membrane fouling of the normal permeable membrane is recovered as the adherent layer is removed from the positive osmosis membrane.
The method of claim 6, wherein the step (C)
(C1) stopping the operation of the forward osmosis membrane process by predicting that the ortho-osmosis membrane fouling index (OFI) is calculated to be greater than 1 (1 <OFI);
(C2) a step of continuing the operation of the normal osmosis process by predicting that the normal osmosis membrane is not contaminated when the normal osmosis membrane fouling index (OFI) is calculated as 1 (OFI = 1);
(C3) Predict membrane fouling of the said osmosis membrane when the ortho-osmotic membrane fouling index (OFI) is greater than the critical reversibility (Rc) and less than 1 (Rc <OFI <1) Wherein the washing step of step (B) is continued; And
(C4) If the ortho-osmotic membrane fouling index (OFI) is less than the critical reversibility (Rc) (Rc > OFI), then the membrane of the pure osmosis membrane can not be recovered by physical washing with the second influent water The operation of the forward osmosis process is stopped, and a pretreatment process such as chemical cleaning is performed,
Wherein the critical reversibility (Rc) is determined by repeatedly performing the positive osmosis process and the washing process so that the membrane contamination of the positive osmosis membrane can not be recovered only by physical washing with the second influent water, Wherein the recovery rate of the water influx of the primary influent water after the washing step (after J _washing ) with respect to the water influx of the tea inflow water (before the J _washing ) is a recovery rate.
7. The method of claim 6, wherein in the step (A)
Wherein the inductive solution is supplied to the membrane contamination simulator with a controlled molar concentration to accelerate the formation of the adherent layer.
7. The method of claim 6, wherein in the step (A)
The inductive solution is controlled by the TDS controller to adjust the total dissolved solids (TDS) of the inductive solution provided to the membrane contamination simulator,
Wherein the first water permeation amount is regulated by a difference between a TDS of the primary influent water and a TDS of the induction solution.

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