KR100384658B1 - Spacer for guiding fluid - Google Patents

Abstract

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to a fluid guide spacer used in a technique for separating a liquid by force-driven flow through a semi-permeable membrane, and particularly relates to turbulence in the flow of fluid by forming long grooves in the spacer. The present invention relates to a fluid guide spacer capable of maximizing filtration efficiency by minimizing concentration polarization.

The present invention for achieving the above object comprises a spacer for supporting a membrane (membrane) in which the filtration proceeds, the filtration device in which waste water treatment, etc. by filtration, the spacer is formed on the surface so that turbulence occurs in the fluid A plurality of long grooves are formed, and a plurality of grooves are formed on the surface of the spacer to prevent concentration polarization and provide an effect of realizing optimal filtration efficiency.

Description

Spacer for guiding fluid

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to a fluid guide spacer used in a technique for separating a liquid by force-driven flow through a semi-permeable membrane, and particularly relates to turbulence in the flow of fluid by forming long grooves in the spacer. The present invention relates to a fluid guide spacer capable of maximizing filtration efficiency by minimizing concentration polarization.

Membrane separation refers to separation of a substance by using a semipermeable membrane that selectively permeates the substance, and the membrane used here is called a separation membrane. In general, filtration refers to the separation of two or more components from a fluid. The concept of membrane filters includes the separation of dissolved solids or mixed gases. .

Separation membranes are classified according to the separation method and the degree, and membranes that are mainly used for water treatment can be largely classified into the types shown in Table 1 below according to the pore size and operating method of the membrane.

Membrane type Operating pressure (kg / cm ² ) Pore size (㎛) Fractional Molecular Weight (MWCO) apply Micro filtration 0.1 ~ 2 0.1-100 200,000 or more Separation of suspended solids within the removal range Ultra filtration 1.5-10 0.005-0.5 More than 10,000 Separation of Colloidal Medium / Polymer Organics Nano filtration 10-20 0.001-0.01 More than 200 Separation of Medium and Low Molecular Organic Divalent Ions Reverse osmosis 20-120 Less than 0.001 Less than 200 Ionic material separation

The membranes used for membrane separation are of two types: asymmetric membranes manufactured in the early 60's and composite membranes commercialized in the 80's. The asymmetric membrane is composed of a material such as a membrane skin layer having a semi-permeable property and a porous support layer supporting the same, and the composite membrane is composed of a different material from the membrane layer and the porous support layer. In the case of asymmetric membranes, the thickness of the thin film layer is about 0.1 ~ 1㎛, but in the case of composite membranes, the thin film layer of 0.1㎛ or less can be cast on the porous support layer by applying ultra thin filming technology. You can choose. Therefore, the thinner the membrane, the more the permeation flux of the membrane can be increased, and the membrane material having excellent salt rejection rate can be selected. Therefore, the structure of the composite membrane can exhibit better performance than the asymmetric membrane. Due to this, there is an advantage that the condensation phenomenon of the film generated can be minimized. However, composite membranes are more expensive to manufacture than asymmetric membranes, and are more expensive to manufacture. Only membrane-type modules can be manufactured, whereas asymmetric membranes are hollow fiber type and hollow fiber type. Since both types of spiral winding modules can be manufactured, both structures are currently used depending on the water condition and process design method to be treated.

Separation technology using membranes has been widely studied and applied and practical in developed countries, ranging from simple laboratory scale to large scale industrial processes, depending on the social needs of high purity, high functional materials and global environmental protection. Since the membrane process does not require a phase change like a distillation process, which is a typical separation method, there is an advantage in that a considerable amount of energy can be saved when compared to a conventional energy saving process. In addition, because of its simple principle and fastening, the device occupies a small space, which reduces the cost of the installation. However, in the membrane separation process, a phenomenon in which filtrate accumulates on the surface of the membrane, that is, concentration polarization occurs inevitably. Since this phenomenon is the biggest cause of deterioration of the membrane fixing efficiency, minimizing the concentration polarization phenomenon is an important task for increasing the efficiency of the process.

Various methods can be considered to solve the concentration polarization phenomenon. One of them is the design of the module, which aims to remove the filtration material accumulated on the membrane surface by making a flow path inside the module. In other words, even if the same membrane is used for fixation, designing a module that can reduce membrane contamination can greatly increase membrane permeation performance.

1 and 2 are schematic diagrams showing states before and after concentration polarization occurs, showing a filtration process in which the membrane 1 is filtered from right to left. 1 shows a state of initial filtration, and FIG. 2 shows a state in which filtration proceeds to some extent. It can be seen from FIG. 1 that the concentration C _b of the bulk solution and the concentration C _w at the surface of the membrane increase constantly while being connected. That is, they are connected by a continuity curve. However, in the case of the filter cake and 2 to some extent in the stacked behind emerging concentration C _g in the gel layer (gel layer) to the surface of the film, while the concentration is kept at a fixed value appears with the concentration of C _b discontinuous connectivity of the bulk solution. That is, when the membrane separation process is performed, when the concentration of the solution shows a discontinuous connection with the concentration of the surface of the membrane 1, this is called concentration polarization phenomenon.

In addition, the material transfer around the film 1 has two directions, as shown in FIG. That is, the flux around the membrane 1 appears in two directions, the flow J _{T in} the flow direction of the fluid and the J _B in the opposite direction of the flow. From a hydrodynamic point of view, J _T corresponds to flux by convection and J _B corresponds to flux by diffusion. Considering the higher concentration nearer the surface of the film 1, it is easy to understand the diffusion phenomenon caused by the concentration difference.

In a typical membrane separation process, the solution moves in a direction perpendicular to the membrane surface. However, in the case of the cross flow C type, the solution flows in a direction parallel to the surface of the membrane 1. In this case, the concentration polarization phenomenon is different from the general case, which is shown in FIG. 4. As shown in FIG. 4, if the plate 2 and the membrane 1 in parallel form a closed system, the frictional force that the incoming solution receives until full development takes place increases. The reduced velocity solution has a reduced ability to dissolve the filtration material that accumulates on the membrane 1 surface. Therefore, the concentration polarization phenomenon (CP) that occurs on the surface of the film 1 occurs as if half of the parabola is cut off. Since the amount of fluid permeated in the region where concentration polarization occurs severely is small, the amount of fluid permeated decreases farther from the outlet.

Ultrafiltration has been industrially used for the separation and concentration of high molecular weight materials with the development of reverse osmosis. In the early stages, applications have been made in dairy food relations, but in recent years they have been applied to the separation of components in the manufacture of pure or ultrapure water for the pharmaceutical and semiconductor industries, and in the pharmaceutical industry. Various types of membranes and modules have also been diversified. In recent years, an inorganic material film coated with zirconia oxide on the surface of a ceramic film, porous glass, or graphite has also been considerably developed. There are four types of UF membranes: plate & frame, tubular, spiral, and hollow fiber. A unit fixed to have a constant membrane area in a cell having an inlet, an outlet of a stock solution, and an outlet of a filtrate is called a module, and there are four types of modules depending on the type of membrane. The features of each module were reviewed at various angles and are shown in comparison to Table 2.

Flat plate Plate type Spiral Hollow fiber type Volume per film area) Membrane area / module volume (m ² / l) small Small to Medium 0.08 0.43 0.52 Installation space medium Medium to large small small Module structure Slightly complicated Slightly complicated complication simple Hygiene Characteristics ○ △ × ○ Ease of Cleaning ○ ◎ △ × Pump capacity medium Large to medium small small Hold up amount medium Large to medium small Small to medium Replacement of membrane Membrane unit Module unit Module unit Module unit Euro Closure (Pollution) Dangerous Low risk Dangerously Dangerously

Conventional disc tube modules are designed with state-of-the-art technology for molecular separation, desalination, and water treatment, and operate efficiently and economically for industrial wastewater with high SDI (silt density index), landfill leachate, seawater and highly concentrated wastewater treatment. 5 to 7, a membrane cushion 12 is overlapped between the hydraulic discs 11, which are spacers, as shown in FIGS. 5 to 7, and fitted to a tension rod 13. The metal flange 14 is coupled to both ends to tightly tighten the separator 12 and the pressure plate, that is, the spacer 11. In addition, the pressure pipe vessel surrounds the outside, and this simple structure makes it possible to easily change the length and material of the disk tube module according to the intended use, and to facilitate the performance inspection and the replacement of the membrane 12. Since the raw water moves into the space and the rib-shaped hole of the short distance between the pressure plate 11 and the separator 12 surface, the flow is smooth and does not restrict the inflow of raw water. Therefore, the sediment accumulated in the separator 12 is automatically removed, so that the membrane contamination is much less than that of other membranes, and the raw water flow method can be operated without any problems through only mechanical filtration sand and fine filters. . Such disk tube modules are currently increasing recovery rates of more than 95% in high concentration systems. Reference numeral 15 denotes a housing.

In the above configuration, the flow of the fluid flows as shown in FIG. 6. First, the fluid introduced through the inlet port 14a moves through the hole 11b formed inside the spacer 11. Filtration is performed through the separator 12 sandwiched between the spacers 11 during the process. Accordingly, the filtered treated water is discharged through the treated water outlet 14b formed around the tension rod 13, and the concentrated water having been filtered is discharged to the outside through the concentrated water outlet 14c.

The spacer 11 of the disc tube module according to the prior art is described in Korean Patent No. 0751895, and has a circular shape as shown in FIG. 7, and has a hole 11a through which the tension rod 13 passes. Is formed, and the slot-shaped hole 11b for moving a fluid is formed in a radial arrangement. Therefore, as shown in FIG. 6, the fluid having passed through the slot-shaped hole 11b is moved to the separator 12 and the spacer 11 at the upper portion thereof, whereby filtration by the separator 12 is performed. In particular, since a plurality of protrusions 11c are formed on the surface of the spacer 11, turbulence is generated in the fluid to be moved, thereby increasing filtration efficiency and preventing concentration polarization. do.

In addition, in the case of the flat panel module among the UF modules according to the related art, the flat separators 21 are stacked at regular intervals as shown in FIG. 8, and fluid flows from one end. It is a structure that is leaked to the other end.

Reference numeral 22 denotes a rubber spacer, 23 denotes a drain pin 23 in which a hole through which the treated water filtered by the separator 21 passes.

However, in the case of the disc tube module of the prior art, when a spacer for supporting the separator is used to form a plurality of protrusions so that turbulence occurs on the surface of the spacer, there is a problem that the manufacturing cost is very expensive.

In addition, in the case of the flat panel module of the prior art, not only do not have a spacer in many cases, but turbulence is not properly generated even when the spacer is installed, there is a problem that the efficiency of the concentration is lowered due to the concentration polarization phenomenon occurs.

The present invention has been made to solve the above-mentioned problems of the prior art, and in selecting the model in the present invention, a module having a spacer inserted with a channel into an existing model was considered. The flow path present inside the spacer serves to remove the solute from the membrane surface by making the incoming fluid turbulent (turbulent flow).

Fractions by UF (ultrafiltration) are mostly defined by the membrane, and depending on the operating conditions the fractions may vary somewhat but are negligible. The economic feasibility is determined by the items shown in Table 3 to determine whether to hire.

Items that cost you Items recoverable Module replacement cost 2. Power cost 3. Film cleaning chemical cost 4. Labor cost 5. Equipment depreciation 6. Repair fee Valuables recovered by concentration 2. Items saved by the introduction of UF Energy cost facility installation space labor cost, etc.3. Yield increase due to improved reliability

The choice of modules is mainly based on economics. This does not mean that it is best to choose the least expensive form. Because the type of process is also very important. As shown in Table 1, each module has its own application. Most of the processing costs by the UF method are power costs and module replacement costs. Therefore, it is important to choose a module with high filtration capacity and how to maintain the filtration capacity. In this study, the module design is selected to replace the module and the design of the module to maintain the filtration capacity for a long time.

1 is a schematic diagram showing a state before filtration by a membrane occurs;

2 is a schematic view showing a state in which concentration polarization phenomenon occurs after filtration by a membrane occurs;

3 is a schematic diagram illustrating a concentration polarization phenomenon along a flow of a fluid;

4 is a schematic diagram illustrating a concentration polarization phenomenon exhibited by a cross flow;

5 is a cross-sectional view of a disk tube module according to the prior art,

Figure 6 is a detailed view showing the flow of fluid in the disk tube module according to the prior art,

7 is a front view of a circular spacer that is part of a disc tube module of the prior art,

8 is a schematic perspective view of a flat panel module according to the prior art,

9 is a schematic perspective view of a flat panel module according to the present invention;

10 is a side cross-sectional view of a flat panel module according to the present invention;

11 is a plan view of a fluid guide spacer according to the present invention;

12 is a front view of a fluid guide spacer according to the present invention;

13 is a plan view of various models for developing a spacer according to the present invention;

FIG. 14 is a partial schematic view of a model 4 of a model for developing a spacer according to the present invention, and FIG. 14B is a partial schematic view of a spacer mixed with models 3 and 4;

15 is a side view of a model for developing a spacer according to the present invention.

<Explanation of symbols on main parts of the drawings>

50 housing 51 separator

52: spacer 53: O-ring

The present invention includes a spacer for supporting a membrane through which filtration proceeds, and a filtration device in which wastewater treatment is performed by filtration, wherein the spacer has a plurality of long grooves formed on a surface thereof so that turbulence occurs in the fluid. It features.

In addition, the present invention is the groove of the spacer is formed long along the flow direction of the fluid, the width of the groove of the spacer is formed to be repeatedly increased or decreased at a constant angle, the constant angle to increase or decrease the width of the groove of the spacer is It is characterized by being 150 degrees.

Hereinafter, embodiments of the present invention will be described with reference to the accompanying drawings.

9 is a schematic perspective view of a flat plate module according to the present invention, FIG. 10 is a side view of a flat plate module according to the present invention, FIG. 11 is a plan view of a fluid guide spacer according to the present invention, and FIG. Is a front view of a fluid guide spacer according to the present invention.

As shown in FIGS. 9 to 12, the flat module having the spacer for guiding the fluid according to the present invention has a plurality of flat separators 51 stacked in the housing 50, and each of the flat modules has a stacking structure. 12 is a structure in which the flat spacer 52 as shown in FIG. 12 is provided.

Looking at the structure of the spacer 52 in detail, first two O-ring holes (52a) for the insertion of the O-ring (53) is formed, a plurality of grooves (52b) in the direction to match the flow of the fluid ) Are formed at regular intervals. The groove 52b is formed such that its width is repeatedly increased and decreased constantly, and the angle for increasing or decreasing the width of the groove 52b is set to 150 degrees. Referring to FIG. 12, which is a front view of the spacer 52, an o-ring 53 is fitted at the center of the spacer 52, and grooves 52b are spaced at regular intervals on both sides of the o-ring 53. It is a structure formed repeatedly.

In the structure of the spacer 52 as described above, as shown in FIGS. 9 to 10, the flow of fluid is similar to a conventional flat module, and raw water is introduced from the left side, and the introduced raw water is separated from the spacer 52 and the separator 51. The filter water is filtered through the separator 51 and discharged to the right outlet, and the treated water filtered by the separator 51 and introduced into the lower portion of the separator 51 is a hole of the spacer 52 in which the O-ring 53 is inserted. It is discharged to the outside through 52a.

The reason for selecting the structure as described above is as follows.

In the present invention, computer simulation was performed using a two-dimensional model and a three-dimensional model to develop a module that can effectively reduce the concentration polarization phenomenon generated in the membrane separation process. In the existing device, the design was carried out considering the module to install the spacer with the flow path. Each of the selected models carried out two-dimensional computational simulations, and based on the results, expanded the computational simulations to three dimensions. Basically, the module selection considerations were based on the velocity distribution near the membrane surface and the pressure distribution in the module. The reason is related to the rate distribution at the membrane surface and how much solute can be removed in the module. In each of the four cases, two-dimensional computer simulations were performed, and then, the optimal model was selected and three-dimensional computer simulations were made with one model. In the case of three-dimensional computer simulation, the optimal model was selected by considering the effect of the change of the number and height of the flow paths in the spacer. Computer simulations used in this study are based on the momentum conservation equations for turbulence. The momentum conservation equation is solved by the finite volume method, and as a result, the velocity distribution and the pressure distribution in the system can be known.

In order to proceed with the above research, first, the model was selected, second, two-dimensional computer simulation for each model, third, the area loss in the module was considered, and fourth, the selected model was Three-dimensional computer simulations were performed and finally the optimal model was selected.

In the above, the properties (density, viscosity) of the fluids used in the computer simulation performed for the model selection were kept constant, the superiority of the model was determined based on the velocity distribution, and the pressure distribution was also considered.

In particular, the velocity distribution was considered at a constant height, and the reference height was considered for the entire surface near the membrane surface. This is because the speed of the membrane surface is the greatest force to remove the filtration material from the surface. The operating conditions were based on atmospheric pressure and room temperature, and the effects of gravity were ignored.

And, the calculation of the experiment as described above is performed by a numerical method, the governing equation is finite difference by the finite volume method is calculated by a simple algorithm (simple algorithm). Finite-differential systems solve three-dimensional matrices for each time unit. This method is called Tri-Diagonal Matrix Algorithm (TDMA).

The governing equations are integrated using the interpolation function of the dependent variables between the grid points for the control volume surrounding each grid. This finite difference equation is a series of algebraic equations that connect the values of the dependent variables between each grid. The solution can be solved by successively solving the equations thus obtained. The process of finding the solution is as follows.

First, a new velocity field is obtained by sequentially calculating the momentum conservation equations representing the velocity in the x, y, and z directions (ignoring the z direction in two dimensions) based on the current pressure values. Second, solve the pressure equation with the new velocity field. Third, calculate a new pressure value. Fourth, the speed value in each direction is calculated using the speed equation. Fifth, the modified pressure is used as a new pressure value, and a series of processes are repeated until the range of error converges.

Since the flow field is to be calculated, the continuous equation and the momentum conservation equation are used as the governing equations. The equations used are shown in Equation 1, the continuity equation, and Equation 2, the momentum equation.

The boundary condition is constant for all computer simulations and the flow velocity of the incoming fluid is defined as 0.2m / s. In addition, the fluid used for computer simulation was selected to have a density of 1000kg / m ³ and a viscosity of 0.01kg / m · s in consideration of the properties of the fluid to be treated. In addition, the size of the system was selected in consideration of the existing membrane size. The contents mentioned so far are shown in Table 4 below, except that the height of the module is considered only in three-dimensional computer simulation, and F _i means the source term of the solute.

size Length: 20cm, Width: 10cm, Height: 0.3cm Inlet speed 0.2 m / s Property value ρ: 1000kg / m, μ: 0.01kg / m

Based on the boundary conditions and property values described above, two-dimensional computational simulation of the models 1,2,3,4 shown in FIG. 13 shows that the model 4 is the best as shown in Table 5 below. On the other hand, considering the pressure distribution, it can be seen that it is not a distribution that will have a big impact on the process.

Speed (m / s) Pressure loss (Pa) Model 1 0.216 34.8 Model 2 0.332 413 Model 3 0.210 984 Model 4 0.425 544

In addition, the two-dimensional computational simulation was extended to fix the height of the flow path to 0.3 cm, and the three-dimensional case was also considered. The results of computer simulation in three dimensions for the models 1,2,3,4 are shown in Table 6 below. The trends were similar to those of two-dimensional computational simulations, and model 4 is most appropriate given the velocity distribution. As shown in Table 6, it can be seen that the pressure distribution is not a variable that can affect the process in terms of its size.

Speed (m / s) Pressure loss (Pa) Model 1 0.301 748 Model 2 0.421 1050 Model 3 0.285 574 Model 4 0.535 1416

On the other hand, it can be seen that model 4 is the most appropriate model that can exist as a result of performing two-dimensional and three-dimensional computer simulation. However, a problem occurs when digging a flow path in the same shape as the model 4. As shown in Fig. 14A, the area in which the incoming fluid can be affected is lost much. As shown in FIG. 14A, when only the model 4 is used, an area lost is increased. In order to minimize this problem, as shown in FIG. 14B, the loss of the loss area is minimized by using the models 3 and 4 simultaneously. In Figs. 14A and 14B, reference numeral 60 denotes a groove and 61 denotes an area to be lost.

In addition, the speed distribution was examined by varying the number of flow paths for the mixed design of model 3 and model 4. The reference surface, that is, the surface showing the velocity distribution, is the surface at a distance of 0.02 cm from the separator. The setting of the reference plane corresponds to the plane that is very close to the act, and the results correspond to the values at the same point. As can be seen from Table 7 below, the velocity distribution appearing on the entire surface becomes faster as the number of flow paths increases. As the number of flow paths increases, the speed increases, and the pressure loss is expected to increase. However, it can be seen that there is no pressure loss that will greatly affect the operating conditions. Although the number of flow paths can be increased further, it is thought that it is difficult to actually cut off the flow path because the width of the flow path, that is, the width of the grooves, is less than 1 cm. If it is necessary to further cut the flow path as needed, the speed distribution is expected to improve as the flow path increases if the flow paths are cut at equal intervals. Since the difference in the pressure loss due to the change in the number of flow paths is not large, it can be seen that even if the number of flow paths is increased to some extent, no pressure loss affecting the process will occur.

Number of euros Speed (m / s) Pressure loss (Pa) Four 0.0519 440 5 0.0525 483 6 0.0742 520

On the other hand, the computer simulation results by changing the height of the flow path is shown in Table 8 below, the bar in Figure 15 means the total height corresponding to a fixed height (0.3cm). Thus, the velocity distribution and the pressure loss were simulated by varying the height of the flow path, that is, the length corresponding to L1 in FIG. 15 while the total height L was fixed. Velocity distribution and pressure loss were examined by changing the height change to 0.1cm, 0.15cm, 0.2cm, 0.21cm, 0.23cm, 0.25cm. In FIG. 15, reference numeral 70 denotes a spacer, 71 denotes a separator, and 70a denotes a groove.

First, when the height of the flow path is 0.1cm, 0.15cm, 0.2cm, it can be seen that the velocity distribution near the membrane increases relatively uniformly and rapidly as the height is increased. However, the speed increase increases above the height of 0.2cm, but it is not efficient considering the total area near the membrane. In terms of the velocity distribution, it can be seen that the optimum velocity distribution appears when the flow path height is 0.2cm, considering that the velocity distribution should be uniform and fast for the entire area near the membrane surface. When the height of the flow path is more than 0.2cm, as can be seen from Table 8, the maximum speed is found to be faster. This phenomenon occurs because when the flow path is above a certain height, it acts as an obstacle that does not mix well in the upper portion of the flow path, that is, the space between the membrane and the flow path. However, as mentioned above, it is more important than the slight increase in velocity that the velocity distribution is evenly distributed over the entire area. Pressure losses are also listed in Table 8 and also did not show significant losses that would affect the process. Therefore, as a result, it can be seen that the pressure loss does not act as a big factor in the fabrication of the flat membrane module.

Height of the flow path (cm) Velocity distribution (m / s) Pressure loss (Pa) 0.1 0.0712 1079 0.15 0.075 1120 0.2 0.081 1224 0.21 0.0762 & 0.09525 divided into two speed ranges 1165 0.23 0.076 & 0.095 divided into two speed ranges 1174 0.25 0.0753 & 0.0941 divided into two speed ranges 1233

As described above, in order to increase the efficiency of the membrane separation process, a shape in which a spacer is inserted into an existing module is considered. In order to remove the filtration material deposited on the surface of the membrane as much as possible, four flow paths were designed and the optimal module was selected as a result of computer simulation expanded in three dimensions. In the expansion of the two-dimensional model, the height of the existing membrane module was referred to, and the influence of the number and the height of the flow path existing inside the spacer at the predetermined overall height was examined. As the number of flow paths increases to a certain extent, it has a positive effect on the efficiency of the process. In the case of the height of the flow paths, it is necessary to find an optimal height at which the speed distribution can be performed quickly and evenly. The optimal design proposed by the present invention is a module having six flow paths in which a mixture of model 3 and model 4 is used, and the height of the flow path is 0.2 cm. In particular, when considering the increase in the number of flow paths, it is proposed to increase evenly. This is based on the fact that the flow paths must be arranged in pairs in order for the velocity distribution to appear evenly on all sides near the membrane. However, as the number of flow paths increases, the width of cutting paths decreases to less than 1 cm, so it is considered that technical aspects should be fully considered. An excessive increase in the number of flow paths can cause large pressure losses, which can be considered for other considerations. If the material is easy to process the material is selected, the thickness is enough to dig grooves to cause turbulence, there is no problem bent to the flow of the fluid to some extent. Some shaking may be more effective at inducing turbulence. The spacing can be adjusted by making the thickness of the O-ring between the plate and the flow path plate as thin as possible. In addition, it is considered that the packing density of the membrane is reduced by half when the flow path plates are installed between the plates, and the amount of filtrate is reduced by that. However, the packing density by narrowing the gap between the plates based on the simulation results Can reduce the decrease. However, by reducing the concentration polarization phenomenon, the effect may be offset to some extent. In order to represent such effects numerically, it is necessary to obtain them through long time experiments.

As a result, the shape of the proposed module requires O-rings to be mounted in the passage for the filtered water, even when considering the housing, so that sufficient space for mounting the O-rings in the center portion of the spacer is required. Therefore, the thickness of the spacer of the central part was designed thick.

For reference, the thickness of the spacer did not specifically specify its value. This is because the flow field inside the flow path is not significantly affected by the thickness of the spacer. It is considered advantageous to be as thin as possible at the limits that are not technically problematic.

As such, the spacer for guiding the fluid according to the present invention has a plurality of grooves formed on the surface thereof such that turbulence is formed in the flow of the flowing fluid, thereby preventing the concentration polarization phenomenon and implementing the optimum filtration efficiency. To provide.

The present invention is not limited to the above embodiments and can be variously modified and implemented by those skilled in the art without departing from the technical gist of the present invention.

Claims (8)

A filtration apparatus comprising a spacer for supporting a membrane through which filtration proceeds, and in which wastewater treatment is performed by filtration, The spacer is a fluid guide spacer, characterized in that a plurality of elongated grooves are formed on the surface so that turbulence occurs in the fluid. The method of claim 1, The groove of the spacer is a fluid guide spacer, characterized in that formed long along the flow direction. The method of claim 2, The groove of the spacer is a fluid guide spacer, characterized in that the width is formed to repeatedly increase and decrease at a predetermined angle. The method of claim 3, And a predetermined angle to increase or decrease the width of the groove of the spacer is 150 degrees. The method of claim 1, And the groove is formed to have a width greater than a gap between the grooves. The method of claim 1, And the groove is six in number. The method of claim 1, The groove is a fluid guide spacer, characterized in that the height is 0.2cm. The method of claim 1, The spacer is a fluid guide spacer, characterized in that the O-ring is inserted into the hole into which the treated water flows, the thickness of the vicinity of the O-ring is thicker than other places.