WO2016143920A1 - Separation membrane contactor module and membrane contact system and membrane contact method for purifying bio-gas using same - Google Patents

Abstract

The present invention relates to a separation membrane contactor module and a membrane contact system and method for purifying bio-gas using the same, in which: the separation membrane contactor module having a flow path control tube (240, 540) installed therein is provided to activate a cross flow, thereby enhancing gas separation efficiency, the flow path control tube (240, 540) having a partition (243, 543) therein; an absorption separation-membrane contactor module (200) and a degassing separation-membrane contactor module (400) are connected to each other such that liquid continuously circulates through the shell sides of the respective modules that communicate with each other; the separation of gas is performed at the tube side of the absorption separation-membrane contactor module (200), and the reduction of pressure is performed at the tube side of the degassing separation-membrane contactor module (500); and a degassing tank (300) is provided on the liquid circulation line to allow degassing to be performed through a change in solubility according to a pressure change, thereby refining high-purity methane from bio-gas.

Description

Membrane Contactor Module and Membrane Contact System and Membrane Contact Method for Biogas Purification

The present invention allows the membrane module for the membrane contactor, which is the core of the membrane contactor, to exhibit the maximum separation efficiency, and to separate methane gas from the biogas generated in the anaerobic digestion process of organic matter using the membrane contactor module and using the same. A membrane contact system for biogas purification and a membrane contact method.

Membrane technology is one of the separation technology using the material selective permeability of the polymer material. The use of separators in water treatment and sewage / wastewater treatment has increased dramatically since the beginning of the 1960s, and membranes are very useful for separating solids and liquids, liquids and liquids, gases and gases, and liquids and gases. As a device, except for a special case, it is possible to save energy because it does not involve a phase change, and because the process is simple, the device occupies little space. Membranes are widely used throughout the industry, including wastewater treatment, water treatment, including water production, concentration in the food and pharmaceutical sectors, separation of oxygen and nitrogen from the air and recovery of ammonia.

These membranes can be classified into various types according to their shape and separation performance. First, they are classified into flat membranes, tubular membranes, and hollow fiber membranes according to their types. Can be. As described above, the use of the separation membrane to separate the mixture by selectively passing a specific component has been widely used in various forms. Among them, the hollow fiber membrane is in the form of a hollow tube, which has a large surface area than other types of membranes, and thus yields a large yield.

On the other hand, the separation of gas mixture technology in the separation membrane technology includes a gas separation membrane process and a membrane contactor process. In a general gas separation membrane process, a non-porous selection layer is applied, and the gas mixture is separated by the difference in solubility and diffusion of each gas component among the gas separation polymer and gas mixture used in the selection layer. Therefore, in the general gas separation membrane process, the material transfer rate inside the membrane selection layer is the slowest, so that the material transfer speed in the membrane selection layer becomes the rate step of the entire process. In the membrane contactor process, a hydrophobic porous membrane is used to form a gas / liquid interface, and the gas mixture is separated by the difference in solubility of the liquid in each gas component at the gas / liquid interface. That is, the gaseous component having a high solubility dissolves quickly in the liquid, so that the gas mixture is separated while passing through the membrane contactor. Since the membrane contactor uses a hydrophobic porous membrane, the mass transfer rate in the gas side and the inside of the separator are very fast, and the rate in the liquid side is the slowest. Membrane contactor process is a technology that can separate the gas mixture very quickly and economically when an effective membrane contactor module is applied because the material transfer rate is about 1,000 times faster than the conventional gas separation membrane process.

In the membrane contactor process, increasing the material transfer rate on the liquid side determines the efficiency of the membrane contactor process. In the operation of the membrane contactor module, both the liquid supply to the shell side of the module and the tube side inside the hollow fiber (membrane) can be used. Increasing the mixing effect by using the method of high mixing effect on the liquid side to increase the material transfer speed on the liquid side will quickly lower the gas concentration on the liquid side at the gas / liquid interface, increasing the driving force of the components transferred from the gas side to the liquid side. Can be. Membrane contactor technology may be used to separate gas mixtures due to differences in solubility in liquids, but may also be applied to a degassing process that produces a pure liquid by applying a vacuum to the gas side to remove gaseous components dissolved in the liquid to the gas side. have.

Looking at the prior art regarding the membrane contactor module, "high efficiency gas / liquid membrane contact gas separation membrane module" (Korean Patent Publication No. 10-2010-0099530, Patent Document 1) as shown in Figure 1 hollow fiber (2) An example is shown in which the bundle is potted and fixed in a plastic or metal housing 1.

The hollow fiber interior space is called the tube side, and the space between the hollow fiber and the hollow fiber and the space between the hollow fiber and the housing is called the shell side.

The contactor module as shown in FIG. 1 has a counter current or a co-current flow from the tube side inlet 5 to the tube side outlet 6 and from the shell side inlet 3 to the shell side outlet 4. Can be driven. For example, when operated in countercurrent, the fluid flowing in the tube side and the shell side flows in opposite directions. When the mixed gas to dissolve the liquid to the tube side flows to the shell side, a gas / liquid interface is formed on the shell side surface, which is the outer wall of the hollow fiber, and the mixed gas components dissolve through this interface to cause gas separation. At this time, a boundary layer is formed at the liquid-side interface of the shell side of the gas / liquid interface, and since the material transfer rate is very slow at this boundary layer, the material transfer at the liquid side becomes a rate-limiting step of the material transfer of the membrane contactor module. The thicker the boundary layer is, the slower the material transfer rate is, which lowers the efficiency of the membrane contactor module. In order to solve this problem, it is possible to increase the flow rate of the liquid flowing to the shell side, but there is a physical limit in increasing this flow rate.

On the other hand, when anaerobic digestion of organic matters such as food waste, sewage sludge, livestock manure and slaughter waste is carried out with oxygen blocked, a gas called Anaerobic Digestion Gas (ADG) or Biogas is generated. do. Biogas is composed of trace components such as 45 to 70% methane, 30 to 55% carbon dioxide, hundreds to thousands of ppm hydrogen sulfide, and hundreds to thousands of ppm ammonia, water and siloxane. The methane contained in biogas is designated as the representative greenhouse gas with global warming index 21. Since its own energy amount is about 5,000 kcal / ㎥, the purification and recovery of methane from biogas prevents global warming, resource recycling, The goal of securing renewable energy can be achieved.

Biogas can be used as a source of city gas and automobile fuel through high-purity through direct combustion and combined heat and power (CHP), refining, and environmental and economical efficiency around biogas sources. Therefore, various applications are being developed. The most economical and energy-efficient technology among biogas resource recycling methods uses biogas as a fuel by purifying and purifying the biogas, which is 2 to 3 times more economical than CHP. Accordingly, the globalization of biogas resources has shifted from CHP to high purity fuel production. Highly purified methane gas (biomethane) can be mixed with existing city gas and used in gas ranges, gas boilers, etc., and can be used as fuel for CNG cars / LNG cars.

Conventional biogas purification methods include water scrubbing, chemical absorption, pressure swing adsorption (PSA), gas separation membrane, liquefied cryogenic, etc. There is this.

In this regard, "a method for separating high-purity methane gas from landfill gas and a methane gas purification apparatus" (Korean Patent Publication No. 10-1086798, Patent Document 2) describes such a conventional purification method. Specifically, US Patent No. 2009/0156875 discloses a mixture of gas-liquid mixed state in a natural gas and landfill gas mainly composed of methane enters a primary gas-liquid separator to separate methane, and then, using a carbon dioxide absorbent, high purity methane of 98% or more. A method of producing a gas is disclosed. In addition, Korean Patent No. 0951367 discloses a method in which methane gas having a low density and specific gravity is collected at the top of a purification tower by using a purification tower composed of activated carbon, a compression, and a water film layer as a methane purification method. In addition, Korean Patent No. 2009-0028696 relates to a method for purifying biomethane and discloses a purification method using a tower and a water supply / discharge tube, a gas supply / discharge tube, and an absorption tower. In addition, Korean Patent No. 2010-0110229 discloses a technique related to a biomethane purification method for purifying biomethane from biogas generated by anaerobic digestion of organic waste such as sewage sludge, livestock waste, landfill waste, and food waste. . However, the above-described biogas purification method has disadvantages for each technology. In the case of water absorption, large installations increase plant installation costs, incur high process operation costs, and chemical absorption can lead to environmental pollution due to the use of additional chemicals. Pressure swing adsorption requires the pretreatment of hydrogen sulfide, ammonia, etc. contained in biogas, and if the pretreatment is insufficient, the efficiency decreases rapidly. As the plant operation period becomes longer, the fine powder is generated due to the wear of the adsorbent. The operating pressure increases and the separation efficiency decreases as the fatigue of the adsorbent increases. Even in the case of the gas separation membrane method, pretreatment for hydrogen sulfide and ammonia, which may damage the separator, is necessary, and the selectivity to methane / carbon dioxide is rather low, resulting in low separation efficiency. As a result, the separation efficiency decreases over time. The liquefied low temperature separation method consumes a lot of energy to obtain the low temperature required for liquefaction, and if it does not meet specific conditions, the economic efficiency is not good, and it becomes an obstacle to commercialization.

* Prior art literature *

(Patent Document 1) KR10-2010-0099530 (2010.09.13)

(Patent Document 2) KR 10-1086798 (2011.11.18)

The membrane contactor module of the present invention, and the membrane contact system and membrane contact method for purification of biogas using the same are to solve the problems occurring in the prior art, and by changing the internal structure of the hollow fiber membrane module for membrane contactors, The change in the flow of liquid in the shellside effectively improves the performance of the membrane contactor, thereby allowing high purity purification of methane.

Specifically, the cross-flow which cannot occur at the shell side of the conventional hollow fiber membrane contactor module is generated at the membrane module shell side, thereby reducing the boundary layer thickness to maximize the mixing effect, thereby purifying methane of high purity. I want to be able to.

The membrane contactor module of the present invention for solving the above problems, the module housing 10 made of a hollow hollow shape; The hollow fiber 20 having a shell side 11 formed inside the module housing and spaced apart from the inner wall surface of the module housing 10 along a longitudinal direction, and having a tube side 21 formed in the longitudinal direction therein. Wow; It is provided at both ends of the module housing 10, the tube side inlet 31 is formed on one side, the tube side outlet 32 is formed on the other side, the inner space 33 is the tube side 21 Two caps 30 having a partition 34 formed therein so as to be in communication with the shell side 11; A middle part is installed to penetrate the two caps 30 and is located inside the module housing 10. A shell side inlet 41 is formed at one end and a shell side outlet 42 at the other end. The inside is formed in the form of a hollow tube, the partition 43 is installed inside the middle portion, and the plurality of holes 44 are formed on both outer peripheral surfaces based on the partition 43, the shell side inlet ( 41, the liquid moves from the side hole 44 to the shell side 11, and the liquid on the side of the shell side 11 flows into the shell side outlet port 44 through the shell side outlet 42 side hole 44. It is configured to include; flow path control tube 40 configured to move to 42.

In this configuration, a plurality of blocking walls 51 are formed inside the longitudinal direction to form a plurality of unit installation spaces 52 divided by the blocking walls 51 to form the module housing 10 and the hollow fiber. 20, the cap 30 and the flow path control tube 40 is inserted into the unit installation space 52 to form a unit 60, respectively, the wall connection to connect each unit installation space 52 A passage 53 is formed, and the connection passage 53 is configured to connect the inner space 33 of the cap 30 of the adjacent unit 60 to each other, and the flow path control tube 40 of the adjacent unit 60 is It is characterized in that the inner case 50 is further provided to communicate with each other inside.

The hole 44 is characterized in that the diameter is made of a size of 0.5 ~ 50mm.

The hole 44 is in a straight line with the axial direction of the flow path control tube 40, it characterized in that the single slot shape formed along the axial direction in a spiral.

The hole 44 is characterized in that a plurality of holes are formed in equally divided positions on the outer circumferential surface based on the cross section of the flow path control tube (40).

At this time, the hole 44 is characterized in that formed in a spiral along the outer peripheral surface of the flow path control tube (40).

In addition, a plurality of the holes 44 are formed at regular intervals along the length direction of the flow path control tube 40, but the holes 44 at the tip adjacent to the partition 43 are partition 43 from the partition 34. It is characterized by being located at 3/5 ~ 4/5 of the distance between.

In addition, the inner diameter / length of the module housing 10 is characterized in that 1/2 ~ 1/20.

The biogas refining membrane contact system of the present invention comprises: a gas compressor (100) for pressurizing a biogas including a gas having a property of dissolving in a liquid to a pressure greater than normal pressure; A module housing 210 having an empty hollow shape and an inside of the module housing are installed to be spaced apart from the inner wall surface of the module housing 210 along a length direction to form a shell side 211 to the outside, and a length inside the module housing 210. The hollow fiber membrane 220 and the tube housing 221 in which the tube side 221 is formed, respectively, are installed at both ends of the module housing 210, and the tube side inlet through which the biogas compressed by the gas compressor 100 flows on one side. 231 is formed, a tube side discharge port 232 through which the biogas in contact with the other side is discharged is formed, and the inner space 233 is in communication with the tube side 221 and the shell side 211 Two caps 230 having the partition wall 234 formed to be blocked, and the middle portion penetrates the two caps 230 and are installed to be positioned inside the module housing 210, and at one end thereof from the outside. Liquid flows in Shell side inlet 241 is formed, the shell side discharge port 242 is formed inside the empty tube form is formed, the liquid flowing in the other end is discharged, the partition 243 is provided inside the middle portion In addition, a plurality of holes 244 are formed at both outer peripheral surfaces of the partition 243, so that the liquid moves from the hole 244 at the shellside inlet 241 to the shellside 211, and the shellside outlet 242. Absorption membrane contactor module 200 composed of a flow path control tube 240 is configured to move to the shell side outlet 242 while the liquid on the side of the shell side 211 through the hole (244) side; A degassing tank 300 for storing the liquid discharged from the shell side outlet 242 of the absorption separator contactor module 200 at atmospheric pressure or in a vacuum state; One side is connected to the upper side of the degassing tank 300, the other side is connected to the gas compressor 100, a blower 410 is installed in the middle of the pipeline to the gas in the injured state of the gas compressor 100 Gas discharge pipe 400 for supplying with; A module housing 510 having an empty hollow shape and a module housing 510 spaced apart from an inner wall surface of the module housing 510 in a longitudinal direction inside the module housing are formed to form a shell side 511 to the outside and have a length therein. The hollow fiber membrane 520 in which the tube side 521 is formed, and the module housing 510 at both ends, respectively, and an inner space 533 communicates with the tube side 521 and the shell side 511. The barrier ribs 534 are formed to be blocked from each other, and the tube side discharge ports 531 connected to the vacuum pump 550 are formed on both sides thereof, and the air inside the tube side 521 is discharged to the outside by the vacuum pump 550. And two caps 530 configured to form a vacuum in the tube side 521, and an intermediate portion is installed inside the module housing 510 while penetrating the two caps 530. In the degassing tank 300 and piping A shell-side inlet 541 is formed to be connected to the liquid stored in the degassing tank 300, and a shell-side outlet 542 is formed in which the liquid introduced into the other end is discharged. The partition 543 is provided inside the middle portion, and a plurality of holes 544 are formed on both outer peripheral surfaces of the partition 543 so that the liquid from the hole 44 at the side of the shellside inlet 541 is formed. Flows to the shell side 511 and moves to the shell side outlet 542 while the liquid on the side of the shell side 511 flows into the shell side through the hole 544 of the shell side outlet 542. A degassing membrane contactor module 500 consisting of 540; One side is connected to the shell side outlet 542, the other side is connected to the shell side inlet 241 of the absorption separator contactor module 200, and a pressure pump 610 is installed at one side of the pipeline to provide a deaeration separator contactor. And a liquid circulation tube 600 configured to supply the liquid passing through the module 500 to the absorption separator contactor module 200 in a pressurized state.

The biogas refining membrane contact method of the present invention comprises the steps of: compressing a biogas containing a gas having a property of dissolving in a liquid by using the system to a pressure higher than normal pressure using the gas compressor (100); The biogas pressurized by the gas compressor 100 is supplied to the tube side inlet 231 of the absorption separator contactor module 200 to make membrane contact with one side of the hollow fiber membrane 220, and the pressure pump 610 is used. Supplying the liquid to the shellside inlet 241 at a higher pressure than the biogas pressurized by the tubeside inlet 231 of the absorption separator contactor module 200 to make the membrane contact with the other side of the hollow fiber membrane 220; The liquid discharged to the shell side outlet 242 after the membrane contact with the hollow fiber membrane 220 is supplied to the degassing tank 300 maintained at atmospheric pressure or vacuum to be dissolved in the liquid and the liquid in the degassing tank 300. Firstly degassing the gas until dissolution equilibrium occurs; Supplying a gas degassed in the degassing tank (300) to the gas compressor (100) through the gas discharge pipe (400); The first degassed liquid from the degassing tank 300 is supplied to the shell side inlet 541 of the degassing membrane contactor module 500 to make membrane contact with one side of the hollow fiber membrane 520, and degassed with the vacuum pump 550. Applying a vacuum to the tube side 521 of the membrane contactor module 500 to perform secondary degassing; Shell side of the absorption separator contactor module 200 through the liquid circulation tube 600 while pressurizing the liquid discharged to the shell side outlet 542 of the degassing membrane contactor module 500 with the pressure pump 610. It is configured to include; supplying to the absorption separator contactor module 200 through the inlet 241.

In this configuration, the pressure applied to the liquid through the pressure pump 610 is characterized in that it is maintained 0.3 bar-0.7 bar higher than the pressure applied to the biogas.

In addition, the ratio of the gas flow rate compressed through the gas compressor 100 to the absorption separator contactor module 200 and the flow rate of the liquid supplied to the absorption separator contactor module 200 through the pressure pump 610 is 0.01 to 10. It is characterized by maintaining as.

In addition, the biogas is a mixed gas generated during the anaerobic digestion of organic substances, characterized in that any one of methane, carbon dioxide, toil sulfide, ammonia is included.

In addition, the degassing tank 300 during the first degassing is characterized in that the internal temperature is maintained at 5 ~ 50 ℃.

According to the present invention, the separation efficiency can be further improved as compared with the conventional contactor module using the hollow fiber membrane of the same quantity and length.

More specifically, cross flow does not occur in the shell side of a general contactor module, so it is difficult to expect a mixing effect, and the separation efficiency according to the boundary layer is formed, whereas the contactor module according to the present invention crosses the shell side. Induces a large flow, resulting in a large mixing effect, thereby reducing the thickness of the shell layer boundary layer to maximize the performance of the module.

This eliminates the need for a separate pretreatment process to remove hydrogen sulfide, ammonia, etc., which are necessary in the pressure swing adsorption and gas separation membrane processes. Compared with the existing absorption method, it is increased 2-3 times, so that the same amount of biogas can be purified even with a small device size.

In addition, since water is used as the absorbent liquid, there is less concern about environmental pollution.

In addition, the biogas is compressed to a pressure higher than the normal pressure to make the membrane contact with one side of the hollow fiber membrane, and at the same time, the bulk flow of the mixed gas flows into the water by the pressure. When a pressure with a differential pressure that can block) is applied, the partial pressure acting on the water-soluble gas increases in proportion to the pressure acting on the biogas without generating bubbles due to biogas in the water. The amount of dissolved gas is increased in proportion to the increase in pressure of the biogas.

In addition, according to the present invention, methane can be separated from biogas at high efficiency and low energy cost compared to the processes using the conventional absorption method, pressure conversion adsorption method, and gas separation membrane method, thereby suppressing greenhouse gas emissions and using methane as fuel. The effect is great.

1 is a schematic view showing an example of a hollow fiber membrane module for a conventional membrane contactor.

Figure 2 is a partially cut perspective view showing an embodiment of the membrane contactor module of the present invention.

Figure 3 is a partially cut perspective view showing an enlarged one end side in Figure 2;

Figure 4 is a partially cut perspective view showing the other end side in an enlarged view in FIG.

Figure 5 is a schematic cross-sectional view showing a form in which the outer casing is further configured in a multi-stage connected in the present invention.

Figure 6 is a plan view showing an embodiment of the flow path control tube in the present invention.

Figure 7 is a plan view showing another embodiment of the flow path control tube in the present invention.

8 is a schematic view showing a membrane contact system for purifying biogas of the present invention.

* Detailed description of the major symbols in the drawings *

10, 210, 510: module housing

11, 211, 511: shellside

20, 220, 520: hollow fiber membrane

21, 221, 521 tube side

30, 230, 530: cap

31, 231: tube side inlet

32, 232, 531: tube side outlet

33, 233, 533: interior space

34, 234, 534: bulkhead

40, 240, 540: Euro control tube

41, 241, 541: shell side inlet

42, 242, 542: shell side outlet

43, 243, 543: dividers

44, 244, 544: hall

50: outer case

51: blocking wall

52: unit installation space

53: connecting passage

60: unit

100: gas compressor

200: Absorption membrane contactor module

300: degassing tank

400: gas discharge pipe

410 blower

500: deaeration membrane contactor module

550: vacuum pump

600: liquid circulation tube

610: pressure pump

Hereinafter, the separator contactor module of the present invention will be described in detail with reference to the accompanying drawings.

The membrane contactor module of the present invention is largely composed of a module housing 10, a hollow fiber membrane 20, a cap 30, and a flow path control tube 40.

The module housing 10 has a hollow shape as shown in FIG. 2.

The material of the module housing 10 may be a plastic material such as PVC, CPVC, PC, acrylic, ABS, PET, PP, PE, and metal materials such as aluminum and stainless steel, but is not limited thereto.

In addition, both ends of the module housing 10 may be formed with a thread or a flange to be connected to the cap 30.

The module housing 10 preferably has an inner diameter / length of 1/2 to 1/220.

When the ratio of the inner diameter length is smaller than the minimum ratio described above, it is unsuitable for separation through the serial arrangement as shown in FIG. 5, and the space utilization is not well achieved. This is formed and smooth separation is not achieved in this part.

As is well known, the hollow fiber membrane 20 is formed with a tube side 21 hollow in the longitudinal direction therein, and is installed along the longitudinal direction inside the module housing 10 described above.

At this time, the hollow fiber membrane 20 is installed to be spaced apart from the inner wall surface of the module housing 10 to form a shell side (11).

In addition, the plurality of hollow fiber membranes 20 are installed in the module housing 10 so as to be spaced apart from each other, thereby forming a shellside 11 which is a space.

Cap 30 is composed of two as shown in Figures 1 to 3 are respectively installed at both ends of the module housing (10).

One of these two caps 30 has a tube side inlet 31 through which gas is introduced, and a tube side outlet 32 through which gas is introduced is formed at the cap 30 on the other side. It is.

In addition, the partition 30 is formed between the cap 30 and the inner space of the module housing 10 to separate the space, but the hollow fiber membrane 20 is connected to the partition 34 so that the inner space of the cap 30 ( 33 is in communication with the tube side 21 which is an internal space of the hollow fiber membrane 20 and is blocked from the shell side 11.

The flow path control tube 40 is a main component in the present invention, and is installed such that an intermediate portion is located inside the module housing 10 while passing through the two caps 30.

In addition, a shellside inlet 41 through which liquid is introduced is formed at one end, and a shellside outlet 42 through which the introduced liquid is discharged is formed at the other end.

The flow control tube 40 is made of a hollow tube shape, the partition 43 is installed inside the middle portion.

This prevents the liquid introduced into the shellside inlet 41 from being discharged to the shellside outlet 42 by direct action.

In addition, a plurality of holes 44 are formed on both outer circumferential surfaces of the partition 43 on the basis of the partition 43, so that the liquid moves from the hole 44 at the shell side inlet 41 to the shell side 11, and the shell side outlet 42 The liquid on the side of the shell side 11 is moved to the shell side outlet 42 while flowing into the shell side 11 through the hole 44.

At this time, the size of the hole 44 is preferably made of 0.5 ~ 50mm in diameter.

If the diameter is less than 0.5mm, the smooth movement of the liquid particles passing through the hole 44 may be difficult to move the liquid through the hole 44, if it exceeds 50mm, the liquid evenly moves through the hole 44 Since a lot of pressure is required below, the separator contactor separation efficiency may be reduced.

In addition, the holes 44 may be arranged in various ways. As shown in FIG. 6, the holes 44 may be aligned with the axial direction of the flow path control tube 40 or spirally along the axial direction of the flow path control tube 40. Can be formed.

In addition, the holes 44 may be formed to be spaced apart from each other along the axial direction of each of the flow path control tube 40 with the above-mentioned diameter, but may be formed in a single slot shape with the above-described diameter or width. .

In addition, as shown in FIG. 7, a plurality of holes 44 are formed at equally divided positions on the outer circumferential surface of the flow control tube 40 based on the cross-section of the passage control tube 40 to be evenly distributed to maintain the separation efficiency.

In particular, in Figure 7, the hole 44 is formed spirally along the outer circumferential surface of the flow path control tube 40 to be discharged or introduced through the hole 44 formed at different angles on the movement path of the liquid to increase the separation efficiency have.

In addition, a plurality of the holes 44 are formed at regular intervals along the length direction of the flow path control tube 40, but the holes 44 at the tip adjacent to the partition 43 are partitioned from the partition 34. It is good to be located 3/5 to 4/5 of the distance between them.

If it is too close to the partition 43 outside the above range when the liquid is introduced and discharged in the adjacent state in the partition 43, the separation efficiency may decrease, on the contrary, if too far from the partition 43 and the partition 43 and In the spaces of the adjacent portions, the separation is not performed smoothly and the boundary layer thickness is thickened, which may reduce the separation efficiency.

As shown in FIG. 5 in the above configuration, the separator contactor module of the present invention may further include an outer case 50.

In detail, the outer case 50 has a plurality of blocking walls 51 formed therein along the longitudinal direction, and a plurality of unit installation spaces 52 divided by the blocking walls 51 are formed.

In addition, the unit housing 10, the hollow fiber membrane 20, the cap 30 and the flow path control tube 40 is formed of one unit 60, each unit 60 in the unit installation space 52 It can be configured to be inserted.

In this case, a connection passage 53 connecting each unit installation space 52 is formed on the wall surface of the outer case 50, and the connection passage 53 is an inner space 33 of the cap 30 of the adjacent unit 60. ) May be connected to each other.

At this time, the units 60 continuously installed in the outer case 50 are installed so that the flow path control tubes 40 of the adjacent unit 60 communicate with each other.

In addition, an insulation may be installed between the outer case 50 and each unit 60.

In such a configuration, the movement of the liquid and the gas may be utilized to be opposite to each other, that is, the liquid moves to the tube side, and the gas moves to the shell side. It is good to move the liquid to the shellside.

Experimental Example 1 Measurement of Nitrogen Concentration

After the manufacture of the membrane contactor module of the first embodiment and the second embodiment having the same structure as shown in Figure 2 and the shape of Figure 6, 7, the shape of Figure 6, 7,

A mixed gas of nitrogen / carbon dioxide (50 vol.% / 50 vol.%) Is supplied at 360 sccm (5.5 bar) to the tube side inlet 31, and 2.5 L / min (6.0 bar) of tap water is supplied to the shell side inlet 41. ) And the degree of dissolution of carbon dioxide in the mixed gas was measured.

In the flow path control tube 40 of FIG. 6, a hole having a diameter of 2 mm is disposed in four parts of the outer circumferential surface of the flow path control tube 40, and spaced apart from each other along the longitudinal direction, but disposed parallel to the axis.

The flow path control tube 40 of FIG. 7 is also manufactured by dividing a hole having a diameter of 2 mm into four equal parts of the outer circumferential surface of the flow path control tube 40, spaced apart from each other along the longitudinal direction, and arranged spirally along the axis.

Since the solubility of carbon dioxide is about 100 times larger than that of nitrogen, more carbon dioxide is dissolved inside the module, and when passed through the module, nitrogen is concentrated and discharged to the shellside outlet 42 by using nitrogen to obtain a high concentration of nitrogen. The concentration of nitrogen was measured and compared.

In addition, in Comparative Example 1, the same mixed gas and tap water were supplied to the conventional module as shown in FIG.

Table 1

Module type	Comparative Example 1	Example 1	Example 2
Euro control tube	none	Figure 6 Shape	Fig. 7 Shape
Shell Side Outlet Nitrogen Concentration (%)	95.3%	98.0%	98.6%

As shown in Table 1, when the module having the same size and the number of hollow fiber membranes is used as a reference, in the case of Examples 1 and 2, the module housing is installed by installing the flow path control tube 40 in which the partition 43 and the hole 44 are formed. (10) As the cross flow is formed in the shell side inside, the mixing effect is further increased, and it can be seen that the final nitrogen concentration is superior to that of Comparative Example 1.

In addition, the difference in the experimental value in the above experimental results is that the nitrogen concentration after passing through the existing module is 95.3%, the data of the high state is already increased to close to 100%, and purely flow control without means such as a separate chemical treatment Achieved through the installation of the tube 40 will be referred to as a high level of effect.

The membrane contactor module of the present invention described above combines the advantages of the water absorption method and the membrane technology, and does not require a separate pretreatment process to remove hydrogen sulfide, ammonia, etc., which are necessary in the pressure swing adsorption method and the gas separation membrane method. By using the polymer membrane in a modular manner, the gas / liquid contact area per unit volume is increased by 2 to 3 times compared to the conventional absorption method using the filler in the absorption tower, so that the same amount of biogas can be purified with a small device size. In addition, there is an advantage that environmental pollution does not occur because water or a small amount of physical absorbent (physical absorbent) is used as the absorbent liquid.

Thus, the membrane contact system and membrane contact method for biogas purification of the present invention are configured to purify biogas using the difference in solubility of each gas component in water of the membrane contactor module described above.

The solubility of water-soluble gases such as carbon dioxide, hydrogen sulfide, and ammonia in water is about 50 to 1000 times higher than that of methane. Using this property, the biogas containing the water-soluble gas (carbon dioxide, hydrogen sulfide, ammonia, etc.) is contacted with water through the pores of the hydrophobic porous polymer membrane to separate the water-soluble gas.

Hydrophobic porous hollow fiber membranes, such as hydrophobic porous polypropylene (PP) hollow fiber membranes, when one side of the membrane is in contact with water and the other side is in contact with a biogas containing water-soluble gas, the access of water through the pores is blocked, but through the pores Water soluble gas is allowed in and out, so that the water soluble gas passing through the pores is dissolved in water. Using this principle, a high purity of methane can be obtained by separating a water-soluble gas from a mixed gas containing a water-soluble gas by a porous hydrophobic hollow fiber membrane.

In addition, in the present invention, the biogas containing the water-soluble gas is compressed to a pressure higher than the normal pressure to make the membrane contact with one side of the hollow fiber membrane, and at the same time, the water is pressurized by a predetermined pressure higher than the pressure of the compressed gas mixture. The membrane is brought into contact with the other side to increase the amount of water-soluble gas dissolved in water and to prevent bubbles from occurring at the same time.

In addition, the water in contact with the hollow fiber membrane is discharged to the degassing tank maintained at atmospheric pressure or reduced pressure to degas the water-soluble gas until the equilibrium of dissolution of water and water-soluble gas.

In addition, the water discharged to the degassing tank is passed through one side of the other hollow fiber membrane while maintaining the state below the atmospheric pressure on the other side of the other hollow fiber membrane to degas the water-soluble gas.

Hereinafter, the membrane contact system and membrane contact method for purifying biogas of the present invention will be described in detail with reference to the accompanying drawings.

In the present invention, "biogas" is used as a generic term for a mixed gas mainly composed of methane and carbon dioxide generated during the anaerobic digestion of organic substances. In addition, “%” means “volume percentage” unless otherwise defined.

The inner space of the hollow fiber membrane is called a tube side, and the space between the hollow fiber membrane and the hollow fiber membrane, which is an outer space of the hollow fiber membrane, and the space between the hollow fiber membrane and the housing are called shell sides.

In the present invention, the gas having a property of dissolving in the liquid may be made of various liquid soluble gases, but most preferably made of a water-soluble gas, and the liquid described in the present invention is preferably made of water.

Biogas purification membrane contact system of the present invention is largely a gas compressor 100, absorption separator contactor module 200, degassing tank 300, gas discharge pipe 400, deaeration membrane contactor module 500, liquid circulation tube ( 600).

In the above configuration, the absorption separator contactor module 200 and the deaeration separator contactor module 500 each include a tube side and a shell side as main components in the present invention, and both components pass through the liquid to the shell side, The biogas to be treated passes through the tube side of the absorption separator contactor module 200, and the tube side of the deaeration membrane contactor module 500 is filled with air, or decompressed or vacuumed by a vacuum pump. consist of.

Referring to the overall configuration of the membrane contact system for biogas purification of the present invention will be described.

The gas compressor 100 is configured to receive a biogas including a gas having a property of dissolving in a liquid from the outside and pressurize it to a pressure greater than normal pressure.

The absorption separator contactor module 200 receives the pressurized biogas from the gas compressor 100 and passes the tube side 221 inside the hollow fiber membrane 220 to perform membrane contact treatment.

At this time, the liquid passes through the shell side 211 outside the hollow fiber membrane 220 while circulating.

The degassing tank 300 receives the liquid that has passed through the shell side 211 of the absorption separator contactor module 200, and decompresses the liquid to atmospheric pressure or vacuum to store the liquid therein.

That is, the degassing tank 300 is degassed until the liquid equilibrium is achieved between the liquid in contact with the hollow fiber membrane 220 and the gas dissolved in the liquid because the interior is made of atmospheric pressure to vacuum.

When the pressure applied to the biogas and the liquid in the degassing tank 300 is lowered, the solubility of the gas in the liquid is lowered, and the gas dissolved in the liquid is separated by the difference.

At this time, a spray nozzle is installed in the degassing tank 300 for smooth degassing so that the introduced liquid is sprayed and stored through the spray nozzle so that smooth degassing of the gas is achieved.

In addition, the degassing tank 300 is preferably a known temperature control device for maintaining the temperature inside.

This may cause a problem that the liquid freezes when the internal temperature of the degassing tank 300 is too low, and if it is too high, the gas solubility is increased so that smooth degassing is not performed.

The suitable temperature inside the degassing tank 300 through the temperature control unit is preferably about 5 ~ 50 ℃.

Gas discharge pipe 400 is one side is connected to the upper degassing tank 300, the other side is connected to the gas compressor 100, a blower 410 is installed in the middle of the pipeline in the degassing tank 300 The degassed gas, that is, the gas in a non-hazardous state, is supplied to the gas compressor 100 and then compressed again to be supplied to the absorption separator contactor module 200.

Degassing membrane contactor module 500 is made of the same structure as the absorber membrane contactor module 200 is made to pass the liquid to the shell side 511, the tube side 521 is connected to the external vacuum pump 550 to reduce the pressure This is to be done.

When such a reduced pressure is achieved, the water-soluble gas can be more completely degassed by maintaining the state below the normal pressure.

In addition, the liquid circulation tube 600 is connected to the shell side outlet 542 of the deaeration membrane contactor module 500, and the other side is connected to the shell side inlet 241 of the absorption membrane contactor module 200. A pressure pump 610 is installed at one side of the pipeline to supply the absorbent membrane contactor module 200 to pressurize the liquid passing through the deaeration membrane contactor module 500 so that continuous circulation is achieved.

The absorption separator contactor module 200 and the deaeration separator contactor module 500 have the same structure as the separator contactor module described above.

The structure of the two contactor modules 200 and 500 will be described in more detail as follows.

The absorption separator contactor module 200 includes a module housing 210, a hollow fiber membrane 220, a cap 230, and a flow path control tube 240. The deaeration membrane contactor module 500 also includes a module housing 510. , Hollow fiber membrane 220, cap 530, flow control tube 540 is configured to include.

The module housings 210 and 510 have a hollow shape as shown in FIG. 2.

The material of the module housings 210 and 510 may be plastic materials such as PVC, CPVC, PC, acrylic, ABS, PET, PP, PE, and metal materials such as aluminum and stainless steel, but is not limited thereto.

In addition, both ends of the module housings 210 and 510 may be formed with threads or flanges to be connected to the caps 230 and 530.

The module housings 210 and 510 preferably have an inner diameter / length of 1/2 to 1/220.

If the ratio of the inner diameter length is smaller than the above-described minimum ratio, it is not suitable for separation through the serial arrangement as shown in FIG. 5, and space utilization is not well achieved. A separate section is formed, where no smooth separation occurs.

As is well known, the hollow fiber membranes 220 and 520 are formed in the tube housings 211 and 511 which are hollow in the longitudinal direction. The hollow fiber membranes 220 and 520 are provided in the module housings 210 and 510 in the longitudinal direction. .

In particular, the hollow fiber membranes 220 and 520 of the present invention are preferably made of a hydrophobic porous hollow fiber membrane molded of a polymer such as polypropylene (PP).

At this time, the hollow fiber membrane (220, 520) is installed to be spaced apart from the inner wall surface of the module housing (210, 510) to form the shell side (211, 511).

In addition, the plurality of hollow fiber membranes 220 and 520 are installed in the module housings 210 and 510 to be spaced apart from each other, thereby forming the shellsides 211 and 511 which are spaces apart from each other.

Caps 230 and 530 are configured in two, as shown in Figures 2 to 4 are installed on both ends of the module housing (210, 510), respectively.

One of the two caps 230 of the absorption separator contactor module 200 is connected to the gas compressor 100 and is provided with a tube side inlet 231 through which the biogas compressed by the gas compressor 100 is introduced. The other is provided with a tube side outlet 232 through which the gas separated by the membrane contact is discharged.

The two caps of the deaeration membrane contactor module 500 are provided with a tube side outlet 531 connected to the vacuum pump 550 such that a vacuum is formed on the tube side of the deaeration membrane contactor module 500 so that secondary degassing is performed. have.

At this time, the vacuum pump 550 may be connected to only one of the two tube side outlet 531.

Partition walls 234 and 534 are formed between the caps 230 and 530 and the internal spaces of the module housings 210 and 510 to separate the spaces between the caps 230 and 530 and the module housings 210 and 510. Since the hollow fiber membranes 220 and 520 are connected to the partition walls 234 and 534, the inner spaces 233 and 533 of the caps 230 and 530 are the inner spaces of the hollow fiber membranes 220 and 520. Is in communication with the shell side (211,511).

The flow path control tubes 240 and 540 are the main components in the present invention, and are installed such that an intermediate portion is located inside the module housings 210 and 510 while passing through the two caps 230 and 530.

In addition, at one end, shell side inlets 241 and 541 through which liquid such as water flows are formed, and on the other end, shell side outlets 242 and 542 through which inflowed liquid is discharged.

The flow control tubes 240 and 540 are formed in a hollow tube shape, and partitions 243 and 543 are installed inside the middle portion.

As a result, the liquid introduced into the shellside inlets 241 and 541 cannot be discharged to the shellside outlets 242 and 542 by the direct.

In addition, a plurality of holes 244 and 544 are formed at both outer peripheral surfaces of the partitions 243 and 543 so that the liquid is released from the side holes 244 and 544 of the shell side inlets 241 and 541. To the shellside outlets 242 and 542 and through the holes 244 and 544 at the shellside outlets 242 and 542 to move to the shellside outlets 242 and 542 while the liquid at the side of the shellsides 211 and 511 flows into the inside. have.

At this time, the size of the holes (244, 544) is preferably made of 0.5 ~ 50mm in diameter.

If the diameter is less than 0.5mm, the smooth movement of the liquid particles passing through the holes 244 and 544 may be difficult, and liquid movement through the holes 244 and 544 may be difficult. , 544) requires a lot of pressure to move through the membrane contactor separation efficiency can be reduced.

In addition, the holes 244 and 544 may be arranged in various ways. The holes 244 and 544 may be arranged in a line with the axial direction of the flow path control tubes 240 and 540 or may be spirally formed along the axial direction of the flow path control tubes 240 and 540. have.

In addition, the holes 244 and 544 may be formed to be spaced apart from each other along the axial direction of the flow path control tubes 240 and 540, respectively, with the above-mentioned diameter, but in a single slot shape with the above-described diameter or width. It may be formed.

In addition, a plurality of holes 244 and 544 are formed at equally divided positions on the outer circumferential surface based on the cross section of the flow path control tube 40 to be evenly distributed so that the separation efficiency is kept constant.

In particular, the holes 244 and 544 are spirally formed along the outer circumferential surfaces of the flow control tubes 240 and 540 to discharge or inflow through the holes 244 and 544 formed at different angles on the liquid path. It can increase.

In addition, a plurality of holes 244 and 544 are formed at regular intervals along the length direction of the flow path control tubes 240 and 540, and the holes 244 and 544 at the ends adjacent to the partitions 243 and 543 are partition walls. It is preferably located at 3/5 to 4/5 of the distance between the (234, 534) and the partitions (243, 543).

If it is too close to the partitions 243 and 543 outside the above range, the separation efficiency may decrease when the liquid is introduced and discharged in the adjacent state from the partitions 243 and 543, and conversely, too far from the partitions 243 and 543. In this case, in the spaces adjacent to the partitions 243 and 543, the separation is not smooth and the thickness of the boundary layer becomes thick, which may reduce the separation efficiency.

The configuration of the modules is a cross flow at the shell side inside the module housings 210 and 510 by installing the flow path control tubes 240 and 540 having the partitions 243 and 543 and the holes 244 and 544. As is formed, the mixing effect is further increased and the gas separation effect is excellent.

Hereinafter, the biogas purification membrane contact method of the present invention will be described in detail.

1. Step 1

By using the above-described membrane contact system, the biogas including gas having a property of dissolving in a liquid is compressed to a pressure higher than normal pressure or a pressure exceeding an operating pressure by using the gas compressor 100.

At this time, it is preferable that the pressure of the compressed biogas is 5 to 15 bar, and the temperature of the cooled biogas is -20 to 50 ° C.

If the pressure of the biogas is less than 5bar, there is a problem that the purity and recovery of methane according to the water-absorbing gas absorption process using the absorption separator contactor module 200 is lowered, the hollow fiber membrane 220 may be damaged at 15 bar or more There is a problem.

If the biogas temperature is less than -20 ℃, there is a problem of inhibiting the dissolution of the water-soluble gas by freezing the water, which is the liquid supplied in the absorber membrane contactor module 200, above 50 ℃ the solubility of the water-soluble gas is reduced to the water-soluble gas There is a problem of inhibiting the dissolution.

2. Step 2

The biogas pressurized by the gas compressor 100 is supplied to the tube side inlet 231 of the absorption separator contactor module 200 to make membrane contact with one side of the hollow fiber membrane 220, and the pressure pump 610 is used. The liquid is supplied to the shellside inlet 241 at a pressure higher than that of the biogas pressurized by the tubeside inlet 231 of the absorption separator contactor module 200 to make membrane contact with the other side of the hollow fiber membrane 220.

In addition, the ratio of the gas flow rate compressed through the gas compressor 100 to the absorption separator contactor module 200 and the flow rate of the liquid supplied to the absorption separator contactor module 200 through the pressure pump 610 is G / L. It is called a (Gas / Liquid) ratio and it is preferable to keep G / L ratio to 0.01-10.

At this time, the liquid pressure is preferably supplied at a pressure of 0.3 bar to 0.7 bar higher than the biogas pressure.

If a pressure lower than the pressure is applied to the liquid, pressure fluctuation with the biogas may not occur due to a change in pressure during the pressure control, or the pressure of the biogas may be temporarily increased, thereby causing bubbles in the water. Not only is the soft hydrophobic porous hollow fiber membrane damaged, but also unnecessary pressurized energy can be consumed.

Carbon dioxide, hydrogen sulfide, ammonia, etc., which are representative water-soluble gases mixed in biogas through the above process, are dissolved in water and moved to the shellside outlet 242, and methane which is not easily dissolved in water is a tubeside outlet ( 232) to increase the methane purity.

The solubility of gas in water is proportional to the pressure exerted on Henry's law.

In particular, water-soluble gases such as carbon dioxide, hydrogen sulfide and ammonia obey this law.

As the pressure of the biogas containing the water-soluble gas increases, the partial pressure of the water-soluble gas also increases in proportion, so that the solubility of the water-soluble gas in water increases in proportion to the pressure of the biogas.

Therefore, when the pressure of the biogas increases from normal pressure (1 atm) to 10 atm, the amount of water-soluble gas dissolved in water also increases by 10 times.

Biogas pressure when the membrane is contacted by passing water through a shellside that is the inside of a hydrophobic porous hollow fiber membrane formed of a polymer such as polypropylene (PP). When the pressure is greater than this pressure, biogas flows through the pores on a large scale toward the water, creating bubbles in the water.

As a result, a problem arises in that effective selective dissolution by membrane contact of only the water-soluble gas contained in the biogas is impossible.

However, in the present invention, the biogas containing the water-soluble gas is compressed to a pressure higher than the normal pressure to come into contact with one side of the hollow fiber membrane, and at the same time, the water is pressurized by a predetermined pressure higher than the pressure of the compressed biogas to make the hollow fiber membrane The membrane was brought into contact with the other side to increase the amount of water-soluble dissolved in water, and to prevent bubbles from occurring in the water.

3. Step 3

The liquid discharged to the shellside outlet 242 after the membrane contact with the hollow fiber membrane 220 contains a water-soluble gas in a dissolved state, which is maintained at atmospheric pressure or vacuum and sprayed to disperse the liquid in the tank at the upper end thereof. The nozzle is supplied to the degassing tank 300 to which the nozzle is installed, and the gas is first degassed until a liquid equilibrium is achieved between the liquid and the gas dissolved in the liquid.

That is, when the pressure applied to the biogas and the liquid in the absorption separator contactor module 200 is lowered to atmospheric pressure or vacuum in the degassing tank 300, the solubility of water in water is lowered, and the water solubility dissolved in water by the difference is reduced. The gas will leave.

4. Step 4

The gas degassed in the degassing tank 300 to become insoluble state is supplied to the gas compressor 100 through the gas discharge pipe 400.

The gas degassed in the degassing tank 300 includes the remaining amount of methane in addition to the methane separated from the first absorption membrane contactor module 200, and supplies the gas compressor 100 to the gas compressor 100 through a pipe again to absorb the membrane contactor module ( 200) to increase the methane recovery of the system.

5. Step 5

The first degassed liquid from the degassing tank 300 is supplied to the shell side inlet 541 of the degassing membrane contactor module 500 to make membrane contact with one side of the hollow fiber membrane 520, and degassed with the vacuum pump 550. A vacuum is applied to the tube side 521 of the separator contactor module 500 to degas the secondary.

When the vacuum pump 550 maintains the state below the normal pressure, the water-soluble gas contained in the liquid can be more completely degassed.

6. Step 6

Shell side of the absorption separator contactor module 200 through the liquid circulation tube 600 while pressurizing the liquid discharged to the shell side outlet 542 of the degassing membrane contactor module 500 with the pressure pump 610. It is supplied to the absorption separator contactor module 200 through the inlet 241.

The liquid from which the water-soluble gas is degassed through the five steps is injected into the absorption separator contactor module 200 and reused to dissolve the water-soluble gas.

That is, the liquid used to absorb and degas the water-soluble gas is a medium for absorbing and degassing and discharging the water-soluble gas while repeating the sequence of the absorption separator contactor module 200, the degassing tank 300, and the deaeration membrane contactor module 500. It will play a role.

Experimental Example 2 Measurement of Purified Methane Concentration and Methane Recovery

A membrane contact system having the configuration as shown in FIG. 8 including the absorption separator contactor module 200 and the deaeration separator contactor module 500 having the structure as shown in FIG. 2 was prepared, and the liquid used was water and the absorption separator contactor module 200 ), Simulated gas mixtures containing 41% methane and 59% carbon dioxide were prepared and supplied.

In addition, the tube side inlet 231 of the absorption separator contactor module 200, the tube side outlet 232, one side of the gas discharge pipe 400 adjacent to the degassing tank 300, and the tube side outlet of the deaeration membrane contactor module 500 ( The pressure, flow rate and methane concentration in 531) were measured and shown in Table 2, respectively.

TABLE 2

Item	Pressure (bar)	Flow rate (sccm)	Methane concentration (%)
Tube side inlet 231 of absorption separator contactor module 200	5.5	1,198.8	41.00
Tube side outlet 232 of the absorption separator contactor module 200	5.5	413.3	97.03
One side of the gas discharge pipe 400 adjacent to the degassing tank 300	0.01	126.3	61.48
Tube side outlet 531 of the deaeration membrane contactor module 500	-0.95	659.2	1.94

As shown in Table 2, the concentration of highly purified methane was 97.03%, and the methane recovery of the system was found to be very high at 97.4%.

Membrane contactor module of the present invention is widely applied throughout the industry, such as wastewater treatment, water treatment, including water production, concentration in the food and pharmaceutical sector, separation of oxygen and nitrogen in the air, recovery of ammonia, solid and liquid, liquid and It may be used to separate liquids, gases and gases, and liquids and gases.

In particular, the membrane contact system and membrane contact method of the present invention will be suitable for separating specific target gases, such as methane, from biogas generated during the anaerobic digestion of organics.

Claims (14)

1. In the membrane contactor module,

   A module housing 10 formed of a hollow hollow shape;

   The hollow fiber membrane 20 having the shell housing 11 formed in the module housing spaced apart from the inner wall surface of the module housing 10 along the longitudinal direction and having the tube side 21 formed in the longitudinal direction therein. and;

   It is provided at both ends of the module housing 10, the tube side inlet 31 is formed on one side, the tube side outlet 32 is formed on the other side, the inner space 33 is the tube side 21 Two caps 30 having a partition 34 formed therein so as to be in communication with the shell side 11;

   A middle part is installed to penetrate the two caps 30 and is located inside the module housing 10. A shell side inlet 41 is formed at one end and a shell side outlet 42 at the other end. The inside is formed in the form of a hollow tube, the partition 43 is installed inside the middle portion, and the plurality of holes 44 are formed on both outer peripheral surfaces based on the partition 43, the shell side inlet ( 41, the liquid moves from the side hole 44 to the shell side 11, and the liquid on the side of the shell side 11 flows into the shell side outlet port 44 through the shell side outlet 42 side hole 44. Configured to include; flow control tube 40 configured to move to 42

   Membrane Contactor Module.
2. The method of claim 1,

   A plurality of blocking walls 51 are formed inside the longitudinal direction to form a plurality of unit installation spaces 52 divided by the blocking walls 51 to form the module housing 10, the hollow fiber membrane 20, and the cap. 30 and the flow path control tube 40 are respectively inserted into the unit installation space 52 to form a unit 60, the wall has a connecting passage 53 for connecting each unit installation space 52 Is formed, the connecting passage 53 is formed to connect the internal space 33 of the cap 30 of the adjacent unit 60, the flow path control tube 40 of the adjacent unit 60 so that the interior is in communication with each other Characterized in that the outer case 50 is further provided,

   Membrane Contactor Module.
3. The method according to any one of claims 1 to 2,

   The hole 44 is characterized in that the diameter is made of a size of 0.5 ~ 50mm,

   Membrane Contactor Module.
4. The method according to any one of claims 1 to 2,

   The hole 44 is in line with the axial direction of the flow path control tube 40, or characterized in that the single slot shape formed along the axial direction in a spiral,

   Membrane Contactor Module.
5. The method according to any one of claims 1 to 2,

   The hole 44 is characterized in that a plurality of holes are formed in equally divided positions on the outer peripheral surface based on the cross section of the flow path control tube 40,

   Membrane Contactor Module.
6. The method of claim 5,

   The hole 44 is characterized in that the spiral formed along the outer peripheral surface of the flow control tube 40,

   Membrane Contactor Module.
7. The method according to any one of claims 1 to 2,

   A plurality of holes 44 are formed at regular intervals along the length direction of the flow path control tube 40, and the holes 44 at the front end adjacent to the partition 43 are formed between the partitions 34 and the partition 43. Characterized in 3/5 to 4/5 of the street,

   Membrane Contactor Module.
8. The method according to any one of claims 1 to 2,

   Inner diameter / length of the module housing 10, characterized in that 1/2 ~ 1/20,

   Membrane Contactor Module.
9. In the membrane contact system for biogas purification,

   A gas compressor (100) for pressurizing a biogas including a gas having a property of dissolving in a liquid to a pressure greater than normal pressure;

   A module housing 210 having an empty hollow shape and an inside of the module housing are installed to be spaced apart from the inner wall surface of the module housing 210 along a length direction to form a shell side 211 to the outside, and a length inside the module housing 210. The hollow fiber membrane 220 and the tube housing 221 in which the tube side 221 is formed, respectively, are installed at both ends of the module housing 210, and the tube side inlet through which the biogas compressed by the gas compressor 100 flows on one side. 231 is formed, a tube side discharge port 232 through which the biogas in contact with the other side is discharged is formed, and the inner space 233 is in communication with the tube side 221 and the shell side 211 Two caps 230 having the partition wall 234 formed to be blocked, and the middle portion penetrates the two caps 230 and are installed to be positioned inside the module housing 210, and at one end thereof from the outside. Liquid flows in Shell side inlet 241 is formed, the shell side discharge port 242 is formed inside the empty tube form is formed, the liquid flowing in the other end is discharged, the partition 243 is provided inside the middle portion In addition, a plurality of holes 244 are formed at both outer peripheral surfaces of the partition 243, so that the liquid moves from the hole 244 at the shellside inlet 241 to the shellside 211, and the shellside outlet 242. Absorption membrane contactor module 200 composed of a flow path control tube 240 is configured to move to the shell side outlet 242 while the liquid on the side of the shell side 211 through the hole (244) side;

   A degassing tank 300 for storing the liquid discharged from the shell side outlet 242 of the absorption separator contactor module 200 at atmospheric pressure or in a vacuum state;

   One side is connected to the upper side of the degassing tank 300, the other side is connected to the gas compressor 100, a blower 410 is installed in the middle of the pipeline to the gas in the injured state of the gas compressor 100 Gas discharge pipe 400 for supplying with;

   A module housing 510 having an empty hollow shape and a module housing 510 spaced apart from an inner wall surface of the module housing 510 in a longitudinal direction inside the module housing are formed to form a shell side 511 to the outside and have a length therein. The hollow fiber membrane 520 in which the tube side 521 is formed, and the module housing 510 at both ends, respectively, and an inner space 533 communicates with the tube side 521 and the shell side 511. The barrier ribs 534 are formed to be blocked from each other, and the tube side discharge ports 531 connected to the vacuum pump 550 are formed on both sides thereof, and the air inside the tube side 521 is discharged to the outside by the vacuum pump 550. And two caps 530 configured to form a vacuum in the tube side 521, and an intermediate portion is installed inside the module housing 510 while penetrating the two caps 530. In the degassing tank 300 and piping A shell-side inlet 541 is formed to be connected to the liquid stored in the degassing tank 300, and a shell-side outlet 542 is formed in which the liquid introduced into the other end is discharged. The partition 543 is provided inside the middle portion, and a plurality of holes 544 are formed on both outer peripheral surfaces of the partition 543 so that the liquid from the hole 44 at the side of the shellside inlet 541 is formed. Flows to the shell side 511 and moves to the shell side outlet 542 while the liquid on the side of the shell side 511 flows into the shell side through the hole 544 of the shell side outlet 542. A degassing membrane contactor module 500 consisting of 540;

   One side is connected to the shell side outlet 542, the other side is connected to the shell side inlet 241 of the absorption separator contactor module 200, and a pressure pump 610 is installed at one side of the pipeline to provide a deaeration separator contactor. And a liquid circulation tube (600) configured to supply the absorbent membrane contactor module (200) while pressurizing the liquid passing through the module (500).

   Membrane contact system for biogas purification.
10. In the membrane contact method for biogas purification,

    Compressing a biogas including a gas having a property of dissolving in a liquid using the biogas purification membrane contact system of claim 9 to a pressure higher than normal pressure using the gas compressor (100);

    The biogas pressurized by the gas compressor 100 is supplied to the tube side inlet 231 of the absorption separator contactor module 200 to make membrane contact with one side of the hollow fiber membrane 220, and the pressure pump 610 is used. Supplying the liquid to the shellside inlet 241 at a higher pressure than the biogas pressurized by the tubeside inlet 231 of the absorption separator contactor module 200 to make the membrane contact with the other side of the hollow fiber membrane 220;

    The liquid discharged to the shell side outlet 242 after the membrane contact with the hollow fiber membrane 220 is supplied to the degassing tank 300 maintained at atmospheric pressure or vacuum to be dissolved in the liquid and the liquid in the degassing tank 300. Firstly degassing the gas until dissolution equilibrium occurs;

    Supplying a gas degassed in the degassing tank (300) to the gas compressor (100) through the gas discharge pipe (400);

    The first degassed liquid from the degassing tank 300 is supplied to the shell side inlet 541 of the degassing membrane contactor module 500 to make membrane contact with one side of the hollow fiber membrane 520, and degassed with the vacuum pump 550. Applying a vacuum to the tube side 521 of the membrane contactor module 500 to perform secondary degassing;

    Shell side of the absorption separator contactor module 200 through the liquid circulation tube 600 while pressurizing the liquid discharged to the shell side outlet 542 of the degassing membrane contactor module 500 with the pressure pump 610. It comprises; supplying to the absorption separator contactor module 200 through the inlet 241,

    Membrane contact method for biogas purification.
11. The method of claim 10,

    The pressure applied to the liquid through the pressure pump 610 is characterized in that to maintain a 0.3 bar-0.7 bar higher than the pressure applied to the biogas,

    Membrane contact method for biogas purification.
12. The method of claim 10,

    The ratio of the gas flow rate compressed through the gas compressor 100 and supplied to the absorption separator contactor module 200 and the flow rate of the liquid supplied to the absorption separator contactor module 200 through the pressure pump 610 is maintained at 0.01 to 10. Characterized in that

    Membrane contact method for biogas purification.
13. The method of claim 10,

    The biogas is a mixed gas generated during the anaerobic digestion of organic substances, characterized in that any one of methane, carbon dioxide, toil sulfide, ammonia,

    Membrane contact method for biogas purification.
14. The method of claim 10,

    Degassing tank 300 during the first degassing, characterized in that for maintaining the internal temperature at 5 ~ 50 ℃,

    Membrane contact method for biogas purification.

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