JP2012210600A - Gas separator - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a gas separator capable of efficiently separating target gas from mixed gas.SOLUTION: The gas separator 100 includes a module 10 comprising tubular membrane elements 14 having separation membranes for selectively permeating and separating the target gas from the mixed gas; a casing 12 storing the membrane elements 14 and having a supply port to which the mixed gas is supplied, and an ejection port from which the mixed gas is ejected; and a passage tube 22B leading out the target gas that has permeated the membrane elements 14, to the outside of the casing 12. The plurality of modules 10 are connected to one another; in the continuously connected modules 10, the ejection port of the upstream module 10 communicates with the supply port of the downstream module 10, and each of the plurality of modules 10 is provided with the passage tube 22B.

Description

  The present invention relates to a gas separation device.

  In recent years, gas discharged from factories and the like has been separated and discharged from the viewpoint of environmental conservation. In particular, carbon dioxide, which is a cause of global warming, is required to reduce emissions, and it is required to efficiently separate carbon dioxide from the exhausted gas.

  In the industrial field, a plurality of membrane elements having tubular gas separation membranes provided on the peripheral surface are arranged in a casing, a mixed gas is passed through the casing or the membrane element, and the target gas is passed through the membrane element. Gas separation is performed by permeating the gas. In such a method, in order to improve the separation efficiency, it has been proposed to increase the permeation performance per module volume by lengthening the membrane element. However, it is difficult to produce a membrane element having a length of 1 m or more, and this problem is particularly noticeable in the case of a liquid membrane with high separation. In addition, when a large number of cylindrical members are connected to increase the length of the casing, the number of connection parts increases, and thus the dead volume increases. Therefore, it is conceivable to connect the membrane elements having a short length, but there is a risk that the transmission efficiency may deteriorate due to the problem of the gas partial pressure in the flow path of the sweep gas.

  Regarding such a problem, for example, in the gas separation filter described in Patent Document 1, a conical membrane element is arranged in the casing. With such a configuration, in this gas separation filter, the surface area is increased without increasing the length dimension of the membrane element.

  Further, in the separation membrane module described in Patent Document 2, the body is installed so that the circular surface of the body is horizontal, the internal space is divided into two in the height direction at one end of the body, and one region is gas. The upstream passage and the other region are the gas downstream passage. And the membrane element is installed in each channel | path, and it has the structure by which the gas which entered from the upstream channel | path in the area | region of the other end part of a fuselage is turned back to a downstream channel | path.

JP 2002-66271 A JP 2009-226374 A

  However, in the thing of the said patent document 1, since it has comprised conical shape, when it is going to arrange in the casing in multiple numbers, a space is needed only in the area | region side of one side, and space efficiency will deteriorate. In addition, in the conical shape, the flow rate of the gas after passing through the membrane element changes depending on the location, so that there is a problem that the target gas does not pass stably. Furthermore, when a liquid film is used for this membrane element, dissolution will reach equilibrium if the mixed gas comes into contact to some extent, and there is a possibility that the gas cannot be sufficiently separated.

  Moreover, although the thing of the said patent document 2 is effective from a viewpoint of the equilibrium of gas, a structure is complicated and the internal diameter of a fuselage becomes large inevitably. Moreover, since the inlet and outlet for the mixed gas are provided at the same end, there is a problem that the form of installation is limited and the practicality is lowered.

  The present invention has been made to solve the above-described problems, and an object of the present invention is to provide a gas separation device that can efficiently separate a target gas from a mixed gas.

  In order to solve the above problems, a gas separation device according to the present invention includes a tubular membrane element having a separation membrane that selectively permeates and separates a target gas from a mixed gas, a membrane gas, and a mixed gas. A module having a tubular casing having a supply port to which gas is supplied and a discharge port from which the mixed gas is discharged, and a lead-out portion for leading the target gas that has passed through the membrane element to the outside of the casing. A plurality of connected modules are connected so that the discharge port of the upstream module and the supply port of the downstream module communicate with each other, and a lead-out portion is provided for each of the plurality of modules. It is characterized by that.

  In this gas separation device, in the connected modules, the discharge port of the upstream module and the supply port of the downstream module are connected so as to communicate with each other. Each of the plurality of modules is provided with a derivation unit that derives the target gas that has passed through the membrane element to the outside of the housing. In this way, by connecting the modules in multiple stages, the contact area between the mixed gas and the membrane element can be increased without forming a long membrane element or connecting a plurality of membrane elements. Gas separation becomes possible. Moreover, since it is a simple structure, what is necessary is just to connect a module in multiple stages according to the desired separation capability, and a structure can be changed according to the objective. As described above, in the gas separation device of the present invention, the target gas can be efficiently separated from the mixed gas.

  In the present specification, the “target gas” is a gas that needs to be obtained by being separated from the mixed gas, and is a gas that is selectively permeated by the separation membrane. Here, “selectively permeate” means not only a mode in which gas molecules diffuse through the pores of a so-called porous membrane, but also diffusion, Includes carrier transport. However, when one kind of gas is separated from the mixed gas, even if the purpose is to obtain a mixed gas from which one kind of gas is removed, the one kind of gas to be removed is referred to as a target gas.

  In the present specification, the “mixed gas” is a mixture of gases containing at least two kinds of gases including the target gas and having different diffusion or solubility with respect to the gas separation membrane. For example, as a mixed gas containing carbon dioxide as a target gas, an exhaust gas obtained by spreading a hydrocarbon-based fuel in a factory or the like, a mixed gas containing hydrogen and carbon dioxide generated from a hydrocarbon as a gas for a fuel cell, or And a mixed gas containing carbon dioxide and carbon-based gas produced in the petroleum industry. Alternatively, when separating oxygen to obtain an oxygen-enriched gas, there is a mixed gas such as nitrogen and oxygen.

  Moreover, it is preferable that a plurality of membrane elements are arranged in the housing. According to such a configuration, the target gas can be more efficiently separated from the mixed gas.

  In addition, it is preferable that the membrane element is connected to the lead-out portion at one end portion and to the introduction portion into which the sweep gas is introduced at the other end portion. In this way, by introducing the sweep gas, the target gas can be recovered satisfactorily.

  The gas separation device according to the present invention can efficiently separate the target gas from the mixed gas.

It is the schematic which shows the gas separation apparatus which concerns on one Embodiment of this invention. (A) is an end view taken along line aa in FIG. 1, (b) is an end view taken along line bb in FIG. 1, and (c) is a view showing a modification of (b). It is the schematic which shows the gas separation apparatus which concerns on an Example. It is the schematic which shows the gas separation apparatus which concerns on an Example. It is the schematic which shows the gas separation apparatus which concerns on an Example. It is the schematic which shows the gas separation apparatus which concerns on a modification.

  Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. In the description of the drawings, the same or equivalent elements will be denoted by the same reference numerals, and redundant description will be omitted.

  FIG. 1 is a schematic view showing a gas separation device according to an embodiment of the present invention. 2A is an end view taken along line aa in FIG. 1, and FIG. 2B is an end view taken along line bb in FIG. In FIG. 1, a part is shown in cross section.

  The gas separation device 100 shown in each figure selectively separates carbon dioxide from exhaust gas generated when, for example, a hydrocarbon-based fuel is spread, and hydrogen generated from a hydrocarbon as a fuel cell gas. It is an apparatus that selectively separates carbon dioxide from a mixed gas of carbon dioxide or separates carbon dioxide and carbon-based gas produced in the petroleum industry. In addition, as other usage methods, a usage method of humidifying or dehumidifying by allowing water vapor to permeate through a membrane, a method of using in a combustion furnace application, an air conditioner application, a diesel engine application, or the like can be considered.

  As shown in FIGS. 1 and 2, the gas separation device 100 is configured by connecting a plurality (here, two) of modules 10. The module 10 includes a casing (housing) 12 and a plurality of membrane elements 14 accommodated in the casing 12. Each module 10 has the same configuration. In the gas separation device 100, the mixed gas to be separated may pass through the outside of the membrane element 14 or may pass through the inside of the membrane element 14. In the following description, a configuration in which a mixed gas is allowed to pass through the outside of the membrane element 14 and the target gas selectively separated by the membrane element 14 passes through the inside of the membrane element 14 having a negative pressure than the outside will be described.

  The casing 12 is made of various materials such as SUS (Steel Use Stainless), aluminum, and resin, and has a tubular shape. The casing 12 accommodates the membrane element 14 and forms a flow path for the mixed gas.

  Holding members 16 </ b> A and 16 </ b> B are disposed at both ends in the longitudinal direction of the casing 12. The holding members 16A and 16B are members that hold the membrane element 14 and have a cylindrical shape. Grooves (not shown) are formed annularly on the outer peripheral surface side of the holding members 16A and 16B in accordance with the outer shape of the casing 12, and both end portions of the casing 12 are inserted into the grooves. A flange 18 is provided around the ends of the holding members 16A and 16B. The flange 18 projects outward in the radial direction of the holding members 16A and 16B, and a plurality of (here, four) through holes H into which bolts (not shown) are inserted are formed.

  As shown in FIG. 2B, a circular opening 20 (21) penetrating the holding member 16A in the thickness direction is formed in the central portion of the holding member 16A (16B). The opening 20 is a mixed gas supply port, and the opening 21 is a mixed gas discharge port. The openings 20 and 21 communicate with the internal space of the casing 12. As shown in FIG. 2C, a plurality of openings 20 (21) may be formed in the holding member 16A (16B). In FIG. 2C, a portion indicated by a broken line indicates a branch flow path portion 22Ab (22Bb) described later which is a membrane element holding hole into which one end of the membrane element 14 is inserted.

  The holding members 16A and 16B are provided with channel tubes 22A and 22B to which a membrane element 14 described later is connected. The channel tube 22A has a main channel portion 22Aa and a branch channel portion 22Ab. The main flow path portion (introduction portion) 22Aa is drawn to the outside of the casing 12, and the opening at the end serves as the introduction port for the sweep gas. The branch flow path portion 22Ab is branched from the main flow path portion 22Aa, and a plurality of branch flow path portions 22Ab are provided corresponding to the arrangement positions of the membrane elements 14. The channel tube 22B has a main channel portion 22Ba and a branch channel portion 22Bb. The main flow path portion (lead-out portion) 22Ba is drawn out of the casing 12, and the opening at the end serves as a lead-out port for the target gas. The branch flow path portion 22Bb branches from the main flow path portion 22Ba, and a plurality of branch flow path portions 22Bb are provided corresponding to the arrangement positions of the membrane elements 14.

  A reinforcing member 24 is disposed in the casing 12. A plurality (four in this case) of the reinforcing members 24 are provided in the casing 12. The reinforcing member 24 is a columnar member, and is provided across the holding members 16A and 16B arranged to face each other. Specifically, the reinforcing member 24 is disposed in the casing 12 in the vicinity of the inner peripheral surface, and is disposed at a position facing the vertical and horizontal directions shown in FIG.

  The membrane element 14 selectively permeates and separates the target gas from the mixed gas. The membrane element 14 has a tubular shape extending in the longitudinal direction of the casing 12, and a separation membrane is provided on the outer surface. One end of the membrane element 14 is held by the holding member 16 </ b> A, and the other end is held by the holding member 16 </ b> B, and is accommodated in the casing 12 with a predetermined gap. That is, in the casing 12, a portion other than the membrane element 14 and the reinforcing member 24 is a mixed gas flow path. Each membrane element 14 is connected to the branch channel portions 22Ab and 22Bb of the channel tubes 22A and 22B, respectively, and the inside communicates with the channel tubes 22A and 22B. Although the arrangement position of the membrane element 14 is arbitrarily set, it can be arranged uniformly along the diameter of the casing 12.

  The module 10 having the above-described configuration is connected in multiple stages to constitute the gas separation device 100. Specifically, in the gas separation device 100, the flange 18 is opposed so that the discharge port (opening 21) of the upstream module 10 and the supply port (opening 20) of the downstream module 10 communicate with each other. Arranged and bolted.

  In the gas separation device 100, the mixed gas supplied from the supply port of the casing 12 (the opening 20 of the holding member 16 </ b> A) passes through the casing 12 while being in contact with the membrane element 14 as indicated by an arrow in FIG. 1. Then, it is discharged from the discharge port (opening 21 of holding member 16B). At this time, the target gas is selectively separated from the mixed gas by the membrane element 14 provided in the casing 12. Thereby, the mixed gas discharged from the discharge port of the casing 12 has a small content of the target gas, and this mixed gas is supplied from the supply port of the module 10 at the next stage.

  The target gas separated by the membrane element 14 is accompanied by the sweep gas introduced from the main flow path portion 22Aa of the flow path tube 22A on the holding member 16A side, and is led out from the main flow path portion 22Ba of the flow path pipe 22B of the holding member 16B. Is done. As the sweep gas, for example, a rare gas such as argon or steam can be used. In the gas separation device 100, the sweep gas is introduced from the main channel portion 22Ba of the channel tube 22B provided in the holding member 16B, and the target gas accompanied by the sweep gas is provided in the holding member 16A. You may derive | lead-out from 22A main flow-path part 22Aa.

  In the gas separation device 100, the pressure on the mixed gas side (external pressure of the membrane element 14) is about 0.1 MPaA to 6.0 MPaA, and the pressure on the target gas side (internal pressure of the membrane element 14) is about 0 MPaA to 0.5 MPaA. In the present embodiment, the gas separation device 100 can separate the mixed gas at a temperature of about 20 ° C. to 200 ° C.

  Next, the membrane element 14 will be described in detail. The membrane element 14 is formed of a membrane material provided with a separation membrane around it, and maintains a certain shape (tubular shape) under the conditions of use. The separation membrane is appropriately selected depending on the target gas to be selectively separated. For example, a porous membrane can be used, and a solution diffusion membrane such as a liquid membrane is more preferable. In the case of using a liquid film, it is preferable that the liquid film is provided so as to face the casing 12 side (mixed gas side) in the membrane element 14 disposed in the gas separation device 100.

  As a method of constructing the tubular membrane element 14, for example, the surface of the hydrophobic porous membrane is irradiated with radiation in a state where a hydrophilic polymer, an oligomer thereof or a liquid containing the monomer is brought into contact with the surface of the porous membrane, thereby There is a method of forming a hydrophilic polymer gel film and impregnating with water. Alternatively, a liquid having affinity for the target gas may be supported in the porous body and covered with the liquid sealing material from both sides.

  The porous film is formed by forming an organic or inorganic porous material into a tubular shape. The porous membrane has a length of about 50 mm to 700 mm, a thickness of 10 μm to 2 mm, preferably 10 μm to 1 mm, and a diameter (outer diameter) of about 5 mm to 20 mm.

As for the pore structure characteristics of this porous membrane, the average pore diameter is usually 10 μm or less, preferably 0.1 μm or less, and the porosity is 5 to 99%, preferably 30 to 90%. The gas permeation rate is preferably, for example, 10 ⁻⁵ (cm ³ (STP) / cm ² · sec · cmHg) or more in terms of carbon dioxide permeation rate.

  The liquid film may be a gel film. A conventionally well-known thing can be used as a hydrophilic polymer for forming a gel film. Examples of hydrophilic polymers include xanthan gum, locust bean gum, gelatin, starch, amylose, amylopectin, cellulose, methylcellulose, hydroxyethylcellulose, carboxymethylcellulose, alginic acid, chitin, and other polysaccharides and modified products thereof, as well as polyvinyl. Alcohol, polyethylene glycol, polyethylene oxide, polyacrylic acid, polysulfonic acid, polyacrylamide, polyallylamine, polyethyleneimine, acrylic acid / vinyl alcohol copolymer, methacrylic acid / vinyl benzene copolymer, acrylic acid / sulfonic acid copolymer Etc.

  In addition, sulfonated products of the above polymers, aminated products, chloromethylated products, ion complexes, and the like can also be used.

  As described above, a polymer gel composite membrane having a structure in which a polymer gel membrane is bonded to one surface of the porous membrane is obtained. In this case, by using a liquid containing water such as an aqueous solution as a liquid, As the polymer gel film, a film containing water (polymer hydrogel film) can be obtained. When the polymer gel film does not contain water, the polymer hydrogel film can be obtained by bringing the gel film into contact with water or a liquid containing water.

Such a polymer gel composite membrane or polymer hydrogel composite membrane is used as it is as a water vapor permeable membrane or as a separation membrane for hydrophilic gases such as CO ₂ , SO ₂ , NO ₂ , CO, NO, and CH _4. Although it can be used, it can be used as a gas separation facilitating transport membrane by containing an aqueous solution of a gas carrier in the polymer gel membrane.

  In this case, as a method of obtaining a polymer gel film containing an aqueous solution of a gas carrier, a method of drying the polymer gel film and then bringing it into contact with an aqueous solution of a gas carrier to form a polymer hydrogel film, or a polymer gel film And a gas carrier aqueous solution is contacted to diffuse the gas carrier aqueous solution into the polymer gel film.

  Examples of such a gas carrier include, for example, alkali metal carbonates such as sodium carbonate and potassium carbonate, alkali metal bicarbonates such as sodium bicarbonate and potassium bicarbonate, ethanolamine, if carbon dioxide is separated. And conventionally known ones such as alkanolamines such as diethanolamine, triethanolamine, propanolamine, dipropanolamine, and tripropanolamine. In addition, in the case of the alkali metal carbonate or bicarbonate described above, a polydentate ligand that forms a complex with an alkali metal ion, sodium arsenite, carbonic anhydrase, boric acid, or the like can be used in combination as an auxiliary additive component. .

  The carbon dioxide carrier is not limited to the above, and any carbon dioxide carrier may be used as long as it has an affinity for carbon dioxide and exhibits water solubility, and various kinds of organic acid alkali metal salts can be used. However, since the carrier has low chemical stability and low vapor pressure and is unlikely to be lost from the membrane, alkali metal carbonates and alkali metal bicarbonates that can be expected to have long-term durability in separation performance, and hydrophilic properties Basic ionic liquids are preferred.

  As the hydrophilic basic ionic liquid, at least one cation selected from the group consisting of known imidazolium cation, ammonium cation and phosphonium cation, glycine, alanine, valine, leucine, isoleucine, serine, threonine, cysteine, methionine, Asparagine, glutamic acid, glutamine, arginine, lysine, histidine, phenylalanine, tyrosine, tryptophan, aspartic acid, proline (amino acids known as natural L-α-amino acids); 2-aminobutyric acid, 2-aminoisobutyric acid, 2-amino At least one aminocarboxylic acid selected from cyclopentanecarboxylic acid (amino acids known as unnatural α-amino acids); and 4-aminobutyric acid (other amino acids) and taurine An ionic liquid composed of an acid anion or an aminosulfonic acid anion is mentioned.

  As the polydentate ligand that forms a complex with an alkali metal ion, conventionally known ones such as: 12-crown-4, 15-crown-5, 18-crown-6, benzo-12-crown-4, benzo -15-crown-5, benzo-18-crown-6, dibenzo-12-crown-4, dibenzo-15-crown-5, dibenzo-18-crown-6, dicyclohexyl-12-crown-4, dicyclohexyl-15 -Cyclic polyethers such as crown-5, dicyclohexyl-18-crown-6, n-octyl-12-crown-4, n-octyl-15-crown-5, n-octyl-18-crown-6; 2.1], cyclic polyether amines such as cryptand [2.2]; cryptand [2.1.1], cryptand [2] 2.2], other bicyclic polyether amines etc. can be used porphyrins, phthalocyanines, polyethylene glycol, ethylene diamine tetraacetic acid and the like.

  These concentrations are 0.1 to 5.0 mol / l, preferably 1.0 to 4.0 mol / l in the case of alkali metal carbonate and / or alkali metal bicarbonate. In the case of a polydentate ligand that forms a complex with an alkali metal ion, the concentration in an aqueous solution is 0.001 mol / l or more, preferably 0.01 to 0.1 mol / l.

  Moreover, it is preferable to prescribe | regulate the density | concentration in the aqueous solution of the alkanolamine which is another example of the substance which has an affinity with a carbon dioxide to 10 weight% or more.

  As described above, in the gas separation device 100, the connected module 10 is connected so that the discharge port of the upstream module 10 and the supply port of the downstream module 10 communicate with each other. Each of the modules 10 is provided with a flow path pipe 22B that guides the target gas that has passed through the membrane element 14 to the outside of the casing 12. Thus, by connecting the modules 10 in multiple stages, the contact area between the mixed gas and the membrane element 14 can be increased without forming the membrane element 14 long or connecting a plurality of the elements, Gas separation is possible at each stage. Moreover, since it is a simple structure, what is necessary is just to connect the module 10 in multiple stages according to the desired separation capability, and a structure can be changed according to the objective. As described above, the gas separation device 100 can efficiently separate the target gas from the mixed gas.

  EXAMPLES Hereinafter, although this invention is demonstrated more concretely based on an Example and a comparative example, this invention is not limited to a following example at all.

Example 1
A 10 wt% concentration aqueous solution of polyethylene glycol (PEG) (number average molecular weight 50,000) is a ceramic porous material (porosity: 50%, average pore diameter: 10 μm, length: 22 cm, outer diameter: 6 mm, inner diameter) : 4 mm) was applied to the outside, set in an electron beam irradiation apparatus (rated at 200 keV, manufactured by Nissin High Voltage), and irradiated with an electron beam from above the film under a nitrogen atmosphere under the condition of an acceleration voltage of 150 keV. A PEG hydrogel film (hydrogel layer) is immobilized in a porous material state by an electron beam with an irradiation dose of 4 Mrad or more.

  The polymer hydrogel composite membrane thus prepared is impregnated with carbon dioxide carrier in the polymer hydrogel membrane by floating on the ionic liquid tetraethylphosphonium taurine for 30 minutes with the polymer hydrogel membrane face down. To produce a membrane element.

The characteristics of the membrane element obtained as described above were evaluated as follows. A mixed gas of CO ₂ / H ₂ = 50/50 was used as a test gas, and this was supplied to the side on which the polymer hydrogel membrane was fixed at a flow rate of 100 ml / min and a total pressure of 1 atm under saturated water vapor. Was reduced in pressure. The permeated gas was analyzed with a gas chromatograph, and the CO ₂ permeation rate (QCO ₂ ) and the separation factor (α) were calculated.

Thereafter, a module using 78 membrane elements was prepared, and a multistage separation membrane was prepared as shown in FIG. A mixed gas of CO ₂ / H ₂ = 50/50 was allowed to flow from the mixed gas inlet at a temperature of 60 ° C. and 4 L / min, and recovered from the mixed gas outlet. Moreover, sweep gas was allowed to flow from the supply port of the flow path tube, and CO ₂ was recovered from the discharge port of the flow path tube. The result was a CO ₂ / H ₂ separation factor of 70.

(Comparative Example 1)
A gas separation device as shown in FIG. 3 was produced using 78 membrane elements having the same length as that of Example 1 and having twice the length. In the gas separation device shown in FIG. 3, the module 10 has a single-stage configuration and has the same configuration as the module 10 described above, but the length dimension is larger than that of the module 10. In this module 10, an experiment was performed under the same conditions as in Example 1. The result was a CO ₂ / H ₂ separation factor of 55. In addition, there was much damage at the time of creation of a membrane element.

(Example 2)
Using the same material and the same membrane element as in Example 1, the gas separation device shown in FIG. 4 was produced. In the gas separation device 110 shown in FIG. 4, only one sweep gas supply port 32 to the first-stage and second-stage modules 30 is provided in the holding member 31A. Further, a sweep gas flow path 35 is provided in the casing 12. The sweep gas is branched by the branch flow path 33 in the holding member 31A of each module 30, flows through each of the membrane elements 14, and is joined in the other holding member 31B. The result was a CO ₂ / H ₂ separation factor of 70.

(Example 3)
A gas separation device shown in FIG. 5 was produced by providing a spiral projection inside the casing. As shown in FIG. 5, in the gas separation device 120, a spiral protrusion 42 protruding inward is provided on the inner peripheral surface of the casing 41. This gas separation device 120 was performed under the same conditions as in Example 2. Results _were CO 2 / _{H 2} separation factor 75.

  The present invention is not limited to the above embodiment. For example, in the above embodiment, a groove is formed in the holding members 16A and 16B, and the end of the casing 12 is inserted into the groove. However, for example, a configuration as shown in FIG.

  As shown in FIG. 6A, in the module 50, reinforcing members 51 </ b> A and 51 </ b> B are inserted into the casing 52. That is, the inner diameter of the casing 52 and the outer diameters of the reinforcing members 51A and 51B are substantially equal. As shown in FIG. 6B, in the module 60, as in the module 10, grooves are formed in the holding members 61A and 61B, and the end of the casing 62 is inserted into the grooves. In the module 60, the holding members 61 </ b> A and 61 </ b> B project outward from the outer peripheral surface of the casing 62. Moreover, as shown in FIG.6 (c), in the module 70, the cap 71 is attached to the module 50 shown to Fig.6 (a).

  In the above-described embodiment, the gas separation device 100 is configured such that the mixed gas passes through the outside of the membrane element 14 and the target gas selectively separated by the membrane element 14 passes through the inside of the membrane element 14. Alternatively, the mixed gas may be introduced into the membrane element 14 so that the target gas passes through the casing 12. Specifically, the mixed gas is supplied from the main flow path portion (supply port) 22Aa of the flow path tube 22A, and the mixed gas is discharged from the main flow path portion (discharge port) 22Ba of the flow path tube 22B. Further, the sweep gas is introduced from the supply port (opening portion 20) of the casing 12, and the target gas selectively permeated through the membrane element 14 is led out from the discharge port (outlet portion: opening portion 21) of the casing 12.

  DESCRIPTION OF SYMBOLS 10 ... Module, 12 ... Casing, 14 ... Membrane element, 20, 21 ... Opening part (supply port, discharge port), 22A, 22B ... Channel pipe | tube (leading-out part, introduction part), 100 ... Gas separation apparatus.

Claims (3)

A tubular membrane element having a separation membrane that selectively permeates and separates a target gas from a mixed gas;
A tubular housing that houses the membrane element and has a supply port to which the mixed gas is supplied and a discharge port from which the mixed gas is discharged;
A module comprising: a deriving unit for deriving the target gas that has passed through the membrane element to the outside of the housing;
A plurality of the modules are connected,
In the connected module, the discharge port of the upstream module and the supply port of the downstream module are connected to communicate with each other,
The gas separation device, wherein the lead-out portion is provided in each of the plurality of modules.   The gas separation device according to claim 1, wherein a plurality of the membrane elements are arranged in the casing.   The gas separation according to claim 1 or 2, wherein the membrane element is connected to the lead-out portion at one end and an introduction portion into which a sweep gas is introduced at the other end. apparatus.

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