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WO2003086592A1 - Module de membranes a fibres creuses - Google Patents

Module de membranes a fibres creuses Download PDF

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Publication number
WO2003086592A1
WO2003086592A1 PCT/JP2003/004201 JP0304201W WO03086592A1 WO 2003086592 A1 WO2003086592 A1 WO 2003086592A1 JP 0304201 W JP0304201 W JP 0304201W WO 03086592 A1 WO03086592 A1 WO 03086592A1
Authority
WO
WIPO (PCT)
Prior art keywords
hollow fiber
fiber membrane
reverse osmosis
osmosis membrane
membrane module
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/JP2003/004201
Other languages
English (en)
Japanese (ja)
Inventor
Atsuo Kumano
Katsushige Marui
Hideto Kotera
Kouichi Baba
Makoto Marutani
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Toyobo Co Ltd
Original Assignee
Toyobo Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from JP2002101683A external-priority patent/JP2003290632A/ja
Priority claimed from JP2002101684A external-priority patent/JP2003290633A/ja
Application filed by Toyobo Co Ltd filed Critical Toyobo Co Ltd
Priority to AU2003220774A priority Critical patent/AU2003220774A1/en
Publication of WO2003086592A1 publication Critical patent/WO2003086592A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/02—Hollow fibre modules
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/02—Hollow fibre modules
    • B01D63/04—Hollow fibre modules comprising multiple hollow fibre assemblies
    • B01D63/043—Hollow fibre modules comprising multiple hollow fibre assemblies with separate tube sheets
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis

Definitions

  • the present invention relates to a hollow fiber membrane module comprising a selectively permeable hollow fiber membrane.
  • a hollow fiber membrane module Used for membrane separation of liquids, for example, reverse osmosis such as desalination of seawater, desalination of brine, purification of wastewater, production of sterile water, production of ultrapure water, advanced water purification treatment, pesticides, odor Removal of hazardous substances such as substances and disinfection by-product precursors, nanofiltration methods such as water softening by removing hardness components, recovery of paint from electrodeposition coating wastewater, and concentration of useful food-related substances Recovery, coagulation sedimentation ⁇ Sand filtration Ultrafiltration methods such as alternative water treatment, recovery of helium from natural gas, separation and recovery of hydrogen from ammonia plant purge gas, and carbonation in tertiary oil recovery
  • the present invention relates to a hollow fiber membrane module comprising a selectively permeable hollow fiber membrane that can be used for gas separation such as gas separation, oxygen enrichment, and nitrogen enrichment.
  • permselective membranes are classified according to the size of the substance to be separated.
  • types of membranes for liquid treatment include ultrafiltration membranes and microfiltration membranes that separate colloids and proteins, nanofiltration membranes that separate low molecular organic substances such as pesticides, and reverse osmosis that separates ions.
  • Reverse osmosis membranes are used under pressure higher than the osmotic pressure of the liquid to be treated, and in the case of seawater desalination, they are used at a pressure of several MPa.
  • the membrane shape of the permselective membrane includes a flat membrane type, a tubular membrane type, a spiral membrane type, and a hollow fiber membrane type.
  • the hollow fiber membrane type has a membrane area per unit volume of a membrane module. Since the shape is suitable for membrane separation operations, it is widely used, for example, in the field of seawater desalination using reverse osmosis membranes.
  • hollow fiber membrane modules have a structural Because of its simplicity and ease of manufacture, it is a so-called one-end open type, in which only one side of the hollow fiber membrane is open.
  • Various studies have been made on the structure of the membrane module depending on the intended performance and use conditions. For example, in JP-A-56-87405 and JP-B-60-37029, in the case of a reverse osmosis membrane, hollow fiber membranes are arranged in an intersecting manner around a supply water pipe so that a hollow fiber membrane is interposed.
  • the permeability of the supply liquid is made uniform, that is, the turbidity in the supply liquid is hardly clogged between the hollow fibers, the so-called excellent turbidity resistance effect,
  • concentration polarization can be suppressed without drift due to the flow. It also discloses the effect of suppressing the pressure loss that occurs when feed water flows through the hollow fiber membrane layer, the so-called module pressure loss.
  • the hollow fiber membranes are open at one end, so that the permeated water flows through the hollow part over a long distance, and the modules are arranged in parallel in parallel with the axis of the hollow fiber membrane module.
  • the hollow fiber membrane becomes longer, and the distance that the permeate flows through the hollow portion becomes further longer, so that there is a problem that the fluid pressure loss in the hollow portion becomes larger.
  • the flow pressure loss in the hollow part becomes large. If this flow pressure loss is large, the effective differential pressure of the membrane will decrease, the separation efficiency of the membrane will decrease, and the permeate volume may decrease.
  • Japanese Patent Publication No. 9-511447 discloses a hollow fiber membrane module in which both ends of a hollow fiber membrane are opened to reduce the flow pressure loss in the hollow part by shortening the distance that the permeate flows through the hollow part.
  • a structure has been proposed.
  • this hollow fiber membrane module has a problem that the hollow fiber membrane is arranged parallel to the length direction of the hollow fiber membrane module, so that drift is likely to occur, and when the recovery rate is increased, the performance is greatly reduced. is there. In other words, the ratio of the performance at a high recovery rate to the performance at a low recovery rate is small, and the recovery dependency is poor, which is a practical problem.
  • the outer peripheral side portion of the hollow fiber membrane is connected to the concentrated fluid outlet by a flow path.
  • a reverse osmosis membrane is a separation membrane in a region having a separation characteristic of a molecular weight of several tens of daltons. Specifically, it is capable of removing 90% or more of salt at an operating pressure of 0.5 MPa or more. .
  • Manipulation of hollow fiber type reverse osmosis membrane used for seawater desalination Since the pressure is large, the diameter of the hollow fiber membrane is generally small, and the flow pressure loss in the hollow portion tends to increase. Further, seawater, which is a fluid to be treated, has a high turbidity and a structure that does not cause clogging between the hollow fiber membranes is preferable, and is an example in which the effects of the present invention are easily obtained.
  • a test solution prepared by dissolving boron in a 35 g / L aqueous solution to a concentration of 4.5 mg / L was supplied to the reverse osmosis membrane module at a pressure of 5.4 MPa, a temperature of 25, and a pH of 7.0 to perform reverse osmosis treatment. Measure the boron removal rate (%) at a recovery rate of 15% after an hour. It is preferable that the boron removal rate when operating at a recovery rate of 15% is 55% or more. If the boron removal rate is not more than 55%, the guideline value of the boron concentration specified in the monitoring items for facilities that desalinate seawater etc. is 0.2 even if the pre-treatment or post-treatment of reverse osmosis membrane treatment is performed.
  • the water permeation amount of the reverse osmosis membrane module in the present invention is as follows: a salt concentration of 3.5% by weight and 4.5 mg L of hydrogen-containing water were treated with the reverse osmosis membrane module at a pressure of 5.4 MPa, a temperature of 25 and a pH of 7.0 a permeate flow after 2 hours of time, the set boss was recovery when there is 1 5%, 30%, each permeate flow in the case of 40% W 15, W 3 o , when the W 40
  • the relationship of 15 ⁇ 15 (m 3 / day) is satisfied from the viewpoint of good recovery rate dependency. More preferably, W 30 / W 15 ⁇ 0. 80 and, W 40 / W 15 ⁇ 0. 50 and is to a relationship of W 15 ⁇ 1 6 (m 3 / day). If the recovery dependence is out of this range, the recovery conditions actually used, for example, 30% And 40% decrease the water permeation etc., and it is necessary to enlarge the membrane module or increase the number of membrane modules, and it is necessary to increase the installation space of the equipment.
  • the water permeation amount W15 of the membrane module at a recovery of 15 % is low, the water permeation amount of the membrane module remains low even though the recovery rate is good, so the membrane module at a recovery of 15% It is preferable that the water permeability W15 has a value of 15 m 3 Z days or more in practical use.
  • the water permeation amount of the reverse osmosis membrane in the present invention refers to a per unit time, per unit membrane area when supply water having a salt concentration of 35 gZL and a temperature of 25 ° C is supplied to the reverse osmosis membrane at a pressure of 5.4 MPa. This is the amount of permeated water.
  • the effective length is about 1 m.
  • the recovery rate that is, the ratio between the amount of permeated water and the amount of supplied water is as small as 5% or less.
  • the water permeability is preferably at least 0.04 m 3 ( ⁇ 2 ⁇ day), more preferably at least 0.05 m 3 Z (m 2 'day). If the water permeation performance is low, the effect of the openings at both ends may not be fully exhibited because the flow pressure loss of the permeated water channel of the reverse osmosis membrane is small.
  • the pressure vessel according to the present invention is not particularly limited as long as it accommodates a hollow fiber membrane element and can give an effective pressure difference to the hollow fiber membrane and can perform a separation operation using the hollow fiber membrane.
  • the fluid does not leak to the outside, and the space on the supply side and the space on the permeation side of the hollow fiber membrane element, and the space on the permeation side and the space on the concentration side are separated fluid-tightly, and It must be able to secure.
  • the positions of the supply fluid inlet, the concentrated fluid outlet, and the permeate fluid outlet are not particularly limited, but are preferably located near the end of the pressure vessel from the viewpoint of efficient use in operation.
  • the winding angle in the present invention is the angle of the hollow fiber membrane with respect to the axial direction of the supply fluid distribution pipe.
  • the angle may be different between the inner layer and the outer layer of the hollow fiber membrane assembly.
  • the angle is preferably 5 to 70 degrees, more preferably 15 to 50 degrees. If this angle is too small, the hollow fiber membrane or the bundle of hollow fiber membranes is likely to collapse during winding, and it is difficult to secure the space between the hollow fiber membranes, making it difficult to achieve the original effect of the crossed arrangement. There is.
  • the effective length L (mm) of the hollow fiber membrane in the present invention is an average length between the openings of the hollow fiber membrane in a portion effectively acting on the separation operation of the hollow fiber membrane in the hollow fiber membrane module.
  • the inner diameter ID (mm) of the hollow fiber membrane is the average inner diameter of the hollow fiber membrane in a portion that effectively acts on the separation operation. If the effective length of the hollow fiber membrane is too long, the flow pressure loss in the hollow portion of the hollow fiber membrane may be too large. If the effective length is too short, the membrane area may be small and the effect of forming the double-ended type may be small.
  • the ratio LZID 2 of the square values of the effective length L (mm) and inner diameter ID of the hollow fiber membrane of the hollow fiber membrane calculated from these values (mm) is 3. 5 X 1 0 5 ( mm-i) above, 7. 0 X 1 0 5 ( mm-i) more preferably in the range, it is very effective to the open ends, more preferably 4.
  • FIG. 2 shows a case where two hollow fiber membrane elements are arranged in parallel connection.
  • the flow and structure of the fluid in the individual hollow fiber membrane elements 1 and 1 ' are basically the same as in FIG.
  • the two hollow fiber membrane elements 1 and 1 ′ are connected by an intermediate connector 16, a part of the supply fluid 12 is supplied to the hollow fiber membrane element 1, and the rest is hollow through the intermediate connector 16. It is supplied to the thread membrane element 1 '.
  • Both the concentrated fluids of the hollow fiber membrane elements 1 and 1 ′ are taken out from the concentrated fluid outlet 10.
  • the permeated fluid of the hollow fiber membrane elements 1, 1 ' is taken out from the respective permeated fluid outlets 11, 1, 1'.
  • a hollow fiber type reverse osmosis membrane composed of a cellulose triacetate membrane was prepared by a dry-wet spinning method.
  • the resulting hollow fiber membrane had an outer diameter of 120 tm and an inner diameter of 47 / zm.
  • the desalination performance of this hollow fiber membrane was measured with an effective length of about 1 m, the water permeability was 0.056 m 3 , (m 2 ⁇ day), the salt removal rate was 99.8%, and the boron removal rate was 6 2 %Met.
  • the measurement conditions were a supply pressure of 5.4 MPa, a temperature of 25, a salt concentration of 3.5% by weight, and a recovery rate of 2% or less.
  • the removal rate of salt and boron is defined by the following equation.
  • a hollow fiber type reverse osmosis membrane made of a cellulose triacetate membrane was produced by a dry-wet spinning method in the same manner as in Example 1.
  • the resulting hollow fiber membrane had an outer diameter of 1 37 (im, inner diameter of 53 im).
  • the desalination performance of this hollow fiber membrane was measured at a length of about 1 m, and the water permeability was 0.0. 6 lm 3 / (m 2 'day), salt removal rate 99.8%, boron removal rate 65%
  • the measurement conditions were the same as in Example I 1. The measurement was performed using this hollow fiber membrane.
  • a hollow fiber membrane element was fabricated in the same manner as in Made.
  • the outer diameter of the hollow fiber layer portion of this hollow fiber membrane element was 260 mm, and the axial length between the open ends was 1310 mm. The average effective length of the hollow fiber membrane was 1380 mm.
  • LLD was 5.0.
  • LZ ID 2 was 4. 9 X 1 0 5 (mm -i).
  • the performance of this hollow fiber membrane element was measured in the same manner as in Example 1-1.
  • the permeate flow rate was 37 m 3 / day, the salt removal rate was 99.5%, and the boron removal rate was 58%.
  • W 3 () ZW 15 is 0. 8 0, W 4. No Wi 5 was 0.55.
  • the hollow fiber membrane module was continuously operated with seawater after actual sand filtration, but no increase in module pressure loss caused by clogging between the hollow fiber membranes was observed.
  • the hollow fiber membrane module was continuously operated with seawater after actual sand filtration, but no increase in module pressure loss caused by clogging between the hollow fiber membranes was observed.
  • a hollow fiber membrane and a hollow fiber membrane element were produced in the same manner as in Example 1.
  • the two hollow fiber membrane elements thus obtained were mounted on a pressure vessel together with an intermediate connector to produce a double type module having a parallel arrangement as shown in FIG.
  • Reverse osmosis treatment was performed under the same conditions as in Example I-1.
  • the water permeation amount 5 and the boron removal rate at a recovery rate of 15% obtained in the same manner as in Example 1 were 100 m 3 / day and 60%, respectively.
  • W 30 W 15 is 0.80
  • 5 was 0.55.
  • Example 1 the hollow fiber membrane module was continuously operated with seawater after actual sand filtration, but no increase in module pressure loss caused by clogging between the hollow fiber membranes was observed. .
  • a hollow fiber membrane and a hollow fiber membrane element were produced in the same manner as in Example 1. Two hollow fiber membrane elements were attached to the pressure vessel together with the intermediate bulkhead to produce a double-type module arranged in series as shown in Fig. 3. Same as Example 11 Reverse osmosis treatment was performed under the same conditions. As a result, the permeate flow rate was 80 m 3 / day, the salt removal rate was 99.5%, and the boron removal rate was 55%. The water permeability W 15 and the boron removal rate at a recovery rate of 15%, determined in the same manner as in Example 1, were 100 m 3 Z days and 60%, respectively. Similarly, W 3. ZW 15 is 0. 8 0, W 4 () / W 15 was 0.5 5.
  • Example 1 the hollow fiber membrane module was continuously operated with seawater after actual sand filtration, but no increase in module pressure loss caused by clogging between the hollow fiber membranes was observed. .
  • a hollow fiber type reverse osmosis membrane made of a cellulose triacetate membrane was produced by a dry-wet spinning method in the same manner as in Example 1.
  • the resulting hollow fiber membrane had an outer diameter of 480 tm and an inner diameter of 185 / xm.
  • the measurement conditions are the same as in Example I-1.
  • Example 1 Using this hollow fiber membrane, a hollow fiber membrane element was produced in the same manner as in Example 1.
  • the outer diameter of the hollow fiber layer portion of this hollow fiber membrane element was 260 mm, and the axial length between the open ends was 131 mm.
  • the average effective length of the hollow fiber membrane was 1380 mm.
  • L LZD is 5. is 0, LZID 2 was 0. 4 X 1 0 5 (mnri ).
  • the performance of this hollow fiber membrane element was measured in the same manner as in Example 1.
  • Permeate flow rate is 1 2m 3 Bruno day, salt removal rate 9 9.5%, the boron removal rate was 5 8%.
  • Each water permeability 5 boron rejection in Example 1 1 determined in the same manner as meta recovery 1 5%, 1 4m 3 Z day, it was 6 2%.
  • W 3. W 15 is 0.80, 5 was 0.55.
  • the removal rate was high, the effective membrane area was small due to the small LZ ID 2 , and the amount of water permeated through the module
  • a double-ended hollow fiber element was produced in the same manner as in Example 1 except that the dimensions of the module were different.
  • the outer diameter of the hollow fiber layer portion of this hollow fiber membrane element was 115 mm, and the axial length between the open ends was 1900 mm.
  • the average effective length of the hollow fiber membrane was 200 Omm.
  • LLZD is 1 6.
  • LZ ID 2 was 9. 0 X 1 0 5 (mm -i).
  • One pressure vessel was attached, and reverse osmosis treatment was performed under the same conditions as in Example I-1. As a result, the permeate flow rate was 7.8 m 3 / day, the salt removal rate was 99.2%, and the boron removal rate was 46%.
  • the axial length between the open ends was 220 mm, and the axial length was 240 mm.
  • the average effective length of the hollow fiber membrane was 700 mm.
  • L LZD 1. is 1, L / ID 2 is 3. were 2 X 1 0 5 (mm- i).
  • One pressure vessel was attached, and reverse osmosis treatment was performed under the same conditions as in Example I-1. Consequently, permeate flow volume was 7. 2m 3 days, salt removal rate 9 9.5%, the boron rejection was 61%.
  • the water permeability at a recovery rate of 15 % and the boron removal rate at a recovery rate of 15 % were 9 m 3 / day and 65%, respectively, obtained in the same manner as Example 1. Similarly, W 3.
  • Example 1 Using this hollow fiber membrane, a hollow fiber membrane element was produced in the same manner as in Example 1.
  • the outer diameter of the hollow fiber layer portion of this hollow fiber membrane element was 260 mm, and the axial length between the open ends was 1310 mm.
  • the average effective length of the hollow fiber membrane was 1380 mm.
  • L LZD was 5.0.
  • LZ ID 2: 1. was 4 X 1 0 5 (mm- i).
  • the performance of this hollow fiber membrane element was measured in the same manner as in Example 1. Permeate flow rate is 1 4m 3 days, salt removal rate 99.1%, the boron rejection was 50%.
  • Each water permeability 5, the boron removal ratio in Example 1 1 determined in the same manner as meta recovery 1 5%, 1 1 m 3 day, was 53%. Likewise 5 0. 80, W 4 () W 15 was 0.55.
  • Table 1 shows the evaluation results of the modules obtained in the examples and the comparative examples.
  • Example 2 the hollow fiber membrane module was continuously operated with seawater after sand filtration, but no increase in module pressure loss caused by clogging between the hollow fiber membranes was observed. (Example 2 3)
  • a hollow fiber membrane and a hollow fiber membrane element were produced in the same manner as in Example 1. Two hollow fiber membrane elements were attached to the pressure vessel together with the intermediate bulkhead to produce a double-type module arranged in series as shown in Fig. 3. Reverse osmosis treatment was performed under the same conditions as in Example I-1. As a result, the permeated water flow rate was 74 m 3 days, the salt removal rate was 99.5%, and the boron removal rate was 58%. Under the same measurement conditions, the water permeability W 15 and the boron removal rate at a recovery rate of 15 % were 9 2 m 3 Z days, 62%. Similarly, the water permeation amount W 4 at the recovery rate of 40%.
  • a double-ended hollow fiber membrane element was produced in the same manner as in Example 1 except that the hollow fiber membrane was arranged parallel to the axis of the supply fluid distribution pipe. Since the hollow fiber membranes are arranged in parallel, the average effective length L of the hollow fiber membrane is 1 130 mm, and LZ ID 2 is 5.1 X 105 mm 1 .
  • the hollow fiber membranes are arranged in a cross shape and hold the space between the hollow fiber membranes, it is difficult to block the turbidity of the supplied fluid, and the pressure loss when passing through the hollow fiber membrane layer is kept low. Thus, drift in the hollow fiber membrane layer can be suppressed. In addition, concentration polarization on the surface of the hollow fiber membrane can be suppressed. Furthermore, since both ends of the hollow fiber membrane are open, the flow pressure loss in the hollow fiber membrane can be reduced as compared with the conventional one-end open type, and high permeability can be achieved. It is also possible to greatly improve the performance of removing boron, which is generally considered difficult to remove.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

La présente invention a trait à un module de membranes à fibres creuses, par exemple des membranes de fibres creuses en agencement entrecroisé dont les deux extrémités sont ouvertes, dans lequel le rapport (LL/D) de la longueur en direction axiale (LL) au diamètre extérieur (D) d'un ensemble de membranes de fibres creuses et le rapport (L/ID2) de la longueur efficace (L) au diamètre intérieur (ID) des membranes sont choisis de manière à se trouver au sein de plages déterminées. Le module de membranes à fibres creuses présente une activité inhibitrice élevée de la turbidité et une perméabilité hautement sélective vis-à-vis du fluide alimenté et, particulièrement dans le cas de membranes d'osmose inverse, et présente également une capacité élevée d'élimination du bore.
PCT/JP2003/004201 2002-04-03 2003-04-02 Module de membranes a fibres creuses Ceased WO2003086592A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU2003220774A AU2003220774A1 (en) 2002-04-03 2003-04-02 Hollow fiber membrane module

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
JP2002-101684 2002-04-03
JP2002101683A JP2003290632A (ja) 2002-04-03 2002-04-03 中空糸膜モジュール
JP2002-101683 2002-04-03
JP2002101684A JP2003290633A (ja) 2002-04-03 2002-04-03 中空糸膜モジュール

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WO2003086592A1 true WO2003086592A1 (fr) 2003-10-23

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1598105A4 (fr) * 2003-02-03 2006-03-01 Toyo Boseki Module a membranes de fibres creuses et agencement de tels modules
WO2016195535A1 (fr) * 2015-06-05 2016-12-08 Publichnoe Aktsionernoe Obschestvo "Gazprom" Module à membranes de séparation de gaz

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4080296A (en) * 1977-03-28 1978-03-21 The Dow Chemical Company Hollow fiber permeator
JPS57102201A (en) * 1980-12-18 1982-06-25 Toyobo Co Ltd Perm selective hollow fiber assembly
US5160042A (en) * 1991-11-05 1992-11-03 Praxair Technology, Inc. Double ended hollow fiber bundle and fluids separation apparatus
WO1996008306A1 (fr) * 1994-09-16 1996-03-21 E.I. Du Pont De Nemours And Company Cartouche a fibres creuses

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4080296A (en) * 1977-03-28 1978-03-21 The Dow Chemical Company Hollow fiber permeator
JPS57102201A (en) * 1980-12-18 1982-06-25 Toyobo Co Ltd Perm selective hollow fiber assembly
US5160042A (en) * 1991-11-05 1992-11-03 Praxair Technology, Inc. Double ended hollow fiber bundle and fluids separation apparatus
WO1996008306A1 (fr) * 1994-09-16 1996-03-21 E.I. Du Pont De Nemours And Company Cartouche a fibres creuses

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1598105A4 (fr) * 2003-02-03 2006-03-01 Toyo Boseki Module a membranes de fibres creuses et agencement de tels modules
WO2016195535A1 (fr) * 2015-06-05 2016-12-08 Publichnoe Aktsionernoe Obschestvo "Gazprom" Module à membranes de séparation de gaz
US9987596B2 (en) 2015-06-05 2018-06-05 Publichnoe Aktsionernoe Obschestvo “Gazprom” Membrane gas separation module

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