WO2006016575A1 - 高透水性中空糸膜型血液浄化器及びその製造方法 - Google Patents
高透水性中空糸膜型血液浄化器及びその製造方法 Download PDFInfo
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- WO2006016575A1 WO2006016575A1 PCT/JP2005/014568 JP2005014568W WO2006016575A1 WO 2006016575 A1 WO2006016575 A1 WO 2006016575A1 JP 2005014568 W JP2005014568 W JP 2005014568W WO 2006016575 A1 WO2006016575 A1 WO 2006016575A1
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- WIPO (PCT)
- Prior art keywords
- hollow fiber
- fiber membrane
- blood purifier
- blood
- mass
- Prior art date
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- 230000010534 mechanism of action Effects 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- UQPSGBZICXWIAG-UHFFFAOYSA-L nickel(2+);dibromide;trihydrate Chemical compound O.O.O.Br[Ni]Br UQPSGBZICXWIAG-UHFFFAOYSA-L 0.000 description 1
- 150000002826 nitrites Chemical class 0.000 description 1
- 239000012299 nitrogen atmosphere Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 229920005597 polymer membrane Polymers 0.000 description 1
- 229920000128 polypyrrole Polymers 0.000 description 1
- 229920005749 polyurethane resin Polymers 0.000 description 1
- 229920002451 polyvinyl alcohol Polymers 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
- 235000011164 potassium chloride Nutrition 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 229940079877 pyrogallol Drugs 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- GHMLBKRAJCXXBS-UHFFFAOYSA-N resorcinol Chemical compound OC1=CC=CC(O)=C1 GHMLBKRAJCXXBS-UHFFFAOYSA-N 0.000 description 1
- 229960001755 resorcinol Drugs 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 235000015067 sauces Nutrition 0.000 description 1
- 230000002000 scavenging effect Effects 0.000 description 1
- 238000006748 scratching Methods 0.000 description 1
- 230000002393 scratching effect Effects 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M sodium chloride Inorganic materials [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 235000009518 sodium iodide Nutrition 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- RPACBEVZENYWOL-XFULWGLBSA-M sodium;(2r)-2-[6-(4-chlorophenoxy)hexyl]oxirane-2-carboxylate Chemical compound [Na+].C=1C=C(Cl)C=CC=1OCCCCCC[C@]1(C(=O)[O-])CO1 RPACBEVZENYWOL-XFULWGLBSA-M 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical class [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
- 239000002344 surface layer Substances 0.000 description 1
- 230000003746 surface roughness Effects 0.000 description 1
- 208000024891 symptom Diseases 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 229920005992 thermoplastic resin Polymers 0.000 description 1
- 239000010409 thin film Substances 0.000 description 1
- KHPCPRHQVVSZAH-UHFFFAOYSA-N trans-cinnamyl beta-D-glucopyranoside Natural products OC1C(O)C(O)C(CO)OC1OCC=CC1=CC=CC=C1 KHPCPRHQVVSZAH-UHFFFAOYSA-N 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
- 238000004804 winding Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
- B01D69/02—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor characterised by their properties
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D67/00—Processes specially adapted for manufacturing semi-permeable membranes for separation processes or apparatus
- B01D67/0081—After-treatment of organic or inorganic membranes
- B01D67/009—After-treatment of organic or inorganic membranes with wave-energy, particle-radiation or plasma
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D67/00—Processes specially adapted for manufacturing semi-permeable membranes for separation processes or apparatus
- B01D67/0081—After-treatment of organic or inorganic membranes
- B01D67/0097—Storing or preservation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
- B01D69/08—Hollow fibre membranes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/66—Polymers having sulfur in the main chain, with or without nitrogen, oxygen or carbon only
- B01D71/68—Polysulfones; Polyethersulfones
-
- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61L—METHODS OR APPARATUS FOR STERILISING MATERIALS OR OBJECTS IN GENERAL; DISINFECTION, STERILISATION OR DEODORISATION OF AIR; CHEMICAL ASPECTS OF BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES; MATERIALS FOR BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES
- A61L2/00—Methods or apparatus for disinfecting or sterilising materials or objects other than foodstuffs or contact lenses; Accessories therefor
- A61L2/02—Methods or apparatus for disinfecting or sterilising materials or objects other than foodstuffs or contact lenses; Accessories therefor using physical phenomena
- A61L2/08—Radiation
- A61L2/081—Gamma radiation
-
- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61L—METHODS OR APPARATUS FOR STERILISING MATERIALS OR OBJECTS IN GENERAL; DISINFECTION, STERILISATION OR DEODORISATION OF AIR; CHEMICAL ASPECTS OF BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES; MATERIALS FOR BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES
- A61L2/00—Methods or apparatus for disinfecting or sterilising materials or objects other than foodstuffs or contact lenses; Accessories therefor
- A61L2/16—Methods or apparatus for disinfecting or sterilising materials or objects other than foodstuffs or contact lenses; Accessories therefor using chemical substances
- A61L2/18—Liquid substances or solutions comprising solids or dissolved gases
- A61L2/186—Peroxide solutions
-
- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61L—METHODS OR APPARATUS FOR STERILISING MATERIALS OR OBJECTS IN GENERAL; DISINFECTION, STERILISATION OR DEODORISATION OF AIR; CHEMICAL ASPECTS OF BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES; MATERIALS FOR BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES
- A61L2202/00—Aspects relating to methods or apparatus for disinfecting or sterilising materials or objects
- A61L2202/20—Targets to be treated
- A61L2202/24—Medical instruments, e.g. endoscopes, catheters, sharps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2323/00—Details relating to membrane preparation
- B01D2323/12—Specific ratios of components used
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2323/00—Details relating to membrane preparation
- B01D2323/30—Cross-linking
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2323/00—Details relating to membrane preparation
- B01D2323/34—Use of radiation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2325/00—Details relating to properties of membranes
- B01D2325/20—Specific permeability or cut-off range
Definitions
- the present invention relates to a medical highly permeable hollow fiber blood purifier having excellent safety and module assemblability, having high water permeability suitable for treatment of chronic renal failure, and a method for producing the same.
- a dialysis module using a hollow fiber membrane blood is usually flowed into the hollow portion of the hollow fiber, dialysate is flowed countercurrently to the outer portion, and urea and sauce are transferred by mass transfer based on diffusion from blood to dialysate.
- the main purpose is to remove low molecular weight substances such as achyun from the blood.
- dialysis complications have become a problem.
- substances to be removed by dialysis have a molecular weight of several thousand to a molecular weight of 10,000 to 20,000. Blood purification membranes are required to expand to high molecular weight substances and to remove these substances as well.
- ⁇ 2 microglobulin with a molecular weight of 11700 has been shown to be a causative agent of carpal tunnel syndrome and is a target for removal.
- the membrane In order to obtain a membrane used for the treatment of such high-molecular-weight substance removal, the membrane has a larger pore size, increased number of pores, increased porosity, membrane, etc. than conventional dialysis membranes. It is preferable to improve by increasing the water permeability of the membrane by reducing the thickness.
- the hydrophilic compound acts as a foreign substance during dialysis, and the hydrophilic compound is susceptible to deterioration such as light deterioration.
- the hydrophilic compound is susceptible to deterioration such as light deterioration.
- the problem of adversely affecting there is also a problem that when the hollow fiber membrane bundle is fixed to the module in the module assembly, the adhesion of the adhesive is inhibited.
- Patent Document 7 discloses a technique in which elution from a hollow fiber membrane of a hydrophilic polymer is 10 ppm or less in a hydrophobic polymer hollow fiber membrane containing a hydrophilic polymer.
- this technology does not give consideration to hemodiafiltration which requires higher pressure resistance and endotoxin exclusion than conventional hemodialysis.
- the content ratio, burst pressure, open area ratio, average pore area of the outer surface poly (vinylpyrrolidone) there is no specific description regarding the important uneven thickness and the burst pressure caused by the flaws.
- the hollow fiber membrane blood purifier is a medical device, it is preferable to perform a sterilization treatment to prevent the growth of various bacteria. Incomplete sterilization can lead to problems with the endotoxins described above.
- formalin, ethylene oxide gas, high-pressure steam sterilization, radiation such as ⁇ -rays, or electron beam irradiation sterilization methods are used, and each exhibits a specific effect.
- the sterilization method using radiation or electron beam irradiation can treat the workpiece in the packaged state and has excellent sterilization effect. Therefore, it is preferable.
- Adhesives and the like used for fixing hollow fiber membranes for blood purifiers are deteriorated by radiation or electron beam irradiation, and a method of sterilizing while preventing deterioration has been proposed.
- a method is known in which the hollow fiber membrane is kept in a wet state to prevent deterioration of the hollow fiber membrane due to ⁇ -ray irradiation (see, for example, Patent Document 8).
- Patent Document 8 it is necessary to keep the hollow fiber membrane in a wet state, so that the weight of the blood purifier is naturally increased, and transportation and handling are inconvenient, particularly in cold regions.
- the water filled in the blood purifier freezes, causing problems such as rupture and damage of the hollow fiber membrane. Furthermore, it has high cost factors such as preparation of sterilized water.
- the hollow fiber membrane is in a wet state where bacteria can easily propagate, it is conceivable that the bacteria will propagate even in a short time until sterilization after packaging.
- the blood purifier manufactured in this way is preferable because it takes a long time to obtain a completely sterilized state, which leads to higher costs or safety problems.
- a method for avoiding the above-mentioned wet state and suppressing deterioration due to radiation irradiation a method is known in which a hollow fiber membrane contains a sterilizing protective agent such as glycerin or polyethylene glycol and is irradiated with ⁇ rays in a dry state.
- a sterilizing protective agent such as glycerin or polyethylene glycol
- Patent Document 9 a sterilizing protective agent
- Patent Document 10 As a method for solving the above-mentioned problems, there is a method of sterilizing by irradiating radiation in a state where the moisture content of the hollow fiber membrane is 5% by mass or less and the relative humidity in the vicinity of the hollow fiber membrane is 40% or less. It is known (see, for example, Patent Document 10). In this method, the above-mentioned problems have been solved, and the ultraviolet absorbance at a wavelength of 220 350 measured according to the dialysis membrane elution test in the artificial kidney device manufacturing approval standard satisfies the standard value of 0.1 or less. ing. However, the method described in Patent Document 10 focuses on decomposition and deterioration only during sterilization, and should be mentioned for long-term storage stability.
- the insoluble component of the membrane material is 10% by mass or less by performing ⁇ -ray irradiation in a state where the moisture content of the hollow fiber membrane is 10% by mass or less.
- Patent Document 11 mentions that it can be achieved that the amount of the hydrophilic polymer per lm 2 of the membrane contact side of the membrane extracted with 40% ethanol aqueous solution is 2. Omg / m 2 or less. ing.
- Patent Document 11 attention is paid to decomposition and deterioration only during sterilization, and long-term storage stability is mentioned.
- Patent Documents 15 and 16 describe a hollow fiber membrane blood purifier that does not use a filling liquid, in which the inside of the hollow fiber membrane blood purifier has an inert gas atmosphere, so that the elution of hydrophilic polymer is small. Is disclosed. However, because the oxygen concentration during sterilization is high or the importance of humidity in the atmosphere has not been studied, peroxides typified by hydrogen peroxide are generated by radiation sterilization, and long-term storage stability is improved. There was a problem in lacking.
- Patent Document 1 Japanese Patent Application Laid-Open No. 2000-107577
- Patent Document 2 Japanese Patent Laid-Open No. 2000-254222
- Patent Document 3 Japanese Patent Laid-Open No. 2001-190934
- Patent Document 4 Japanese Patent No. 3193262
- Patent Document 5 Japanese Patent Laid-Open No. 2001-38170
- Patent Document 6 Japanese Unexamined Patent Publication No. 2000-140589
- Patent Document 7 Japanese Unexamined Patent Publication No. 2001-170171
- Patent Document 8 Japanese Patent Publication No. 55-23620
- Patent Document 9 JP-A-8-168524
- Patent Document 10 Japanese Unexamined Patent Publication No. 2000-288085
- Patent Document 11 Japanese Patent Laid-Open No. 2001-205057
- Patent Document 12 Japanese Patent Application Laid-Open No. 62-74364
- Patent Document 13 Japanese Patent Laid-Open No. 62-204754
- Patent Document 14 W098Z58842
- Patent Document 15 Japanese Patent Application Laid-Open No. 2001-170167
- Patent Document 16 Japanese Patent Laid-Open No. 2003-245526
- An object of the present invention is to provide a medical hollow fiber blood purifier excellent in safety and module assemblability and having high water permeability suitable for treatment of chronic renal failure, and a method for producing the same.
- the present invention relates to a hydrophobic polymer hollow fiber membrane containing a hydrophilic polymer, wherein the content of the hydrophilic polymer on the outer surface of the hollow fiber membrane is 25 to 50% by mass, and the outer surface is open.
- the water permeability of the vessel is 150 to 2000 mlZm 2 ZhrZmmHg, the oxygen concentration in the ambient atmosphere of the hollow fiber membrane is 0.001% or more and 0.1% or less, and the water content is 0.
- the present invention relates to a highly permeable hollow fiber membrane blood purifier characterized by being irradiated with radiation in a state of 2 mass% or more and 7 mass% or less.
- the present invention also relates to a method for producing a highly water-permeable hollow fiber membrane blood purifier comprising irradiation with radiation as described above.
- the invention's effect is a method for producing a highly water-permeable hollow fiber membrane blood purifier comprising irradiation with radiation as described above.
- the hollow fiber blood purifier of the present invention is excellent in safety and module assembly, and is suitable as a medical hollow fiber blood purifier having high water permeability suitable for treatment of chronic renal failure. .
- the hollow fiber membrane used in the present invention is characterized in that it is composed of a hydrophobic polymer containing a hydrophilic polymer.
- the material of the hydrophobic polymer in the present invention include, for example, regenerated senorelose, senorelose acetate, senorelose coconut resin such as senorelose triacetate, polysulfone rosin such as polysulfone and polyethersulfone, polyacrylonitrile, polymethylmethacrylate. Examples thereof include tallylate and ethylene butyl alcohol copolymer.
- a cellulose-based resin or a polysulfone-based resin which can easily obtain a hollow fiber having a water permeability of 150 mLZm 2 ZhrZmmHg or more, is preferable.
- a cenololose diacetate or a cenololose triacetate is preferred.
- the hydrophilic polymer used in the present invention is not particularly limited, but those capable of forming a micro phase separation structure in a solution with a hydrophobic polymer are preferably used.
- Specific examples include polyethylene glycol, polyvinyl alcohol, carboxymethyl cellulose, and polypyrrole pyrrolidone. From the viewpoints of safety and economy, it is preferable to use polyvinylbi-lidone.
- the content of the hydrophilic polymer in the membrane with respect to the hydrophobic polymer is not particularly limited as long as it is in a range that can provide sufficient hydrophilicity and high water content to the hollow fiber membrane. It is preferable that the force is 0 to 99% by mass and the hydrophilic polymer is 1 to 20% by mass. If the content of the hydrophilic polymer relative to the hydrophobic polymer is too small, the hydrophilicity-imparting effect of the film may be insufficient. Therefore, the content is more preferably 2% by mass or more. On the other hand, if the content is too high, the effect of imparting hydrophilicity is saturated and the amount of hydrophilic polymer dissolved out from the membrane increases. May exceed.
- the amount of elution of the hydrophilic polymer from the hollow fiber membrane is 10 ppm or less. If the elution amount exceeds lOppm, side effects and complications may occur due to long-term dialysis due to the eluted hydrophilic polymer.
- the method for satisfying the characteristics is not limited, and can be achieved, for example, by setting the content of the hydrophilic polymer relative to the hydrophobic polymer within the above range or optimizing the film forming conditions of the hollow fiber membrane.
- a more preferred hydrophilic polymer elution amount is 8 ppm or less, more preferably 6 ppm or less, and particularly preferably 4 ppm or less.
- the amount of hydrophilic polymer eluted is preferably zero, but when the amount of hydrophilic polymer eluted is zero, the degree of hydrophilicity of the blood contact surface decreases, Blood compatibility may be reduced. Therefore, the elution amount of hydrophilic polymer seems to be within the allowable range of about 0.1 ppm.
- the hydrophilic polymer is insolubilized by crosslinking.
- the crosslinking method and the degree of crosslinking are not limited. Examples of the crosslinking method include ⁇ -rays, electron beams, thermal crosslinking, and chemical crosslinking. Among them, residues such as initiators do not remain and ⁇ Cross-linking with a wire or an electron beam is preferred.
- degassed RO water means RO water heated to room temperature to 50 ° C. and stirred for 15 minutes to 2 hours in a reduced pressure of 500 to 750 mmHg. If water that has not been degassed is used, the dissolved oxygen in the water may cause deterioration of the membrane material and increase the amount of eluate.
- the insoluble matter relates to the solubility when the crosslinked membrane is immersed in dimethylformamide. That is, the cross-linked film 1. Og is taken, dissolved in 100 ml of dimethylformamide and visually inspected for the presence or absence of insoluble matter.
- the filling liquid is first drained, then pure water is poured into the dialysate side channel at 500 mL for 5 minutes, and then the pure water is similarly poured into the blood side channel. Run for 5 minutes at 200mLZmin. Most Later, 200 mLZmin of pure water is passed through the membrane so that it passes through the membrane from the blood side to the dialysate side.
- the hollow fiber membrane is taken out from the obtained module and freeze-dried to make a sample for measuring insoluble components. In the case of a dry blood purifier, the same washing process is performed to obtain a measurement sample.
- the content force S of the above-described hydrophilic polymer on the outer surface of the hollow fiber membrane is S25 to 50% by mass.
- the content of the hydrophilic polymer on the outer surface is too low, the content of the hydrophilic polymer on the entire membrane, particularly the inner surface of the membrane, becomes too low, and blood compatibility and permeation performance may deteriorate.
- the priming property may be lowered.
- a hemodialyzer is used for blood purification therapy, it is necessary to perform wetting and defoaming by allowing physiological saline or the like to flow inside and outside the hollow fiber membrane of the hemodialyzer.
- the roundness of the hollow fiber membrane, the crushing of the end, deformation, and the hydrophilicity of the membrane material are thought to affect the priming properties.
- the hydrophilic / hydrophobic balance of the hollow fiber membrane greatly affects the priming property. Therefore, the more preferable content of the hydrophilic polymer is 27% by mass or more, and further preferably 30% by mass or more. If the content of hydrophilic polymer on the outer surface is too high, endotoxin (endotoxin) contained in the dialysate may enter the blood, causing side effects such as fever or drying the membrane.
- the hydrophilic polymer present on the outer surface of the membrane intervenes and the hollow fiber membranes stick together (adhere), which may cause problems such as poor module assembly. Therefore, the more preferable content is 47% by mass or less, and further preferably 45% by mass or less.
- Examples of the method for setting the content of the hydrophilic polymer on the outer surface of the hollow fiber membrane in the above-described range include, for example, setting the content of the hydrophilic polymer relative to the hydrophobic polymer in the above-described range,
- the film forming conditions of the hollow fiber membrane are optimized. It is also an effective method to wash the formed hollow fiber membrane.
- Examples of the film forming method include adjusting the humidity of the air gap portion at the nozzle outlet, stretching conditions, the temperature of the coagulation bath, and the composition ratio of the solvent and the non-solvent in the coagulation liquid. As washing methods, warm water washing, alcohol washing, centrifugal washing and the like are effective.
- the air gap portion is surrounded by a member for blocking outside air.
- Air gap The internal humidity is preferably adjusted by the composition of the spinning dope, the nozzle temperature, the air gap length, the temperature of the external coagulation bath, and the composition.
- polyethersulfone Z polyvinylpyrrolidone Z dimethylacetamide RO water 10 to 25 ZO. 5 to 12.5 / 52.5 to 59.5 to 89.5 / 0 to 10.0
- the absolute humidity of the air gap is 0. 01-0. 3kg / kg dry air.
- the internal coagulation liquid a 0 to 80 mass% dimethylacetamide (DMAc) aqueous solution is preferable. If the concentration of the internal coagulating liquid is too low, the dense layer on the inner surface of the hollow fiber membrane becomes thick, which may reduce the solute permeability.
- the concentration of the internal coagulation liquid is more preferably 15% by mass or more, further preferably 25% by mass or more, and particularly preferably 30% by mass or more. In addition, if the concentration of the internal coagulating liquid is too high, the dense layer may be incompletely formed and the fractionation characteristics may deteriorate immediately.
- the concentration of the internal coagulating liquid is more preferably 70% by mass or less, further preferably 60% by mass or less, and particularly preferably 50% by mass or less.
- the external coagulation liquid concentration is more preferably 40% by mass or less, further preferably 30% by mass or less, and particularly preferably 25% by mass or less. If the concentration of the external coagulation liquid is too low, a large amount of water needs to be used to dilute the solvent brought in from the spinning stock solution, which may increase the cost for waste liquid treatment. Therefore, the lower limit of the external coagulation liquid concentration is more preferably 3% by mass or more, and further preferably 5% by mass or more.
- stretching is not substantially applied before the hollow fiber membrane structure is completely fixed.
- the fact that the film is not substantially stretched means that the spinning solution discharged from the nozzle is not loosened or excessively tensioned. It means controlling the speed. Discharge linear speed Z Ratio of coagulation bath first roller speed
- the draft ratio is preferably in the range of 0.7 to 1.8. If the draft ratio is too low, the traveling hollow fiber membrane may become slack and lead to a decrease in productivity. Accordingly, the draft ratio is more preferably 0.8 or more, more preferably 0.9 or more, and particularly preferably 0.95 or more. When the draft ratio is too large, the membrane structure may be destroyed, for example, the dense layer of the hollow fiber membrane is torn. Therefore, the draft ratio is more preferably 1.7 or less, further preferably 1.6 or less, particularly preferably 1.5 or less, and most preferably 1.4 or less. By adjusting the draft ratio within this range, pore deformation and destruction can be prevented, and clogging of blood proteins into the membrane pores can be prevented. As a result, performance stability over time and sharp fractionation characteristics can be expressed.
- the hollow fiber membrane that has passed through the washing bath is wound up in a wet state to make a bundle of 3,000-20,000.
- the obtained hollow fiber membrane bundle is washed to remove excess solvent and hydrophilic polymer.
- the hollow fiber membrane bundle is treated by immersing it in hot water at 70 to 130 ° C, or at room temperature to 50 ° C, 10 to 40 vol% ethanol or isopropanol aqueous solution. I prefer to do it.
- the hollow fiber membrane bundle immersed in excess RO water in the pressurized container can be treated at 121 ° C for about 2 hours.
- the content of the above-mentioned hydrophilic polymer on the surface of the hollow fiber membrane surface was measured and calculated by the ESCA method as described below, and the content of the surface layer of the surface of the hollow fiber membrane (surface force) The absolute value of the content of the depth of several A to several tens of A) is obtained.
- the ESCA method (outermost layer) can measure the hydrophilic polymer (PVP) content up to about 10 100A deep from the hollow fiber membrane surface.
- the burst pressure of the hollow fiber membrane housed in the blood purifier is 0.5 MPa or more, and the water permeability of the blood purifier is 150 mlZm 2 ZhrZmmHg or more. If the burst pressure is too low, it will not be possible to detect potential defects that can lead to blood leaks as described below. On the other hand, if the water permeability is too low, the dialysis efficiency decreases. To increase dialysis efficiency, it is effective to increase the pore size or increase the number of pores, but this tends to cause problems such as a decrease in membrane strength and defects.
- the porosity of the support layer is optimized by optimizing the pore diameter of the outer surface, and the solute permeation resistance and membrane strength are balanced.
- a more preferable range of water permeability is 200 mlZm 2 ZhrZmmHg or more, more preferably 300 mlZm 2 ZhrZmmHg or more, particularly preferably 400 mlZm 2 ZhrZmmHg or more, and most preferably 500 mlZm 2 ZhrZmmHg or more.
- 2000 mlZm 2 ZhrZmmHg or less is preferable.
- it is 1800 mlZm 2 ZhrZmmHg or less, more preferably 1500 mlZm 2 ZhrZmmHg or less, particularly preferably 1300 mlZm 2 ZhrZmmHg or less, particularly preferably lOOOOmlZ m 2 ZhrZmmHg or less.
- the present inventors examined the physical properties of a hollow fiber membrane suitable for use in a blood purifier.
- the blood purifier performs a leak test in which the inside or outside of the hollow fiber membrane is pressurized with air in order to confirm defects in the hollow fiber membrane or module at the final stage of production.
- a leak is detected by pressurized air, the module is discarded as defective or the defect is repaired.
- the air pressure for this leak test is often several times the guaranteed pressure of a hemodialyzer (usually 500 mmHg). With particularly high water permeability
- microscopic scratches, crushing, and tears in the hollow fiber membrane that cannot be detected by the normal pressure leak test are the manufacturing process (mainly sterilization and packaging) and transportation after the leak test.
- the hollow fiber membrane is cut and pinholes are generated during handling in the process or clinical setting (unpacking, priming, etc.), and as a result, blood leaks during treatment. They found out.
- potential yarn defects that lead to the breakage of hollow fiber membranes and the occurrence of pinholes during clinical use cannot be detected by pressure in normal pressurized air leak tests, and are higher.
- the inventors have found that pressure is required and that suppressing the occurrence of uneven thickness of the hollow fiber membrane is effective for suppressing the occurrence of the above-described potential defects, and have led to the present invention.
- the burst pressure in the present invention is an index of the pressure resistance performance of a hollow fiber membrane that has a hollow fiber as a module, and pressurizes the inside of the hollow fiber membrane with gas and gradually increases the pressure. This is the pressure when the hollow fiber membrane bursts without being able to withstand the internal pressure.
- the burst pressure is preferably 2. OMPa or less. More preferably, it is 1.7 MPa or less, more preferably 1.5 MPa or less, particularly preferably 1.3 MPa or less, particularly preferably 1. OMPa or less.
- the present invention is based on the knowledge that the safety of hollow fiber membranes in long-term dialysis cannot be sufficiently proved by the blood leak characteristics that are governed by the conventionally known macro characteristics such as membrane strength. Based on this. In other words, in order to ensure the safety of blood leaks during long-term dialysis, in addition to macro characteristics, the establishment of an evaluation method that includes the above-mentioned defects due to potential defects! The invention has been completed.
- the thickness deviation in the present invention is a deviation in film thickness when 100 cross sections of hollow fiber membranes in a blood purifier are observed, and is expressed as a ratio between a maximum value and a minimum value.
- the minimum thickness deviation of 100 hollow fibers is 0.6 or more. Even one of the 100 hollow fibers is biased If hollow fibers with a wall thickness of less than 0.6 are included, the hollow fibers may cause a leak during clinical use. Therefore, the uneven wall thickness of the present invention represents the minimum value of 100 fibers, which is not an average value. . Higher unevenness increases the uniformity of the film, suppresses the appearance of latent defects, and improves the burst pressure. Therefore, it is more preferably 0.7 or more, more preferably 0.8 or more, and particularly preferably 0. More than 85. If the uneven thickness is too low, the burst pressure becomes low as soon as latent defects become apparent, and blood leaks easily occur.
- the thickness of the hollow fiber membrane is 10 m or more and 60 m or less. If the film thickness is too large, the permeability of the medium to high molecular weight substance having a low movement speed may be lowered even if the water permeability is high. The thinner the film thickness is, the higher the material permeability is, and 55 m or less is more preferable, 50 m or less is more preferable, and particularly preferably 47 m or less. On the other hand, if the film thickness is too small, the film strength is low, and the burst pressure may be low even if the thickness deviation is 0.6 or more. Therefore, the film thickness is more preferably 20 m or more, more preferably 25 ⁇ m or more, particularly preferably 30 ⁇ m or more, and most preferably 35 ⁇ m or more.
- the hollow fiber membrane in the present invention can be suitably used as a hollow fiber membrane for blood purification, and in particular, a hollow fiber membrane suitable for the treatment of patients with renal failure, such as blood dialysis, hemodiafiltration and blood filtration. It is preferable.
- a solution in which a blend of a hydrophobic polymer and a hydrophilic polymer having the above-described composition is dissolved in a solvent that dissolves the blend is preferably produced by a dry and wet method.
- burst pressure In order to set the burst pressure to 0.5 MPa or more, it is effective to set the uneven thickness of the hollow fiber membrane to 0.6 or more as described above. In order to make the thickness deviation 0.6 or more, for example, it is preferable to make the slit width of the nozzle that is the discharge port of the film forming solution strictly uniform.
- a hollow fiber membrane spinning nozzle is generally a tube-in-orifice type nozzle having an annular portion for discharging a spinning raw solution and a core liquid discharge hole serving as a hollow forming agent inside thereof.
- the slit width refers to the width of the outer annular portion that discharges the spinning dope. By reducing the variation in the slit width, uneven thickness of the spun hollow fiber membrane can be reduced.
- the ratio between the maximum value and the minimum value of the slit width should be 1.00 or more and 1.11 or less, and the difference between the maximum and minimum values should be 10 m or less, preferably 7 m or less. More preferably 5 m or less, particularly preferably 3 ⁇ m or less.
- the nozzle temperature is optimized.
- the nozzle temperature is preferably 20-100 ° C. If the nozzle temperature is too low, it is easily affected by the room temperature, the nozzle temperature is not stable, and the discharge stock of the spinning stock solution may occur. Therefore, the nozzle temperature is more preferably 30 ° C or higher, more preferably 35 ° C or higher, even more preferably 40 ° C or higher. In addition, if the nozzle temperature is too high, the viscosity of the spinning dope becomes too low and ejection may not be stable, or the thermal degradation or decomposition of the hydrophilic polymer may proceed. Therefore, the nozzle temperature is more preferably 90 ° C. or less, further preferably 80 ° C. or less, and particularly preferably 70 ° C. or less.
- the guide to be used has a surface that has been subjected to surface strength or knurled to avoid contact resistance with the hollow fiber membrane as much as possible.
- the contact surface force with the hollow fiber membrane does not directly insert the hollow fiber membrane bundle into the module container.
- the hollow fiber membrane wound with a satin-finished film It is preferable to use a method in which a bundle is inserted into a module container and the module container force is extracted from only the film.
- the spinning dope is preferably filtered using a filter having a pore size smaller than the thickness of the hollow fiber membrane.
- the uniformly melted spinning solution is passed through a sintered filter having a pore diameter of 10 to 50 m provided while the dissolving tank force is also led to the nozzle.
- the filtration process may be performed at least once, but the ability to perform the filtration process in several stages is preferable in order to increase the filtration efficiency and filter life.
- the pore size of the filter is more preferably 10 to 45 ⁇ m, more preferably 10 to 40 m force S, and even more preferably 10 to 35 m force S. Filter hole diameter is If it is too small, the back pressure will increase, and the quantitativeness of the discharge of the spinning dope may be reduced.
- the method for suppressing the mixing of bubbles it is effective to defoam a polymer solution for film formation.
- Static defoaming or vacuum defoaming can be used. Specifically, after the pressure in the dissolution tank is reduced to 1-100-1750 mmHg, the tank is sealed and allowed to stand for 5-30 minutes. This operation is repeated several times to perform a defoaming process. If the degree of decompression is too low, the treatment may take a long time because it is necessary to increase the number of defoaming times. On the other hand, when the degree of vacuum is too high, the cost for increasing the degree of sealing of the system may increase.
- the total treatment time is preferably 5 minutes to 5 hours. If the treatment time is too long, the hydrophilic polymer may be decomposed and deteriorated due to the effect of reduced pressure. If the treatment time is too short, the defoaming effect may be insufficient.
- the porosity of the outer surface of the hollow fiber membrane is 8 to 25%, and the average pore area of the apertures on the outer surface of the hollow fiber membrane is 0.3 to 1. 0 m 2 is effective and preferable for imparting the above-mentioned characteristics. If the porosity is too small, the water permeability may decrease. Further, when the membrane is dried, the hollow polymer membranes are fixed to each other due to the presence of a hydrophilic polymer existing on the outer surface of the membrane, which may cause problems such as poor module assembly. Therefore, the open area ratio is more preferably 9% or more, more preferably 10% or more.
- the average pore area is more preferably 0.4 m 2 or more, more preferably 0.5 m 2 or more, still more preferably 0.6 m 2 or more.
- the porosity is preferably 23% or less, more preferably 20% or less, even more preferably 17% or less, and most preferably 15% or less.
- the average pore area is preferably 0.95 m 2 or less, more preferably 0.90 m 2 or less.
- the composition ratio of the hydrophobic polymer and the hydrophilic polymer in the spinning dope is set to 95. : 5 to 67:33, the condition of the external coagulation liquid is adjusted to 5 to 40% by mass, or hot water washing or alcohol washing is performed after film formation.
- the hollow fiber membrane of the present invention has a high water permeability (that is, a pore size of the membrane) by making the hydrophilic high molecular weight of the outer surface within a specific range, and making the membrane surface porosity and pore area a specific range. Even in hollow fiber membranes (large and high porosity), there is no leak when using blood filtration or hemodiafiltration, and both solute removal and safety, which suppresses the entry of foreign substances into the blood, are compatible in both dimensions. It is a thing.
- the eluate measurement here is for the purpose of confirming the ultraviolet absorbance specified in the dialysis-type artificial kidney device manufacturing approval standard, the elution test of the circuit in the dialysis-type artificial kidney device manufacturing approval standard, and long-term storage stability. The measurement was carried out in accordance with the measurement of the hydrogen peroxide concentration representative of peroxide.
- oxygen, nitrogen, and an inert gas can be used, and if this method is limited, oxygen concentration can be reduced by using a deoxidizer in a sealed system. It was possible to reduce this. Since it takes a chemical reaction for the oxygen in the system to react with the oxygen scavenger after enclosing the oxygen scavenger, it takes time. The chemical reaction proceeds stochastically faster when the oxygen concentration in the system is high, but the force is stochastically delayed as the oxygen concentration decreases. In order to achieve the oxygen concentration as proposed in the present invention, it is preferable to leave at room temperature for 10 hours or more, more preferably 18 hours or more, and even more preferably 24 hours or more.
- Oxygen concentration during irradiation is 0.001% or more 0 1% or less is preferable, and more preferably 0.003% or more and 0.05% or less in consideration of the stability of the eluate.
- the water content of the hollow fiber membrane is preferably 7% by mass or less in order to ensure adhesion to a resin sealed when assembling the blood purifier, such as urethane resin. In order to ensure productivity, 6% by mass or less is more preferable, and 5% by mass or less is more preferable. Under normal temperature and normal pressure where the hollow fiber membrane can be substantially observed, the equilibrium moisture content was around 2% by mass.
- the moisture content region of the hollow fiber membrane of 2% by mass or more the water content of the hollow fiber membrane seems to suppress the generation of free radicals, but the generation of peroxide can be suppressed. It was. However, in order to improve productivity, it is possible to control the moisture content at the end of drying to 2% to 7% by weight in order to suppress adhesiveness and peroxides, but it is possible to control the weight. Since there is still room for improvement, further studies were conducted. As a result, even if the moisture content of the hollow fiber membrane itself is less than 2% by mass, it will be peroxidized if the relative humidity at the ambient air force around 25 ° C at the time of irradiation is greater than 40% RH. We found that the amount of products can be reduced.
- the amount of peroxide produced is reduced because the moisture in the air reacts with radiation and the radiation cannot directly attack the polymer that forms the membrane. It can be inferred that the water content during radiation sterilization becomes a buffer for free radical attacks by irradiation.
- the amount of peroxyacid can be stably reduced even if the moisture content of the hollow fiber membrane is less than 2% by mass. Therefore, although it can be considered that sterilization is possible even when the moisture content is substantially 0% by mass, 0.2% by mass or more is preferable in terms of a substantially dry state, which improves productivity, reduces running costs, etc. 0.5 mass% or more is more preferable. 1 mass% or more is a more preferable embodiment.
- the packaging material used for the bag is preferably oxygen permeability and low Z or water vapor permeability at least oxygen permeability lcm 3 / (m 2 '24hr'atm) (20 ° C, 90% RH ) Or less and water vapor permeability of 5 g / (m 2 '24hr'atm) (40 ° C., 90% RH) or less is preferable for the purpose of the present invention.
- oxygen permeability and low Z or water vapor permeability at least oxygen permeability lcm 3 / (m 2 '24hr'atm) (20 ° C, 90% RH ) Or less and water vapor permeability of 5 g / (m 2 '24hr'atm) (40 ° C., 90% RH) or less is preferable for the purpose of the present invention.
- substitution with an inert gas as described above or use of an oxygen scavenger is preferred.
- oxygen scavenger that can be used in the present invention, it is preferable to use an oxygen scavenger that has a function of releasing moisture as well as a function of deoxidizing.
- functional agents that exhibit a deoxygenation function include sulfites, bisulfites, nitrites, hydroquinones, catechol, resorcin, pyrogallol, gallic acid, longgarite, which are used as general-purpose oxygen absorbers.
- Ascorbic acid and / or a salt thereof, sorbose, glucose, capita, dibutylhydroxytoluene, dibutylhydroxylazole, ferrous salt, iron powder, and other metal powders can be used, and can be appropriately selected from these.
- an oxygen scavenger for the main component of metal powder as an oxygen scavenger for the main component of metal powder, as an oxidation catalyst, salt sodium chloride, potassium chloride, magnesium chloride, salt calcium, salt aluminum, ferrous chloride, ferrous chloride Metals such as ferric, sodium bromide, potassium bromide, magnesium bromide, calcium bromide, iron bromide, nickel bromide, sodium iodide, potassium iodide, magnesium iodide, calcium iodide, iron iodide You can choose one or more of halogenated compounds.
- a porous carrier such as a moisture releasing oxygen scavenger (for example, Ageless (R) Z-200PT manufactured by Mitsubishi Gas Chemical Co., Ltd.) or zeolite powder impregnated with moisture is used.
- the method of bundling can be preferably adopted.
- the shape of the oxygen scavenger is not particularly limited. For example, it may be any of powder, granule, lump, and sheet, and a sheet in which various oxygen absorbent compositions are dispersed in thermoplastic resin. It can be an oxygen scavenger in the form of a film or film!
- the oxygen scavenging time is extended for the purpose of ensuring the humidity around the hollow fiber membrane. It is also possible to optimize the length and increase of storage temperature.
- the water content of the hollow fiber membrane is 0.2 mass% or more and 7 mass% or less, and preferably the humidity around the hollow fiber membrane is higher than 40% RH. It is possible to advantageously reduce the peroxidic acid represented by
- Peroxides represented by hydrogen peroxide affect the long-term storage stability of blood purifiers.
- the peroxidic acid in the blood purifier expands its chemical reaction while attacking the polymer constituting the membrane by chemical reaction accompanied by free radicals with time. Therefore, the amount of hydrogen peroxide extracted from the hollow fiber membrane immediately after radiation sterilization is low, but it is obvious that the amount of hydrogen peroxide extracted from the hollow fiber after 3 months from the implementation of radiation sterilization. ⁇
- Less than lOppm of hydrogen is preferred to ensure sufficient stability for six months, one year, and three years, which is generally the warranty period for blood purifiers. 8ppm or less is preferable and 5ppm or less is more preferable for safer guarantee.
- the amount of hydrogen peroxide extracted from the hollow fiber membrane after 3 months from irradiation is 10 ppm, at least thereafter, unless the blood purifier is removed from the packaging bag. It is confirmed empirically that degradation and degradation of the hollow fiber membrane is suppressed for 3 years (thus, the elution amount of hydrogen peroxide does not increase).
- a blood purifier that ensures safety, biocompatibility, and long-term storage stability can be provided by appropriately combining production methods that have been intensively studied as described above.
- the blood outlet circuit of the dialyzer (the outlet side from the pressure measurement point) was sealed with forceps to form a total filtration circuit.
- Purified water kept at 37 ° C is placed in a pressurized tank, and the pressure is controlled by a regulator.
- the pure water is sent to the dialyzer kept at 37 ° C constant temperature bath, and the mass of the filtrate flowing out from the dialysate side is Measure up to.
- the transmembrane pressure difference (TMP) is
- TMP (Pi + Po) / 2
- TMP The filtration flow rate was measured at four points, and the water permeability (mLZhrZmmHg) was calculated from the slope of the relationship. At this time, the correlation coefficient between TMP and filtration flow rate must be 0.999 or more. In order to reduce the pressure loss error due to the circuit, TMP was measured in the range of lOOmmHg or less. As for the water permeability of the hollow fiber membrane, the membrane area and the water permeability of the dialyzer were also calculated.
- UFR (H) is the water permeability of the hollow fiber membrane (mLZm 2 ZhrZmmHg)
- UFR (D) is the water permeability of the dialyzer (mL / hrZmmHg)
- A is the membrane area (m 2 ) of the dialyzer.
- the membrane area of the dialyzer was determined as a reference for the inner diameter of the hollow fiber membrane.
- n is the number of hollow fiber membranes in the dialyzer, ⁇ is the circumference, d is the inner diameter (m) of the hollow fiber membrane, and L is the effective length (m) of the hollow fiber membrane in the dialyzer.
- the dialysate side of a module consisting of about 10,000 hollow fiber membranes was filled with water and plugged. Dry air or nitrogen was fed from the blood side at room temperature and pressurized at a rate of 0.5 MPa per minute. The pressure was increased, and the air pressure when the hollow fiber membrane burst (bursts) with pressurized air and bubbles were generated in the liquid filled on the dialysate side was taken as the burst pressure.
- a cross section of 100 hollow fibers was observed with a 200 ⁇ projector.
- the thickness of the thinnest part, the thinnest part, and the thinnest part were measured on one thread cross-section with the greatest difference in film thickness.
- a measurement method when polyvinylpyrrolidone is used as the hydrophilic polymer is exemplified.
- Extraction was performed by a method defined in the dialysis artificial kidney device manufacturing approval standard, and polyvinylpyrrolidone in the extract was quantified by a colorimetric method.
- physiological saline was passed through the dialysate side channel of the module at 500 mLZ min for 5 minutes, and then passed through the blood side channel at 200 mLZmin. Thereafter, the solution was passed through the blood-side dialysate side with filtration at 200 mLZmin for 3 minutes, and then freeze-dried to obtain a dry membrane, and the above-mentioned quantification was performed using the dry membrane.
- the content of the hydrophilic polymer relative to the hydrophobic polymer was determined by X-ray photoelectron spectroscopy (ESCA method).
- ESA method X-ray photoelectron spectroscopy
- One hollow fiber membrane was attached to a sample stage and measured by X-ray photoelectron spectroscopy (ESCA method).
- the measurement conditions are as follows.
- Photoelectron escape angle 45 °
- Vacuum degree about 10 _7 Pa or less
- the measurement method when PVP is used as the hydrophilic polymer is illustrated.
- the sample was dried for 48 hours at 80 ° C using a vacuum dryer, and its lOmg was analyzed with a CHN coder (manufactured by Yanaco Analytical Co., Ltd., MT-6 type).
- the content of PVP was determined from the nitrogen content. Was calculated by the following formula.
- the outer surface of the hollow fiber membrane is observed with a 10,000x electron microscope and a photograph (SEM photograph) is taken.
- the image was processed with image analysis processing software to obtain the porosity of the outer surface of the hollow fiber membrane.
- Image analysis processing software is measured using, for example, Image Pro Plus (Media Cybernetics, Inc.).
- the emphasis' filter operation was performed so that the captured image could be identified as a hole and a blockage. Thereafter, the hole is counted, and if the lower polymer chain can be seen inside the hole, the hole is combined and counted as one hole.
- Counting was performed in the same manner as in the previous section to determine the area of each hole. In addition, holes on the measurement range boundary were excluded during counting. This was carried out for 10 fields of view and the average of all pore areas was obtained.
- the cross section of the hollow fiber membrane is projected with a projector with a magnification of 200 times, and the inner diameter (A) and outer diameter (B) of the largest, smallest and medium size hollow fibers are measured in each field of view.
- the average film thickness of 90 hollow fibers with 30 fields of view was calculated.
- Dialysate with endotoxin concentration of 200 EUZL is fed from the inlet of the module at a flow rate of 500 mlZmin, and dialysate containing endotoxin is passed from the outside to the inside of the hollow fiber membrane. Filtration was performed at a filtration rate of 15 mlZmin for 2 hours, and the dialysate filtered from the outside of the hollow fiber membrane to the inside of the hollow fiber membrane was stored, and the endotoxin concentration of the stored solution was measured. The endotoxin concentration was analyzed using Limulus ESII test KOKO (manufactured by Wako Pure Chemical Industries, Ltd.) according to the method described in the instruction manual (gelation overturning method).
- the measurement was performed by gas chromatography. Use a column packed with molecular sieves (GL Sieves molecular sieve 13X-S mesh 60/80), carrier gas with argon gas, detector with heat conduction method, column temperature 60 ° C I analyzed it.
- the gas in the packaging bag was collected by piercing the syringe needle directly into the unopened packaging bag.
- the absolute dry method was adopted for the measurement. Using a weighing bottle, the weight of a hollow fiber membrane of about 1 lg representing the sample was accurately measured to 4 digits after the decimal point. Thereafter, it was completely dried at 105 ° C. for 3 hours, and then sufficiently cooled to room temperature, and then the weight of the hollow fiber membrane after being completely dried was measured accurately to 4 digits after the decimal point.
- the water content was calculated by the following formula.
- Ron (R) RH type manufactured by T & D
- physiological saline (Otsuka Pharmaceutical Co., Ltd.) was flowed as an initial cleaning solution on the blood side at a flow rate of lOOmLZmin. After the blood purifier was full, the cleaning solution (25 mL) was sampled for 15 seconds. . In addition, in order to confirm the amount of eluate after 5 minutes from the start of washing, the washing solution was sampled for 15 seconds (25 mL) from 5 minutes after the start of washing. 10 mL of these sample forces were taken out, 20 mL of 2.0 ⁇ 10 _3 mol / l potassium permanganate aqueous solution and 1 mL of dilute hydrochloric acid were added and boiled for 3 minutes.
- the difference between the amount of sodium thiosulfate aqueous solution required for the titration of water and the amount of sodium thiosulfate aqueous solution required for the titration of the sample without passing through the blood purifier was calculated as the amount of potassium permanganate aqueous solution consumed by the eluate ( Consumption of potassium permanganate aqueous solution).
- the measurement was performed at 20 ° C. and 90% RH using an oxygen transmission rate measuring device (OX-TORAN100 manufactured by Modern Controls).
- Polyethersulfone manufactured by Sumika Chemtex Co., Sumikaetaseru (R) 5200P
- 17 Weight 0/0 Poly Bulle pyrrolidone (BASF Corp. Kollidon (R) K- 90) 2.5 Weight 0/0
- dimethyl ⁇ Seto amide (D MAc ) Dissolve 77.5% by mass, 3% by mass of RO water uniformly at 50, and then reduce the pressure to ⁇ 500 mmHg using a vacuum pump.
- the system was immediately sealed and left for 15 minutes. This operation was repeated three times to degas the film forming solution.
- the membrane-forming solution is passed through 15 m and 15 m two-stage sintered filters in order, and then degassed for 30 minutes at 700 mm Hg as a hollow forming agent from a tube-in orifice nozzle heated to 80 ° C.
- the sample was discharged using a 60% by weight DMAc aqueous solution, passed through a 400mm dry section cut off from the outside air by a spinning tube, coagulated in a 20% by weight DMAc aqueous solution at 60 ° C, and sprinkled thoroughly in a wet state. Raised.
- the nozzle slit width of the tube-in-orifice nozzle used is an average of 60 m, the maximum is 61 ⁇ m, the minimum is m, the maximum and minimum slit width ratio is 1.03, and the draft ratio of the film-forming solution is 1.06.
- the absolute humidity of the part was 0.18 kgZkg dry air.
- the roller contacted with the hollow fiber membrane was a mirror-finished surface, and all guides were surface-finished.
- a polyethylene film whose surface on the side of the hollow fiber bundle has been textured is wound around about 10,000 bundles of the hollow fiber membranes, and then heated in hot water at 80 ° C for 30 minutes X 4 Washed twice. After cleaning, drying was performed in a nitrogen atmosphere at 40 ° C.
- the resulting hollow fiber membrane had an inner diameter of 198.5 m and a film thickness of 28.5 m.
- the content of the hydrophilic polymer in the hollow fiber membrane was measured and found to be 4.3% by mass.
- a blood purifier was assembled using the hollow fiber membrane thus obtained, and a leak test was performed. As a result, the adhesion failure caused by the sticking of the hollow fibers was not recognized.
- the blood purifier was preliminarily degassed with RO water and irradiated with 25 kGy of ⁇ -rays for crosslinking. Blood purifier power after ⁇ -irradiation The hollow fiber membrane was cut out and subjected to the eluate test. As a result, the elution amount of PVP was 8 ppm, which was a satisfactory level.
- the blood purifier was filled with pressurized air at a pressure of O.lMPa, and a product that passed the leak test with a pressure drop for 10 seconds of 30 mm Aq or less was used in the subsequent tests. Also, hollow fiber from blood purifier When the film was taken out and the outer surface was observed with a microscope, no defects such as scratches were observed.
- the blood purifier together with AGELESS (R) Z-200PT (manufactured by Mitsubishi Gas Chemical Company), has an oxygen permeability of 0.5 cm 3 / (m 2 ⁇ 24 hr-atm) (20 ° C, 90 % RH) and water vapor permeability of 3 g / (m 2 24 hr'atm) (40 ° C, 90% RH), sealed with nitrogen gas, sealed, and kept at room temperature for 12 hours. After standing, the blood purifier was sterilized with 25 kGy ⁇ -rays.
- the moisture content relative to the weight of the hollow fiber membrane was 2.5% by mass
- the relative humidity around the hollow fiber was 60% RH (25 ° C)
- the oxygen concentration in the packaging bag was 0.05%.
- the eluate from the hollow fiber membrane was 7 ppm
- the consumption of the potassium permanganate aqueous solution was 2 mL per lm 2 of the surface area of the hollow fiber membrane.
- the elution amount of hydrogen peroxide was 3 ppm.
- Table 1 The other analysis results are shown in Table 1.
- a wet hollow fiber membrane bundle was obtained in the same manner as in Example 1 except that the same membrane-forming solution as in Example 1 was not passed through the filter and was not washed.
- a blood purifier was assembled using the hollow fiber membrane thus obtained.
- the blood purifier was filled with RO water and subjected to crosslinking treatment by irradiating X-rays with an absorbed dose of 25 kGy.
- the resulting hollow fiber membrane had an inner diameter of 199 ⁇ m and a film thickness of 28 m.
- the content of the hydrophilic polymer in the hollow fiber membrane was measured and found to be 9.6% by mass.
- the blood purifier together with Ageless (R) Z-200PT (manufactured by Mitsubishi Gas Chemical Co., Ltd.) has an oxygen permeability of 0.5 cm 3 / (m 2 ⁇ 24 hr-atm) (20 ° C, 90 % RH) and water vapor permeability of 3 g / (m 2 24 hr'atm) (40 ° C, 90% RH), sealed with nitrogen gas, sealed, and left at room temperature for 12 hr Later, the blood purifier was sterilized with 25 kGy of ⁇ rays.
- the moisture content relative to the weight of the hollow fiber membrane was 2.8% by mass
- the relative humidity around the hollow fiber was 70% RH (25 ° C)
- the oxygen concentration in the packaging bag was 0.08%.
- the eluate of strong hollow fiber membrane was 8 ppm
- the consumption of potassium permanganate aqueous solution was 3 mL per lm 2 of the inner surface area of the hollow fiber membrane.
- the elution amount of hydrogen peroxide was 3 ppm.
- Table 1 The other analysis results are shown in Table 1.
- Polyethersulfone manufactured by Sumika Chemtex Co., Sumikaetaseru (R) 5200P
- poly Bulle pyrrolidone BASF Corp. Kollidon (R) K-90
- This membrane-forming solution was passed through a 100-m filter and then simultaneously with 30% by weight DMAc aqueous solution degassed at 700 mmHg for 2 hours as a hollow forming agent from a tube-in orifice nozzle heated to 60 ° C. After discharging and passing through a 600 mm dry section cut off from the outside air by a spinning tube, it was solidified in a DMAc aqueous solution having a concentration of 10 mass% and 60 ° C.
- the nozzle slit width of the tube-in-orifice nozzle used averaged 100 ⁇ m, maximum 110 ⁇ m, minimum 90 ⁇ m, maximum slit width value, minimum value ratio 1.22, draft ratio 2.41, dry section
- the absolute humidity was 0.12kgZkg dry air.
- the obtained hollow fiber membrane was passed through a 40 ° C. water washing tank for 45 seconds to remove the solvent and excess hydrophilic polymer, and then was wound up in a wet state and dried in air at 50 ° C.
- the resulting hollow fiber membrane had an inner diameter of 197.8 m and a film thickness of 29.2 m.
- the content of hydrophilic polymer in the hollow fiber membrane was measured and found to be 7.4% by mass.
- a blood purifier was assembled using the hollow fiber membrane thus obtained.
- ⁇ -rays were irradiated with an absorbed dose of 25 kGy to carry out a crosslinking treatment.
- Blood purifier power after ⁇ -ray irradiation Hollow fiber membranes were cut out and subjected to the eluate test.
- the VP elution amount was 12 ppm. Insufficient cleaning of the hollow fiber membrane was considered.
- the blood purifier was filled with pressurized air at a pressure of O. lMPa, and a module having a pressure drop for 10 seconds of 30 mmAq or less was used for the test. In the blood leak test using bovine blood, two of the 30 modules showed blood cell leaks.
- Polyethersulfone manufactured by Sumika Chemtex Co., Sumikaetaseru (R) 4800P
- poly Bulle pyrrolidone BASF Corp. Kollidon (R) K- 90
- Weight 0/0 Poly Bulle pyrrolidone
- DMAc73.5 mass 0/0 5% by mass of water was dissolved at 50%.
- the system was immediately sealed and allowed to stand for 10 minutes so that the solvent and the like were volatilized and the film forming solution composition did not change. This operation was repeated three times to degas the film forming solution.
- the obtained film-forming solution was passed through 15 m and 15 m two-stage filters, and then degassed for 2 hours at -700 mmHg from a tube in orifice nozzle heated to 70 ° C as a hollow forming agent.
- the 50 mass% 0 ⁇ 1 ⁇ aqueous solution was discharged at the same time, passed through a 300 mm air gap section cut off from the outside air by a spinning tube, and then coagulated in 60 ° C water.
- the absolute humidity was 0.12kgZkg dry air.
- Coagulation bath strength The pulled-up hollow fiber membrane was passed through a 85 ° C water washing tank for 45 seconds to remove the solvent and excess hydrophilic polymer, and then rolled up.
- the roller for changing the yarn path during the spinning process was a mirror-finished surface, and the fixed guide was a satin-finished surface.
- the blood purifier was subjected to the subsequent analysis without carrying out the crosslinking treatment of the hydrophilic polymer.
- the elution amount of PVP was as good as 6 ppm.
- the hollow fiber membrane was taken out from the blood purifier and the outer surface was observed with a microscope, defects such as scratches were not observed.
- the endotoxin permeation test the endotoxin filtered inside the hollow fiber was below the detection limit and was at a satisfactory level.
- the blood purifier was combined with AGELESS (R) Z-200PT (Mitsubishi Gas Chemical Co., Ltd.), and the oxygen permeability was 0.5 cm 3 / (m 2 '24hr'atm) (20 ° C, 90% RH ) And water vapor permeability of 3g / (m 2 '24hr • atm) (40 ° C, 90% RH), replaced with nitrogen gas, sealed and left at room temperature for 36hr, then 25kGy
- the blood purifier was sterilized with ⁇ rays.
- the moisture content relative to the weight of the hollow fiber membrane was 2.2% by mass
- the relative humidity around the hollow fiber was 60% RH (25 ° C)
- the oxygen concentration in the packaging bag was 0.03%.
- the eluate from the hollow fiber membrane was 8 ppm
- the consumption of the potassium permanganate aqueous solution was 2 mL per lm 2 of the inner surface area of the hollow fiber membrane.
- the elution amount of hydrogen peroxide was 2 ppm.
- Table 1 The other analysis results are shown in Table 1.
- Polyethersulfone manufactured by Sumika Chemtex Co., Sumikaetaseru (R) 7800P) 22 Weight 0/0, poly Bulle pyrrolidone (BASF Corp. Kollidon (R) K-30) 9 mass 0/0, DMAC 66 mass 0/0, water 3% by mass was dissolved at 50 ° C, and after reducing the pressure in the system to -350mmHg using a vacuum pump, the solvent was volatilized and the film forming solution composition was not changed immediately. Sealed and left for 30 minutes. This operation was repeated twice to degas the film forming solution.
- the obtained film-forming solution was passed through a 30 m and 30 m two-stage filter, and was then degassed in advance as a hollow forming agent from a tube-in orifice nozzle heated to 50 ° C. It is discharged at the same time as the aqueous solution, passes through a 300 mm air gap that is blocked from the outside air by a spinning tube, and then condenses in 50 ° C water. Solidified.
- the nozzle slit width of the tube-in-orifice nozzle used is an average of 45 m, the maximum is 45.5 m, the minimum is 44.5 m, the maximum and minimum slit width ratio is 1.02, the draft ratio is 1.06, and the absolute humidity of the dry section is 0.07 kgZkg dry air.
- the hollow fiber membrane pulled up from the coagulation bath was passed through a 40 ° C water washing tank for 45 seconds to remove the solvent and excess hydrophilic polymer, and then wound up.
- the resulting 10,000 hollow fiber membrane bundles were not washed and dried at 40 ° C in an air atmosphere.
- the resulting hollow fiber membrane had an inner diameter of 199.5 m and a film thickness of 29.0 m. When the content of the hydrophilic polymer in the hollow fiber membrane was measured, it was 7.7% by mass.
- Example 2 The same membrane-forming solution as in Example 1 was passed through a two-stage filter of 30 m and 15 m, and then heated to 80 ° C. using a 60 mass% DMAc aqueous solution degassed in advance as a hollow forming agent.
- the tube was simultaneously discharged from the tube-in orifice nozzle, passed through a 400 mm long dry section cut off from the outside air by a spinning tube, and then coagulated in a coagulation bath consisting of 70 ° C RO water.
- Nozzle slit width of tube-in-orifice nozzle used averaged 60 ⁇ m, maximum 62 ⁇ m, minimum 58 ⁇ m, maximum and minimum slit width ratio 1.07, draft ratio 1.06, absolute dry section
- the humidity was 0.23 kgZkg dry air.
- the hollow fiber membrane pulled up from the coagulation bath was then immersed in a water washing bath at a temperature of 60 ° C for 45 seconds, wound up, and dried in a dry heat oven at 70 ° C.
- the obtained hollow fiber membrane had an inner diameter of 200 m and a film thickness of 31 ⁇ m.
- the content of the hydrophilic polymer in the hollow fiber membrane was measured and found to be 6.3% by mass.
- a blood purifier was assembled using the hollow fiber membrane thus obtained, and an air leak test was performed. As a result, it was observed that bubbles were generated in the module adhesion force. It seems that poor adhesion due to the sticking of hollow fibers occurred.
- the blood purifier force without cross-linking treatment was also cut out of the hollow fiber membrane and subjected to the eluate test, the amount of PVP elution was 12 ppm. This was thought to be due to insufficient washing of the hollow fiber membrane and uncrosslinked hydrophilic polymer.
- the blood purifier is filled with pressurized air at a pressure of O.lMPa and the pressure drop is reduced for 10 seconds. Modules with the bottom below 30mmAq were used for the test.
- Polyethersulfone manufactured by Sumika Chemtex Co., Sumikaetaseru (R) 5200P
- poly Bulle pyrrolidone BASF Corp. Kollidon (R) K- 90
- 7.5 Weight 0/0, DMAc72.5 mass 0/0 3% by weight of water was dissolved at 50 ° C, and after reducing the pressure to 500 mmHg using a vacuum pump, the solvent etc. volatilized and the film forming solution composition did not change!
- the system was sealed and left for 30 minutes. This operation was repeated three times to degas the film forming solution.
- the obtained film-forming solution was discharged through a tube-in orifice nozzle heated to 50 ° C without passing through a filter and simultaneously with a 75 mass% DMAc aqueous solution degassed under reduced pressure in advance as a hollow forming agent. After passing through a 600mm air gap, which was blocked from the outside air, the solution was solidified in 70 ° C water.
- the nozzle slit width of the tube-in-orifice nozzle used averaged 60 m, maximum 64 m, minimum 56 / ⁇ ⁇ , maximum / minimum slit width ratio 1.14, draft ratio 1.06, absolute dry section
- the humidity was 0.17 kgZkg dry air.
- the obtained hollow fiber membrane was washed with water to remove the solvent, and then wound up into about 10,000 bundles.
- the film was immersed in a 30% by mass, 50 ° C glycerin aqueous solution for 1 hour, and then dried at 80 ° C.
- the resulting hollow fiber membrane had an inner diameter of 197; ⁇ ⁇ and a film thickness of
- the content of the hydrophilic polymer in the hollow fiber membrane was measured and found to be 6.1% by mass.
- the hollow fiber membrane bundle thus obtained did not adhere to the hollow fibers because glycerin was adhered to the membrane surface.
- the assembled blood purifier was composed of an end urethane oligomer. The amount was too much to guarantee sufficient safety.
- the blood purifier was irradiated with ⁇ rays at an absorbed dose of 25 kGy in a state filled with water.
- the elution amount of PVP was 13 ppm. It was thought that crosslinking of the hydrophilic polymer was hindered by insufficient washing of the hollow fiber membrane and the effect of glycerin contained in the filling liquid.
- Polysulfone (Amokone earth manufactured P- 3500) 18 Weight 0/0, poly Bulle pyrrolidone (BASF Corp. K-60) 9 wt%, DMAc68 wt%, water 5% by weight was dissolved at 50, then using a vacuum pump After reducing the pressure in the system to ⁇ 300 mmHg, the system was immediately sealed and allowed to stand for 15 minutes so that the solvent and the like were volatilized and the film forming solution composition did not change. This operation was repeated three times to degas the film forming solution.
- the obtained film-forming solution was passed through a 15 m and 15 m two-stage filter, and then a 35 mass% DMAc aqueous solution degassed in advance as a hollow forming agent from a tube-in orifice nozzle heated to 40 ° C. At the same time, it was discharged, passed through a 600 mm air gap section cut off from the outside air by a spinning tube, and then solidified in 50 ° C water.
- the absolute humidity was 0.07 kgZkg dry air.
- Coagulation bath strength The pulled-up hollow fiber membrane was passed through a 85 ° C water washing tank for 45 seconds to remove the solvent and excess hydrophilic polymer, and then rolled up. About 10,000 bundles of the hollow fiber membranes were immersed in pure water and washed in an autoclave for 121 ° CXI hours. After a polyethylene film similar to that in Example 1 is wound around the hollow fiber membrane bundle after washing
- the roller for changing the yarn path during the spinning process was a mirror-finished surface, and the fixed guide was a satin-finished surface.
- the obtained hollow fiber membrane had an inner diameter of 201 ⁇ m and a film thickness of 43 m.
- the content of the hydrophilic polymer in the hollow fiber membrane was measured and found to be 8.8% by mass.
- the blood purifier was filled with pressurized air at a pressure of O.lMPa, and a product that passed a leak test with a pressure drop of 10 mm or less of 30 mmAq or less was used in the subsequent tests. Further, when the blood purification device hollow fiber membrane was taken out and the outer surface was observed with a microscope, no defects such as scratches were observed. In addition, the blood cell leaked with citrated fresh bovine blood at a blood flow rate of 200 mL / min and a filtration rate of lOmL / min. Endotoxin filtered from the outside of the hollow fiber to the inside of the hollow fiber was below the detection limit and was at a problematic level.
- the blood purifier together with AGELESS (R) Z-200PT (Mitsubishi Gas Chemical Co., Ltd.) has an oxygen permeability of 0.5 cm 3 / (m 2 '24hr'atm) (20 ° C, 90% RH ) And water vapor permeability of 3g / (m 2 '24hr • atm) (40 ° C, 90% RH), replaced with nitrogen gas, sealed and left at room temperature for 36hr, then 25kGy
- the blood purifier was sterilized with ⁇ rays.
- the moisture content relative to the weight of the hollow fiber membrane was 3.1% by mass
- the relative humidity around the hollow fiber was 70% RH (25 ° C)
- the oxygen concentration in the packaging bag was 0.05%.
- the eluate from the hollow fiber membrane was 6 ppm
- the consumption of the potassium permanganate aqueous solution was 2 mL per lm 2 of the inner surface area of the hollow fiber membrane.
- the elution amount of hydrogen peroxide was 4 ppm.
- Table 1 The other analysis results are shown in Table 1.
- the obtained membrane-forming solution was passed through a three-stage filter of 15 m, 15 m, and 15 ⁇ m, and then degassed under reduced pressure as a hollow forming agent from a tube-in orifice nozzle heated to 40 ° C.
- the solution was discharged at the same time as the mass% DMAc aqueous solution, passed through a 600 mm air gap portion cut off from the outside air by a spinning tube, and then solidified in 50 ° C water.
- the average nozzle width and groove slit width of the tube orifice nozzle used were 60 ⁇ m, maximum 61 ⁇ m, minimum 59 ⁇ m, slit
- the ratio of the maximum and minimum values of the width was 1.03
- the draft ratio was 1.01
- the absolute humidity of the dry section was 0.12 kgZ kg dry air.
- the hollow fiber membrane with increased coagulation bath power was passed through a 85 ° C water washing tank for 45 seconds to remove the solvent and excess hydrophilic polymer, and then rolled up. About 10,000 bundles of the hollow fiber membranes were immersed in pure water and washed in an autoclave at 121 ° C for 1 hour. A polyethylene film was wound around the hollow fiber membrane bundle after washing, and then dried in a nitrogen stream at 45 ° C.
- the roller used for changing the yarn path during the spinning process was a mirror-carried surface, and the fixed guide was a satin-finished surface.
- the resulting hollow fiber membrane had an inner diameter of 201 ⁇ m and a film thickness of 46 m.
- the content of the hydrophilic polymer in the hollow fiber membrane was measured and found to be 5.2% by mass.
- a blood purifier was assembled using the hollow fiber membrane thus obtained.
- the blood purifier was filled with RO water and irradiated with ⁇ rays at an absorbed dose of 25 kGy for crosslinking treatment.
- the PVP elution amount was 7 ppm, which was not a problem.
- the blood purifier was filled with pressurized air at a pressure of O.lMPa, and a product that passed the leak test with a pressure drop for 10 seconds of 30 mmAq or less was used in subsequent tests. Further, when the hollow fiber membrane was taken out from the blood purifier and the outer surface was observed with a microscope, no defects such as scratches were observed. In addition, the blood flow was 200 mL / min at a flow rate of 200 mL / min and the filtration rate was lOmL / min. Endotoxin filtered from the outside of the hollow fiber to the inside of the hollow fiber is below the detection limit and should be used at a satisfactory level.
- the blood purifier was combined with AGELESS (R) Z-200PT (manufactured by Mitsubishi Gas Chemical Co., Ltd.) with an oxygen permeability of 0.5 cm 3 / (m 2 '24hr'atm) (20 ° C, 90 % RH) and water vapor permeability of 3g / (m 2 '24hr • atm) (40 ° C, 90% RH). Replace with nitrogen gas, seal, and leave at room temperature for 36hr.
- the blood purifier was sterilized with 25 kGy gamma rays.
- the moisture content with respect to the weight of the hollow fiber membrane was 2.9% by mass
- the relative humidity around the hollow fiber was 70% RH (25 ° C)
- the oxygen concentration in the packaging bag was 0.05%.
- the eluate from the hollow fiber membrane was 4 ppm
- the consumption of the potassium permanganate aqueous solution was the inner surface of the hollow fiber membrane.
- the volume was 1 mL per lm 2
- the elution amount of hydrogen peroxide was 6 ppm when the blood purifier was stored at 25 ° C and 50% RH for 3 months.
- Table 1 The other analysis results are shown in Table 1.
- a hollow fiber membrane was obtained in the same manner as in Example 1, and a blood purifier was assembled. As a result of the leak test, no adhesion failure due to the sticking of the hollow fibers was observed.
- the blood purifier was subjected to the subsequent analysis without performing the crosslinking treatment of the hydrophilic polymer.
- the elution amount of PVP was 6 ⁇ m, which was good.
- the hollow fiber membrane was taken out from the blood purifier and the outer surface was observed with a microscope, no defects such as scratches were observed.
- bovine blood no blood cell leak was observed.
- endotoxin permeation test endotoxin filtered from the outside of the hollow fiber to the inside of the hollow fiber is below the detection limit, and it is not a problem.
- the blood purifier has an oxygen permeability of 0.5 cm 3 / (m 2 ⁇ 24hr-atm) (20 ° C, 90% RH) and a water vapor permeability of 3 g / (m 2 '24hr'atm ) Placed in a packaging bag (40 ° C, 90% RH), replaced with nitrogen gas, sealed, and sterilized blood purifier with 25 kGy ⁇ -rays.
- the moisture content relative to the weight of the hollow fiber membrane was 3.7% by mass
- the relative humidity around the hollow fiber membrane was 45% RH (25 ° C)
- the oxygen concentration in the packaging bag was 0.08%.
- the eluate from the hollow fiber membrane was 7 ppm, and the consumption of the potassium permanganate aqueous solution was 4 mL per lm 2 of the inner surface area of the hollow fiber membrane.
- the elution amount of hydrogen peroxide was 7 ppm.
- a hollow fiber membrane bundle was obtained under the same spinning stock solution and spinning conditions as in Example 1.
- a blood purifier similar to that of Example 1 was assembled using the obtained hollow fiber membrane bundle.
- the blood purifier was subjected to the subsequent analysis without performing the crosslinking treatment of the hydrophilic polymer.
- the elution amount of PVP was as good as 6 ppm. Further, when the hollow fiber membrane was taken out from the blood purifier and the outer surface was observed with a microscope, no defects such as scratches were observed.
- the blood purifier was used together with AGELESS (R) Z-200PT (manufactured by Mitsubishi Gas Chemical Co., Ltd.) and an oxygen permeability of 0.5 cm 3 / (m 2 '24hr'atm) (20 ° C, 90 % RH) and water vapor permeability of 3g / (m 2 '24hr • atm) (40 ° C, 90% RH). Replace with nitrogen gas, seal, and leave at room temperature for 36hr.
- the blood purifier was sterilized with 25 kGy gamma rays.
- the moisture content relative to the weight of the hollow fiber membrane was 0.3% by mass
- the relative humidity around the hollow fiber membrane was 80% RH (25 ° C)
- the oxygen concentration in the packaging bag was 0.04%.
- the eluate of strong hollow fiber membrane was 6 ppm
- the consumption of potassium permanganate aqueous solution was 2 mL per lm 2 of the surface area of the hollow fiber membrane.
- the elution amount of hydrogen peroxide was 4 ppm.
- Table 1 The other analysis results are shown in Table 1.
- a hollow fiber membrane bundle was obtained under the same spinning stock solution and spinning conditions as in Example 1.
- a blood purifier similar to that of Example 1 was assembled using the obtained hollow fiber membrane bundle.
- the blood purifier was subjected to the subsequent analysis without performing the crosslinking treatment of the hydrophilic polymer.
- the elution amount of PVP was as good as 6 ppm. Further, when the hollow fiber membrane was taken out from the blood purifier and the outer surface was observed with a microscope, no defects such as scratches were observed.
- the blood purifier was used with AGELESS (R) Z-200PT (Mitsubishi Gas Chemical Co., Ltd.) and an oxygen permeability of 0.5 cm 3 / (m 2 '24hr'atm) (20 ° C, 90 % RH) and water vapor permeability of 3g / (m 2 '24hr • atm) (40 ° C, 90% RH). Replace with nitrogen gas, seal, and leave at room temperature for 36hr.
- the blood purifier was sterilized with 25 kGy gamma rays.
- the moisture content with respect to the weight of the hollow fiber membrane was 2.2% by mass, the relative humidity around the hollow fiber was 35% RH (25 ° C), and the oxygen concentration in the packaging bag was 0.03%.
- the eluate from the hollow fiber membrane was 15 ppm, and the consumption amount of the potassium permanganate aqueous solution was the inner surface of the hollow fiber membrane.
- Table 1 The other analysis results are shown in Table 1.
- a hollow fiber membrane bundle was obtained under the same spinning stock solution and spinning conditions as in Example 1.
- a blood purifier similar to that of Example 1 was assembled using the obtained hollow fiber membrane bundle.
- the blood purifier was subjected to the subsequent analysis without performing the crosslinking treatment of the hydrophilic polymer.
- the elution amount of PVP was as good as 6 ppm. Further, when the hollow fiber membrane was taken out from the blood purifier and the outer surface was observed with a microscope, no defects such as scratches were observed.
- the eluate from the hollow fiber membrane was 18 ppm, and the consumption of the potassium permanganate aqueous solution was 7 mL per lm 2 of the surface area of the hollow fiber membrane.
- the amount of hydrogen peroxide dissolved was 22 ppm.
- a hollow fiber membrane bundle was obtained under the same spinning stock solution and spinning conditions as in Example 1.
- a blood purifier similar to that of Example 1 was assembled using the obtained hollow fiber membrane bundle.
- the blood purifier was subjected to the subsequent analysis without performing the crosslinking treatment of the hydrophilic polymer.
- the blood purifier without irradiation with y-rays was also cut out of a hollow fiber membrane and subjected to the eluate test. I got it. Further, when the hollow fiber membrane was taken out from the blood purifier and the outer surface was observed with a microscope, no defects such as scratches were observed. In the blood leak test using bovine blood, no blood cell leak was observed.
- the endotoxin permeation test the endotoxin filtered from the outside of the hollow fiber to the inside of the hollow fiber was below the detection limit and was at a problematic level.
- the blood purifier was combined with AGELESS (R) Z-200PT (manufactured by Mitsubishi Gas Chemical Co., Ltd.) with an oxygen permeability of 10 cm 3 / (m 2 ⁇ 24 hr ⁇ atm) (20 ° C, 90% RH) and a water vapor transmission rate of 15 g / (m 2 ⁇ 24 hr • atm) (40 ° C, 90% RH), replace with nitrogen gas, seal, and leave at room temperature for 36 hr.
- the blood purifier was sterilized with 25 kGy gamma rays.
- the moisture content with respect to the weight of the hollow fiber membrane was 2.2% by mass, the relative humidity around the hollow fiber was 50% RH (25 ° C), and the oxygen concentration in the packaging bag was 16.2%.
- the effluent from the hollow fiber membrane was 226 ppm, and the consumption of the potassium permanganate aqueous solution was 15 mL per lm 2 of the surface area of the hollow fiber membrane.
- the elution amount of hydrogen peroxide was 51 lppm.
- Example 2 Example 3
- Example 4 Example 5
- Example 6 Example 1
- Example 2 Example 3
- Example 4 Example 5
- Example 6 Example 7
- Example 8 Permeability (ml / iin 2 * hr mm mmHg) ⁇ 510 342 602 290 339 343 498 D26-Shi 2 329 336 498 Paste pressure (MPa) 0.6 0.6 0.7 0.6 0.6 0.2 0.3 0.7 0.2 0.6 0.6 0.6 Unevenness 0.73 0.90 0,88 0.90 0.92 0.47 0.41 ⁇ 0.72 0.43 0.90 0.91 0,74 Blood leak module (main) 0 0 0 0 0 0 3 2-0 4 0 0 0 0
- the blood purifier of the present invention has high water permeability suitable for the treatment of chronic renal failure with high safety and stability of performance.
- the blood purifier of the present invention can be used in a dry state, the blood purifier is suitable as a high-performance blood purifier that is easy to handle and free from fear of freezing.
- the eluate which is a foreign substance, can be suppressed when viewed from the human body, and is safe as a medical device, and thus is suitable for a blood purifier.
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Abstract
Description
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Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
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US11/573,339 US20080000830A1 (en) | 2004-08-10 | 2005-08-08 | Highly Water Permeable Hollow Fiber Membrane Type Blood Purifier and Process for Manufacturing the Same |
EP05770443A EP1797916A4 (en) | 2004-08-10 | 2005-08-09 | HIGHLY WATER-PERMISSIBLE BLOOD CLEANER OF THE HOLLY FIBER MEMBRANE TYPE AND METHOD FOR ITS MANUFACTURE |
JP2006531648A JP4848278B2 (ja) | 2004-08-10 | 2005-08-09 | 高透水性中空糸膜型血液浄化器及びその製造方法 |
BRPI0514298-9A BRPI0514298A (pt) | 2004-08-10 | 2005-08-09 | purificador de sangue de tipo membrana de fibras ocas, altamente permeável à água, e processo para a sua preparação |
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US (1) | US20080000830A1 (ja) |
EP (1) | EP1797916A4 (ja) |
JP (1) | JP4848278B2 (ja) |
CN (1) | CN101043911A (ja) |
BR (1) | BRPI0514298A (ja) |
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WO (1) | WO2006016575A1 (ja) |
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- 2005-08-08 US US11/573,339 patent/US20080000830A1/en not_active Abandoned
- 2005-08-09 JP JP2006531648A patent/JP4848278B2/ja active Active
- 2005-08-09 EP EP05770443A patent/EP1797916A4/en not_active Withdrawn
- 2005-08-09 CN CN200580033571.4A patent/CN101043911A/zh active Pending
- 2005-08-09 RU RU2007107948/14A patent/RU2389513C2/ru active
- 2005-08-09 BR BRPI0514298-9A patent/BRPI0514298A/pt not_active IP Right Cessation
- 2005-08-09 WO PCT/JP2005/014568 patent/WO2006016575A1/ja active Application Filing
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Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2016052567A1 (ja) * | 2014-09-29 | 2016-04-07 | 旭化成メディカル株式会社 | 中空糸膜型血液浄化装置 |
KR20170009957A (ko) | 2014-09-29 | 2017-01-25 | 아사히 가세이 메디컬 가부시키가이샤 | 중공사막형 혈액 정화 장치 |
JPWO2016052567A1 (ja) * | 2014-09-29 | 2017-06-29 | 旭化成メディカル株式会社 | 中空糸膜型血液浄化装置 |
US10232320B2 (en) | 2014-09-29 | 2019-03-19 | Asahi Kasei Medical Co., Ltd. | Hollow-fiber membrane blood purification device |
WO2023190448A1 (ja) * | 2022-03-29 | 2023-10-05 | 国立大学法人東海国立大学機構 | 間葉系幹細胞の培養方法 |
Also Published As
Publication number | Publication date |
---|---|
EP1797916A4 (en) | 2010-07-21 |
RU2007107948A (ru) | 2008-09-20 |
EP1797916A1 (en) | 2007-06-20 |
US20080000830A1 (en) | 2008-01-03 |
CN101043911A (zh) | 2007-09-26 |
RU2389513C2 (ru) | 2010-05-20 |
BRPI0514298A (pt) | 2008-06-10 |
JPWO2006016575A1 (ja) | 2008-05-01 |
JP4848278B2 (ja) | 2011-12-28 |
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