WO2020216981A1 - Procedimiento de obtención de heparinas de bajo peso molecular por filtración de flujo tangencial - Google Patents
Procedimiento de obtención de heparinas de bajo peso molecular por filtración de flujo tangencial Download PDFInfo
- Publication number
- WO2020216981A1 WO2020216981A1 PCT/ES2020/070263 ES2020070263W WO2020216981A1 WO 2020216981 A1 WO2020216981 A1 WO 2020216981A1 ES 2020070263 W ES2020070263 W ES 2020070263W WO 2020216981 A1 WO2020216981 A1 WO 2020216981A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- concentration
- tff
- carried out
- heparin
- process according
- Prior art date
Links
- 238000009295 crossflow filtration Methods 0.000 title claims abstract description 92
- 238000000034 method Methods 0.000 title claims abstract description 87
- 229940127215 low-molecular weight heparin Drugs 0.000 title claims abstract description 23
- HTTJABKRGRZYRN-UHFFFAOYSA-N Heparin Chemical compound OC1C(NC(=O)C)C(O)OC(COS(O)(=O)=O)C1OC1C(OS(O)(=O)=O)C(O)C(OC2C(C(OS(O)(=O)=O)C(OC3C(C(O)C(O)C(O3)C(O)=O)OS(O)(=O)=O)C(CO)O2)NS(O)(=O)=O)C(C(O)=O)O1 HTTJABKRGRZYRN-UHFFFAOYSA-N 0.000 claims abstract description 72
- 229920000669 heparin Polymers 0.000 claims abstract description 68
- 229960002897 heparin Drugs 0.000 claims abstract description 61
- 230000008569 process Effects 0.000 claims abstract description 53
- 238000011026 diafiltration Methods 0.000 claims abstract description 33
- 238000009826 distribution Methods 0.000 claims abstract description 21
- 238000001914 filtration Methods 0.000 claims abstract description 16
- 238000001556 precipitation Methods 0.000 claims abstract description 16
- 229960005153 enoxaparin sodium Drugs 0.000 claims description 43
- CIJQTPFWFXOSEO-NDMITSJXSA-J tetrasodium;(2r,3r,4s)-2-[(2r,3s,4r,5r,6s)-5-acetamido-6-[(1r,2r,3r,4r)-4-[(2r,3s,4r,5r,6r)-5-acetamido-6-[(4r,5r,6r)-2-carboxylato-4,5-dihydroxy-6-[[(1r,3r,4r,5r)-3-hydroxy-4-(sulfonatoamino)-6,8-dioxabicyclo[3.2.1]octan-2-yl]oxy]oxan-3-yl]oxy-2-(hydroxy Chemical compound [Na+].[Na+].[Na+].[Na+].O([C@@H]1[C@@H](COS(O)(=O)=O)O[C@@H]([C@@H]([C@H]1O)NC(C)=O)O[C@@H]1C(C[C@H]([C@@H]([C@H]1O)O)O[C@@H]1[C@@H](CO)O[C@H](OC2C(O[C@@H](OC3[C@@H]([C@@H](NS([O-])(=O)=O)[C@@H]4OC[C@H]3O4)O)[C@H](O)[C@H]2O)C([O-])=O)[C@H](NC(C)=O)[C@H]1C)C([O-])=O)[C@@H]1OC(C([O-])=O)=C[C@H](O)[C@H]1O CIJQTPFWFXOSEO-NDMITSJXSA-J 0.000 claims description 43
- 239000012528 membrane Substances 0.000 claims description 37
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 27
- 239000003055 low molecular weight heparin Substances 0.000 claims description 25
- 238000011282 treatment Methods 0.000 claims description 21
- 150000002482 oligosaccharides Polymers 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 239000008346 aqueous phase Substances 0.000 claims description 14
- 238000011118 depth filtration Methods 0.000 claims description 12
- 238000004108 freeze drying Methods 0.000 claims description 12
- 238000005352 clarification Methods 0.000 claims description 10
- 239000012141 concentrate Substances 0.000 claims description 2
- 230000001476 alcoholic effect Effects 0.000 abstract description 7
- 229960000610 enoxaparin Drugs 0.000 abstract description 7
- 238000002360 preparation method Methods 0.000 abstract description 5
- 229960003616 bemiparin Drugs 0.000 abstract description 3
- 238000000108 ultra-filtration Methods 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 59
- 239000012466 permeate Substances 0.000 description 38
- 210000004379 membrane Anatomy 0.000 description 34
- 239000000243 solution Substances 0.000 description 28
- 230000004907 flux Effects 0.000 description 18
- 239000012465 retentate Substances 0.000 description 18
- 229940110519 bemiparin sodium Drugs 0.000 description 10
- 238000000746 purification Methods 0.000 description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 230000000717 retained effect Effects 0.000 description 9
- 239000012535 impurity Substances 0.000 description 7
- 239000002904 solvent Substances 0.000 description 6
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000011148 porous material Substances 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 4
- 150000001298 alcohols Chemical class 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000012467 final product Substances 0.000 description 4
- -1 heparin benzyl ester Chemical class 0.000 description 4
- 229910052708 sodium Inorganic materials 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 2
- 239000003146 anticoagulant agent Substances 0.000 description 2
- 229960003872 benzethonium Drugs 0.000 description 2
- MSWZFWKMSRAUBD-UHFFFAOYSA-N beta-D-galactosamine Natural products NC1C(O)OC(CO)C(O)C1O MSWZFWKMSRAUBD-UHFFFAOYSA-N 0.000 description 2
- MSWZFWKMSRAUBD-QZABAPFNSA-N beta-D-glucosamine Chemical compound N[C@H]1[C@H](O)O[C@H](CO)[C@@H](O)[C@@H]1O MSWZFWKMSRAUBD-QZABAPFNSA-N 0.000 description 2
- 239000008366 buffered solution Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- SIYLLGKDQZGJHK-UHFFFAOYSA-N dimethyl-(phenylmethyl)-[2-[2-[4-(2,4,4-trimethylpentan-2-yl)phenoxy]ethoxy]ethyl]ammonium Chemical compound C1=CC(C(C)(C)CC(C)(C)C)=CC=C1OCCOCC[N+](C)(C)CC1=CC=CC=C1 SIYLLGKDQZGJHK-UHFFFAOYSA-N 0.000 description 2
- 150000004676 glycans Chemical class 0.000 description 2
- AEMOLEFTQBMNLQ-CLQWQSTFSA-N l-iduronic acid Chemical compound O[C@H]1O[C@H](C(O)=O)[C@H](O)[C@@H](O)[C@@H]1O AEMOLEFTQBMNLQ-CLQWQSTFSA-N 0.000 description 2
- 238000007726 management method Methods 0.000 description 2
- 230000028161 membrane depolarization Effects 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- 229920001282 polysaccharide Polymers 0.000 description 2
- 239000005017 polysaccharide Substances 0.000 description 2
- 239000008213 purified water Substances 0.000 description 2
- 239000004627 regenerated cellulose Substances 0.000 description 2
- 159000000000 sodium salts Chemical class 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- IAJILQKETJEXLJ-UHFFFAOYSA-N Galacturonsaeure Natural products O=CC(O)C(O)C(O)C(O)C(O)=O IAJILQKETJEXLJ-UHFFFAOYSA-N 0.000 description 1
- 229920002683 Glycosaminoglycan Polymers 0.000 description 1
- 229920002971 Heparan sulfate Polymers 0.000 description 1
- MSFSPUZXLOGKHJ-UHFFFAOYSA-N Muraminsaeure Natural products OC(=O)C(C)OC1C(N)C(O)OC(CO)C1O MSFSPUZXLOGKHJ-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 description 1
- 108010013639 Peptidoglycan Proteins 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000001342 alkaline earth metals Chemical class 0.000 description 1
- AEMOLEFTQBMNLQ-WAXACMCWSA-N alpha-D-glucuronic acid Chemical compound O[C@H]1O[C@H](C(O)=O)[C@@H](O)[C@H](O)[C@H]1O AEMOLEFTQBMNLQ-WAXACMCWSA-N 0.000 description 1
- 230000002785 anti-thrombosis Effects 0.000 description 1
- 229940127219 anticoagulant drug Drugs 0.000 description 1
- 229940127217 antithrombotic drug Drugs 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- UREZNYTWGJKWBI-UHFFFAOYSA-M benzethonium chloride Chemical compound [Cl-].C1=CC(C(C)(C)CC(C)(C)C)=CC=C1OCCOCC[N+](C)(C)CC1=CC=CC=C1 UREZNYTWGJKWBI-UHFFFAOYSA-M 0.000 description 1
- 229960001950 benzethonium chloride Drugs 0.000 description 1
- KCXMKQUNVWSEMD-UHFFFAOYSA-N benzyl chloride Chemical compound ClCC1=CC=CC=C1 KCXMKQUNVWSEMD-UHFFFAOYSA-N 0.000 description 1
- 229940073608 benzyl chloride Drugs 0.000 description 1
- 238000004061 bleaching Methods 0.000 description 1
- 239000000872 buffer Substances 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000007857 degradation product Substances 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002255 enzymatic effect Effects 0.000 description 1
- ZFGMDIBRIDKWMY-PASTXAENSA-N heparin Chemical compound CC(O)=N[C@@H]1[C@@H](O)[C@H](O)[C@@H](COS(O)(=O)=O)O[C@@H]1O[C@@H]1[C@@H](C(O)=O)O[C@@H](O[C@H]2[C@@H]([C@@H](OS(O)(=O)=O)[C@@H](O[C@@H]3[C@@H](OC(O)[C@H](OS(O)(=O)=O)[C@H]3O)C(O)=O)O[C@@H]2O)CS(O)(=O)=O)[C@H](O)[C@H]1O ZFGMDIBRIDKWMY-PASTXAENSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000000968 intestinal effect Effects 0.000 description 1
- 210000004347 intestinal mucosa Anatomy 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000013386 optimize process Methods 0.000 description 1
- 230000000144 pharmacologic effect Effects 0.000 description 1
- 108700015808 potyvirus HC-Pro Proteins 0.000 description 1
- 238000011045 prefiltration Methods 0.000 description 1
- 239000012264 purified product Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000013557 residual solvent Substances 0.000 description 1
- 238000007127 saponification reaction Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08B—POLYSACCHARIDES; DERIVATIVES THEREOF
- C08B37/00—Preparation of polysaccharides not provided for in groups C08B1/00 - C08B35/00; Derivatives thereof
- C08B37/006—Heteroglycans, i.e. polysaccharides having more than one sugar residue in the main chain in either alternating or less regular sequence; Gellans; Succinoglycans; Arabinogalactans; Tragacanth or gum tragacanth or traganth from Astragalus; Gum Karaya from Sterculia urens; Gum Ghatti from Anogeissus latifolia; Derivatives thereof
- C08B37/0063—Glycosaminoglycans or mucopolysaccharides, e.g. keratan sulfate; Derivatives thereof, e.g. fucoidan
- C08B37/0075—Heparin; Heparan sulfate; Derivatives thereof, e.g. heparosan; Purification or extraction methods thereof
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08B—POLYSACCHARIDES; DERIVATIVES THEREOF
- C08B37/00—Preparation of polysaccharides not provided for in groups C08B1/00 - C08B35/00; Derivatives thereof
- C08B37/006—Heteroglycans, i.e. polysaccharides having more than one sugar residue in the main chain in either alternating or less regular sequence; Gellans; Succinoglycans; Arabinogalactans; Tragacanth or gum tragacanth or traganth from Astragalus; Gum Karaya from Sterculia urens; Gum Ghatti from Anogeissus latifolia; Derivatives thereof
- C08B37/0063—Glycosaminoglycans or mucopolysaccharides, e.g. keratan sulfate; Derivatives thereof, e.g. fucoidan
- C08B37/0075—Heparin; Heparan sulfate; Derivatives thereof, e.g. heparosan; Purification or extraction methods thereof
- C08B37/0078—Degradation products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/145—Ultrafiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/16—Feed pretreatment
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L5/00—Compositions of polysaccharides or of their derivatives not provided for in groups C08L1/00 or C08L3/00
- C08L5/10—Heparin; Derivatives thereof
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2649—Filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2315/00—Details relating to the membrane module operation
- B01D2315/10—Cross-flow filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2315/00—Details relating to the membrane module operation
- B01D2315/16—Diafiltration
-
- 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 process for obtaining low molecular weight heparins with a specific molecular weight distribution, which comprises at least one concentration step by tangential flow filtration. Apart from concentration by tangential flow filtration, the process can encompass other steps such as diafiltration or treatment with hydrogen peroxide. Therefore, the present invention can be included in the field of pharmaceutical technology.
- Heparin is a polysaccharide of the family of glycosaminoglycans, formed by uronic acid (L-iduronic acid or D-glucuronic acid) and D-glucosamine, linked alternately.
- L-iduronic acid can be 2-O-sulphated and D-glucosamine can be / V-sulphated and / or 6-O-sulphated, and to a lesser extent / V-acetylated or 3-O-sulphated.
- Heparin is preferably used as a sodium salt, but it can also be used as a salt of other alkali or alkaline earth metals and is mainly used as an antithrombotic and anticoagulant drug.
- Heparins can be classified according to their molecular weight into unfractionated heparin (UFH), low molecular weight heparin (LMWH) and very low molecular weight heparin (HMBPM).
- UH unfractionated heparin
- LMWH low molecular weight heparin
- HMBPM very low molecular weight heparin
- patent CN 103342761 describes a process for the preparation of enoxaparin sodium which includes two ultrafiltrations in series by membranes of 8 KDa and 2 KDa respectively, with the aim of eliminating degradation products and low molecular weight impurities and control the molecular weight and the molecular weight distribution of the product in the presence of alcoholic solvents.
- the purified product Once the purified product has been obtained, it is lyophilized to obtain sodium enoxaparin. In this case, lyophilization is used to eliminate solvents and moisture that could have been lodged in the structure of the enoxaparin sodium obtained from the process of this patent.
- Patent CN 102050888 also describes a final purification process for enoxaparin sodium in the presence of alcoholic solvents with a membrane concentration step of ⁇ 1 KDa and subsequent lyophilization in which the molecular weight and molecular weight distribution of the product are also controlled. .
- lyophilization is used to eliminate solvents and humidity that could have been lodged in the structure of the enoxaparin sodium obtained from the process of this patent.
- a tangential filtration methodology (or TFF for its acronym in English) is used using non-alcoholic diafiltration buffers, which represents a significant advantage over the procedures described in the prior art since in addition the content of residual solvents in the product obtained is minimized, therefore improving the purity profile with respect to these.
- the method designed in the present invention provides a process that can be carried out continuously since it allows the profiling of the product obtained without the need for structural adjustments. This means that with respect to the production processes that involve purification by fractional precipitations, the production time is minimized with the consequent improvement in terms of cost reduction and increased production capacity.
- the crude depolymerized heparin is the product of a heparin depolymerization process.
- the process of the invention excludes the use of fractional precipitation of depolymerized heparin, in particular the use of fractional precipitation of depolymerized heparin produced by depolymerization of heparin is excluded.
- the invention provides embodiments in which low molecular weight heparin is prepared in two main steps: a) depolymerization of heparin to form crude depolymerized heparin; and b) purification of the crude depolymerized heparin by means of TFF (concentration and / or diafiltration using membranes as described below) and without the use of fractional precipitation.
- TFF concentration and / or diafiltration using membranes as described below
- the depolymerized heparin is enoxaparin sodium or bemiparin sodium; preferably enoxaparin sodium.
- crude enoxaparin sodium (or bemiparin sodium) is the product of a heparin depolymerization process.
- the process of the invention excludes the use of fractional precipitation of enoxaparin sodium (or bemiparin sodium), in particular the use of fractional precipitation of enoxaparin sodium (or bemiparin sodium) produced by depolymerization of heparin is excluded.
- the invention provides embodiments in which pure enoxaparin sodium (or bemiparin sodium) is prepared in two steps.
- SUBSTITUTE SHEET (RULE 26) Main: a) depolymerization of heparin to form crude enoxaparin sodium (or bemiparin sodium) without fractional precipitation; and b) purification of crude enoxaparin sodium (or bemiparin sodium) by means of TFF (concentration and / or diafiltration using membranes as described below) and without the use of fractional precipitation.
- TFF concentration and / or diafiltration using membranes as described below
- the molecular weight (Mw) of enoxaparin falls within the following ranges.
- the molecular weight (Mw) of bemiparin falls within the following ranges.
- certain filtration membranes are selected with a defined pore size that allows their use on products in a wide range of molecular weights.
- Generally available membranes range from 1 kDa to 1000 kDa (or ⁇ 1 kDa) nominal cutoff.
- the nominal cutoff or "nominal molecular weight cutoff” (NMWCO) is defined as the minimum molecular weight of a solute that is retained by 90% by the membrane and is determined by evaluating the retention by the membrane of components of different molecular weights ( Figure 6).
- the inventors of the present invention have developed a method that allows the obtaining of LMWH, and specifically of enoxaparin sodium and bemiparin sodium, by concentration by TFF without the need to use alcohols or other organic solvents, or buffered media with salts, obtaining a product with a better purity profile than those methods described in previous documents, with adequate quality attributes, according to the parameters described in the monograph for this product according to the European Pharmacopoeia (latest edition) and the United States Pharmacopoeia (latest edition) .
- the product has an average molecular weight profile and an ideal oligosaccharide chain distribution for its possible pharmacological applications.
- the present invention relates to a process for obtaining low molecular weight heparins (LMWH) with an average molecular weight distribution of between approximately 3.0 and approximately 5.0 KDa, comprising the following steps:
- the solution of step a) is an aqueous solution.
- the heparin concentration in step a) is preferably between about 3% and about 4% w / v, more preferably between about 3.5% and about 4% w / v, even more preferably about 4% w / v.
- the membrane used for concentration by tangential flow filtration has a nominal cut-off of from about 0.7 to about 1 KDa; more preferably from about 0.9 to about 1 KDa. In a particular embodiment, it has a nominal cut of approximately 1 KDa.
- SUBSTITUTE SHEET (RULE 26) Tangential flow filtration (TFF), as well as the rest of the steps of the method of the invention (clarification, depth filtration, diafiltration, treatment with H2O2), can be carried out in the aqueous phase without alcohol or other organic solvents.
- Step b) can include at least one concentration step by tangential flow filtration (TFF) in the aqueous phase using a membrane of approximately ⁇ 1 KDa nominal cut-off, for example 1, 2 or 3, until a maximum concentration of the heparin of approximately 25% w / v.
- TMF tangential flow filtration
- the concentration of the heparin achieved can be at least 5% w / v, preferably at least 8% w / v.
- a heparin concentration of at least 10% w / v is achieved, preferably between about 10% and about 25% w / v; more preferably between about 10% and about 22% w / v; even more preferably between about 10% and about 20%.
- a heparin concentration of between approximately 10% and approximately 22% w / v is achieved.
- a single concentration step is performed by TFF.
- a single concentration stage is carried out by means of TFF until a heparin concentration of at least 10% w / v is achieved, preferably between approximately 10% and approximately 22% w / v, plus preferably between about 12% and about 22% w / v.
- a single concentration step is carried out by means of TFF until achieving a heparin concentration of at least 5% w / v; preferably at least 10% w / v, more preferably between about 5% and about 15% w / v or between about 10% and about 22%.
- the method of the invention comprises:
- TMF tangential flow filtration
- step b) includes two steps of concentration by TFF.
- a first concentration is carried out by means of TFF until a concentration of the heparin of between approximately 4% and approximately 10% w / v is achieved, preferably between approximately 5% and approximately 10% w / v , and a second concentration step by means of TFF until achieving a heparin concentration of between approximately 10% to approximately 25% w / v.
- the second concentration step achieves a heparin concentration of between about 12% and about 25%, more preferably between about 12% and about 22% w / v.
- a concentration is carried out by TFF, in a single step, from approximately 4% w / v to approximately 12-22% w / v (or approximately 10-25% w / v).
- the process of the invention may include one or more additional steps such as clarification, depth filtration, diafiltration with water, treatment with hydrogen peroxide or lyophilization.
- step (a) At least one clarification step of the heparin solution of step (a) is carried out.
- At least one depth filtration step is performed which may be prior or subsequent to any of the TFF concentration steps. For example, before or after the TFF concentration step (if only one is carried out) or the first TFF concentration step in case step b) comprises more than one TFF concentration step in case the step b) comprises more than one TFF concentration step.
- At least one diafiltration step is carried out with water, which can be before or after any of the TFF concentration steps.
- the TFF concentration stage or the first TFF concentration stage in case stage b) comprises more than one TFF concentration stage in case stage b) comprises more than one TFF concentration stage.
- a treatment step with H2O2 is carried out, which may be prior to the TFF concentration step or prior to any of the concentration steps in case step b) comprises more than one TFF concentration step.
- step b) comprises two TFF concentration steps
- a treatment step with H2O2 can be carried out prior to the first concentration step or prior to the second concentration step.
- At least one diafiltration step with water is carried out, which may be prior to the TFF concentration step or the TFF concentration step or the first TFF concentration step (in case step b) comprises more than one TFF concentration step) or prior to the HO treatment step mentioned above.
- a lyophilization step of the concentrate obtained in step (b) is carried out.
- BRM is understood to be heparins with an average molecular weight less than about 8000 Da.
- the membranes available for use are limited since the ideal is that they present a lower cutoff of the average molecular weight of LMWH so as to allow removal of low molecular weight impurities without loss of oligosaccharide chains.
- the nominal cut-off of the membranes used is ⁇ 1 kDa, although this can be varied depending on the molecular weights to be obtained.
- the maintenance steps that may be required for cleaning and / or regeneration of the membranes are preferably carried out, using water, NaOH or any other product. in accordance with their specifications.
- Figure 2 General diagram of the tangential filtration procedure.
- FIGS 4A and 4B Schemes of the purification process according to the invention.
- Figures 5A-5D Includes various graphs that represent that the variation both in average molecular weight (FIG. 5A) and in the distribution of molecular weights (FIG. 5B: ⁇ 2000 KDa; FIG. 5C:> 8000KDa; FIG. 5D: 2000-8000 KDa) is linear during the second concentration from 10% to 20% of the nominal concentration of the product in the retentate.
- tangential flow filtration or “TFF” is understood as the filtration technique in which the solution to be filtered passes tangentially over the filter surface, so that the pressure difference that is generated allows the components that are smaller than pore size pass through (permeate).
- the oversized components are retained by passing over the filter surface and back into the feed tank (retained).
- clarification is understood as the filtration that is carried out to eliminate suspended particles present in the solution, such as filtration carried out with filters of between 1-60 microns, preferably between 1-25 microns. .
- depth filtration is understood as that filtration in which a filter medium with multiple labyrinth-shaped passages is used, which helps to retain the particles. The larger ones will be retained on the surface and the finer ones continue their way towards the interior of the filter medium, being trapped in the internal layers, so that the turbidity of the solution is reduced.
- it is a filtration carried out with filters of between 1-5 microns, preferably between 2-4 microns. Filtration can be accomplished with the use of water or buffered solution.
- concentration is understood as the tangential filtration stage in which the retained product increases its concentration in the solution as permeate is eliminated (see Figure 3).
- diafiltration is understood as the tangential filtration stage in which, while the permeate is eliminated, the solution is fed with
- a membrane can be used as in concentration by TFF, i.e. a membrane of about ⁇ 1 KDa nominal cutoff, preferably about 0.7 to about 1 KDa, more preferably about 0.9 to about 1 KDa , even more referable about 1 KDa.
- the heparin (after depolymerization) is a sodium salt of heparin, eg, enoxaparin sodium or bemiparin sodium.
- Crude enoxaparin sodium can be obtained by alkaline depolymerization (e.g. NaOH) of heparin benzyl ester obtained from porcine intestinal mucosa.
- the product obtained after the depolymerization of enoxaparin sodium corresponds to a solution that, in addition to containing crude enoxaparin sodium, contains impurities corresponding to the saponification in alkaline medium of the benzyl ester of heparin, in addition to salts corresponding to the adjustments of pH carried out during the breaking process.
- the TFF process is carried out on this crude enoxaparin sodium solution, so that the concentration of this solution is carried out with the objective, on the one hand, of eliminating low molecular weight impurities, and on the other, to reach the adequate concentration to carry out the bleaching treatment with hydrogen peroxide.
- the decolorizing treatment with H2O2 could be carried out before the concentration step by TFF.
- the decolorizing treatment with H2O2 could be carried out before the concentration step by TFF.
- a diafiltration process for exhaustive removal of low molecular weight impurities, before or after the concentration step.
- a second concentration is carried out in order to eliminate the saline impurities generated and adjust the content of low molecular weight oligosaccharide chains, for which the average molecular weight of the solution is monitored; Once the optimal value is reached, it is lyophilized to obtain sodium enoxaparin of the appropriate purity.
- the method of the invention comprises: a) providing a solution of depolymerized enoxaparin sodium with a distribution range of oligosaccharide chains of between approximately 0.6 to approximately 10 KDa and an enoxaparin sodium concentration of up to
- b) carry out a concentration step by means of TFF in the aqueous phase using a membrane of ⁇ 1 KDa of nominal cut-off until achieving a heparin concentration of up to approximately 25% w / v, up to approximately 10% w / v, or preferably between about 5% and about 10% w / v; c) optionally, carry out a diafiltration step with water (eg non-buffered water) before or after step b),
- water eg non-buffered water
- step d) carry out a treatment step with H2O2 before or after step b), e) optionally, carry out a second concentration step by means of TFF in the aqueous phase using a membrane of ⁇ 1 KDa of nominal cut-off until a heparin concentration is achieved up to about 25% w / v, preferably between about 12% and about 25% w / v, and f) carrying out a lyophilization step of the product obtained.
- the method of the invention comprises:
- b) carry out a concentration step by means of TFF in the aqueous phase using a membrane of ⁇ 1 KDa of nominal cut-off until achieving a heparin concentration of up to approximately 25% w / v, up to approximately 10% w / v, or preferably between about 5% and about 10% w / v; c) carry out a treatment step with H2O2 of the product obtained in step b), d) carry out a second concentration step by means of TFF in the aqueous phase using a membrane of ⁇ 1 KDa of nominal cut-off until a heparin concentration of up to about 25% w / v, preferably between about 12% and about 25% w / v; and e) carrying out a lyophilization step of the product obtained.
- the method of this embodiment includes a step of
- the method of the invention comprises:
- SUBSTITUTE SHEET (RULE 26) b) carry out a concentration step by means of TFF in the aqueous phase using a membrane of ⁇ 1 KDa of nominal cut-off until achieving a heparin concentration of up to approximately 25% w / v, up to approximately 10% w / v, or preferably between about 5% and about 10% w / v; c) carry out a stage of diafiltration with water of the product obtained in stage b), d) carry out a stage of treatment with H2O2 of the product obtained in stage c), e) optionally, carry out a stage of depth filtration of the product obtained in step d),
- the method of this embodiment includes a step of
- the method of the invention comprises:
- b) carry out a concentration step by means of TFF in the aqueous phase using a membrane of ⁇ 1 KDa of nominal cut-off until achieving a heparin concentration of up to 25% w / v, preferably between approximately 5% and approximately 10% w / v ;
- step d) carry out a treatment step with H2O2 of the product obtained in step c), e) carry out a second concentration step by means of TFF in the aqueous phase using a membrane of ⁇ 1 KDa of nominal cut-off until a heparin concentration of up to about 25% w / v, preferably between about 12% and about 25% w / v; and f) carrying out a lyophilization step of the product obtained.
- the method of this embodiment includes a step of
- the method of the invention comprises:
- b) carry out a stage of diafiltration with water of the solution of stage a), c) carry out a stage of treatment with H2O2 of the product obtained in stage c), d) carry out a concentration stage by means of TFF in aqueous phase using a ⁇ 1 kDa nominal cutoff membrane to achieve a heparin concentration of up to about 25% w / v, preferably between about 5% and about 20% w / v; Y
- the method of this embodiment includes a step of
- SUBSTITUTE SHEET (RULE 26) a) first concentration by TFF to obtain a product with a heparin concentration of 4% to 10% w / v;
- crude enoxaparin sodium was used as the starting product with a product concentration of 40 g / L and an oligosaccharide chain distribution between 0.6 and 10 KDa.
- This initial product was pre-filtered with a 3.0 pm Clarigard ® filter.
- Crude Enoxaparin Sodium is a product of the heparin depolymerization process.
- the first concentration stage was carried out using TFF, aimed at increasing the concentration of enoxaparin to a value between 4% and 10%, as well as reducing the concentration of contaminants (mainly salts with a molecular weight ⁇ 0.5 KDa and other small products resulting from previous manufacturing procedures).
- a Millipore ® regenerated cellulose membrane with a nominal cutoff of ⁇ 1 KDa was used.
- the concentration stage started with approximately 2005 g of product with a transmembrane pressure (TMP) of 3.25 bar prior to passing the permeate flow to a separate container, the system was kept in total recirculation for about 15 minutes.
- TMP transmembrane pressure
- a second concentration stage was carried out using TFF, destined this time to reach an enoxaparin concentration of between 10% and 20% w / v, also using a Millipore ® regenerated cellulose membrane of ⁇ 1 Nominal cutoff KDa.
- Table 3 shows the molecular weights of the samples taken during the process described above, analyzed according to the method established by the European Pharmacopoeia (EP).
- the process of the invention was carried out following the following main steps: a) First concentration by TFF to obtain a product with a heparin concentration from 4% to 10% w / v;
- SUBSTITUTE SHEET (RULE 26) concentration P8.
- a sample of the retentate volume was also collected at the end of the concentration (R4), after having depolarized the membrane by leaving the system operating at a low TMP (0.8 bar) for 10 minutes.
- Table 4 shows the molecular weights of the samples taken during the process described above, analyzed according to the method established by the European Pharmacopoeia (EP).
- the process of the invention was carried out following the following main steps: a) First concentration by TFF to obtain a product with a heparin concentration from 4% to 10% w / v;
- the permeate flux ranged from an initial 9.6 to a final 3.9 LMH (41% of the initial flux), for an average flux of 5.8 LMH.
- a sample of the initial feed (BT) was also taken, before its transfer to the tank.
- the RT solution was passed through a Millistak + ® HC Pro C0SP depth filter, reducing the turbidity to 0.57 NTU, to be subsequently treated with H2O2. Approximately 0.8 liters of product were transferred to the tank after having been treated with H2O2 and the second concentration step was carried out.
- This second concentration was performed by taking aliquots sequentially of both the retentate and the permeate, from the initial nominal concentration of 10% (samples R'3 and P'3, respectively) to the final nominal concentration of 20% (samples R'12 and R ⁇ 2, respectively), passing through intermediate concentrations of 1 1, 12, 13, 14, 15, 16, 17, 18 and 19%.
- Table 5 shows the molecular weights of the samples taken during the process described above, analyzed according to the method established by the European Pharmacopoeia (EP).
- Example 4 The product obtained in the previous example is analyzed for its anti-FXa and anti-FIla activities. The results obtained were the following:
- Example 5 The process of the invention was carried out following the following main steps: a) Diafiltration;
- the permeate flux ranged from an initial 17.7 to a final 13.1 LMH, with an average flux of 12.6 LMH, and for 6 diavolumes.
- samples of both the permeate (DP1 to DP6) and the retentate (DR1 to DR6) were collected.
- the permeate is treated with H2O2 and approximately 2720 g of treated product is transferred to the tank.
- the permeate flux ranged from 12.7 initial to 1.28 final LMH (89.9% reduction), for an average flux of 5.1 LMH.
- the concentration was made from 4 to 15%, collecting both a permeate sample (CP1 to CP6) and a retentate (CR1 to CR6) from 10%.
- a sample of the retentate volume was also collected at the end of the concentration (R4), after having depolarized the membrane by leaving the system operating at a low TMP (0.8 bar) for 10 minutes.
- Table 6 shows the molecular weights of the samples taken during the process described above, analyzed according to the method established by the European Pharmacopoeia (EP).
- the variation in both the average molecular weight and the molecular weight distribution is linear from 10% to 15% of the nominal concentration of the product in the retentate, so that, adjusting the final value of the concentration of the product in the solution of the retained, it is possible to define a certain profile of molecular weights and distribution of oligosaccharide chains to obtain enoxaparin sodium.
- the retentate solution is lyophilized to obtain dry enoxaparin sodium.
- Example 6 The product obtained in the previous example is analyzed for its anti-FXa and anti-FIla activities. The results obtained were as follows.
- the term "about” is taken to mean ⁇ 10%, ⁇ 5%, or ⁇ 1% of a specified value, preferably ⁇ 10%.
Landscapes
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Polymers & Plastics (AREA)
- Medicinal Chemistry (AREA)
- Molecular Biology (AREA)
- Materials Engineering (AREA)
- Biochemistry (AREA)
- General Health & Medical Sciences (AREA)
- Water Supply & Treatment (AREA)
- Polysaccharides And Polysaccharide Derivatives (AREA)
- Pharmaceuticals Containing Other Organic And Inorganic Compounds (AREA)
Abstract
Description
Claims
Priority Applications (15)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PE2021001650A PE20212330A1 (es) | 2019-04-26 | 2020-04-24 | Procedimiento de obtencion de heparinas de bajo peso molecular por filtracion de flujo tangencial |
KR1020217032026A KR20220005441A (ko) | 2019-04-26 | 2020-04-24 | 접선유동여과법에 의해 저분자량 헤파린을 얻는 방법 |
CA3134458A CA3134458C (en) | 2019-04-26 | 2020-04-24 | Method for obtaining low-molecular-weight heparins by means of tangential flow filtration |
ES202090025A ES2888148B2 (es) | 2019-04-26 | 2020-04-24 | Procedimiento de obtencion de heparinas de bajo peso molecular por filtracion de flujo tangencial |
MX2021011671A MX2021011671A (es) | 2019-04-26 | 2020-04-24 | Procedimiento de obtencion de heparinas de bajo peso molecular por filtracion de flujo tangencial. |
AU2020263142A AU2020263142A1 (en) | 2019-04-26 | 2020-04-24 | Method for obtaining low-molecular-weight heparins by means of tangential flow filtration |
BR112021020048A BR112021020048A2 (pt) | 2019-04-26 | 2020-04-24 | Método para obtenção de heparinas de baixo peso molecular através de filtração de fluxo tangencial |
SG11202111009WA SG11202111009WA (en) | 2019-04-26 | 2020-04-24 | Method for obtaining low-molecular-weight heparins by means of tangential flow filtration |
CN202080001040.1A CN112673027A (zh) | 2019-04-26 | 2020-04-24 | 通过切向流过滤获得低分子量肝素的方法 |
JP2021559706A JP2022530321A (ja) | 2019-04-26 | 2020-04-24 | タンジェンシャルフロー濾過により低分子量ヘパリンを得る方法 |
EP20794489.3A EP3943513A4 (en) | 2019-04-26 | 2020-04-24 | METHOD FOR OBTAINING LOW MOLECULAR WEIGHT HEPARIN BY TANGENTIAL FLOW FILTRATION |
IL286931A IL286931A (en) | 2019-04-26 | 2021-10-03 | A method for obtaining low molecular weight heparins using tangential flow filtration |
CONC2021/0013320A CO2021013320A2 (es) | 2019-04-26 | 2021-10-05 | Procedimiento de obtención de heparinas de bajo peso molecular por filtración de flujo tangencial |
US17/509,255 US20220112315A1 (en) | 2019-04-26 | 2021-10-25 | Method for Obtaining Low Molecular Weight Heparins by Tangential Flow Filtration |
ZA2021/09022A ZA202109022B (en) | 2019-04-26 | 2021-11-12 | Method for obtaining low-molecular-weight heparins by means of tangential flow filtration |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
ES201930373 | 2019-04-26 | ||
ESP201930373 | 2019-04-26 | ||
CN202010078241 | 2020-01-23 | ||
CN202010078241.3 | 2020-01-23 |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US17/509,255 Continuation-In-Part US20220112315A1 (en) | 2019-04-26 | 2021-10-25 | Method for Obtaining Low Molecular Weight Heparins by Tangential Flow Filtration |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2020216981A1 true WO2020216981A1 (es) | 2020-10-29 |
Family
ID=72941056
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/ES2020/070263 WO2020216981A1 (es) | 2019-04-26 | 2020-04-24 | Procedimiento de obtención de heparinas de bajo peso molecular por filtración de flujo tangencial |
Country Status (18)
Country | Link |
---|---|
US (1) | US20220112315A1 (es) |
EP (1) | EP3943513A4 (es) |
JP (1) | JP2022530321A (es) |
KR (1) | KR20220005441A (es) |
AU (1) | AU2020263142A1 (es) |
BR (1) | BR112021020048A2 (es) |
CA (1) | CA3134458C (es) |
CL (1) | CL2021002647A1 (es) |
CO (1) | CO2021013320A2 (es) |
ES (1) | ES2888148B2 (es) |
GE (1) | GEP20247598B (es) |
IL (1) | IL286931A (es) |
MA (1) | MA55388A (es) |
MX (1) | MX2021011671A (es) |
PE (1) | PE20212330A1 (es) |
SG (1) | SG11202111009WA (es) |
WO (1) | WO2020216981A1 (es) |
ZA (1) | ZA202109022B (es) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR20240006648A (ko) * | 2021-05-12 | 2024-01-15 | 넥서스 다이애그노스틱스, 인코포레이티드 | 고분자량 헤파린 화합물의 제조 방법 |
Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5110918A (en) | 1986-05-16 | 1992-05-05 | Sanofi S.A. | Process for preparing EDTA-free heparins, heparin fractions and fragments |
US5767269A (en) | 1996-10-01 | 1998-06-16 | Hamilton Civic Hospitals Research Development Inc. | Processes for the preparation of low-affinity, low molecular weight heparins useful as antithrombotics |
ES2161615A1 (es) | 1999-07-23 | 2001-12-01 | Rovi Lab Farmaceut Sa | Composiciones de heparinas de muy bajo peso molecular. |
US20070154492A1 (en) | 2006-01-13 | 2007-07-05 | Baxter International Inc. | Method for Purifying Polysaccharides |
US20090105194A1 (en) | 2005-05-09 | 2009-04-23 | Universitetet For Miljo-Og Biovitenskap | Process for the production of a low molecular weight heparin |
WO2010111710A1 (en) | 2009-03-27 | 2010-09-30 | Solazyme, Inc. | Microalgal polysaccharide compositions |
CN102050888A (zh) | 2010-12-13 | 2011-05-11 | 河北常山生化药业股份有限公司 | 一种依诺肝素钠的制备方法 |
CN103342761A (zh) | 2013-07-15 | 2013-10-09 | 河北常山生化药业股份有限公司 | 一种膜分离制备依诺肝素钠工艺 |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102731683A (zh) * | 2012-07-17 | 2012-10-17 | 湖北亿诺瑞生物制药有限公司 | 一种从肝素废液中分离天然低分子肝素的方法 |
CN103936889A (zh) * | 2014-03-19 | 2014-07-23 | 苏州英诺凯生物医药科技有限公司 | 一种使用切向流过滤纯化依诺肝素的方法 |
-
2020
- 2020-04-24 KR KR1020217032026A patent/KR20220005441A/ko active Search and Examination
- 2020-04-24 GE GEAP202015747A patent/GEP20247598B/en unknown
- 2020-04-24 SG SG11202111009WA patent/SG11202111009WA/en unknown
- 2020-04-24 JP JP2021559706A patent/JP2022530321A/ja active Pending
- 2020-04-24 MX MX2021011671A patent/MX2021011671A/es unknown
- 2020-04-24 CA CA3134458A patent/CA3134458C/en active Active
- 2020-04-24 BR BR112021020048A patent/BR112021020048A2/pt unknown
- 2020-04-24 AU AU2020263142A patent/AU2020263142A1/en active Pending
- 2020-04-24 EP EP20794489.3A patent/EP3943513A4/en active Pending
- 2020-04-24 ES ES202090025A patent/ES2888148B2/es active Active
- 2020-04-24 WO PCT/ES2020/070263 patent/WO2020216981A1/es active Application Filing
- 2020-04-24 PE PE2021001650A patent/PE20212330A1/es unknown
- 2020-04-24 MA MA055388A patent/MA55388A/fr unknown
-
2021
- 2021-10-03 IL IL286931A patent/IL286931A/en unknown
- 2021-10-05 CO CONC2021/0013320A patent/CO2021013320A2/es unknown
- 2021-10-08 CL CL2021002647A patent/CL2021002647A1/es unknown
- 2021-10-25 US US17/509,255 patent/US20220112315A1/en active Pending
- 2021-11-12 ZA ZA2021/09022A patent/ZA202109022B/en unknown
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5110918A (en) | 1986-05-16 | 1992-05-05 | Sanofi S.A. | Process for preparing EDTA-free heparins, heparin fractions and fragments |
US5767269A (en) | 1996-10-01 | 1998-06-16 | Hamilton Civic Hospitals Research Development Inc. | Processes for the preparation of low-affinity, low molecular weight heparins useful as antithrombotics |
ES2161615A1 (es) | 1999-07-23 | 2001-12-01 | Rovi Lab Farmaceut Sa | Composiciones de heparinas de muy bajo peso molecular. |
US20090105194A1 (en) | 2005-05-09 | 2009-04-23 | Universitetet For Miljo-Og Biovitenskap | Process for the production of a low molecular weight heparin |
US20070154492A1 (en) | 2006-01-13 | 2007-07-05 | Baxter International Inc. | Method for Purifying Polysaccharides |
WO2010111710A1 (en) | 2009-03-27 | 2010-09-30 | Solazyme, Inc. | Microalgal polysaccharide compositions |
CN102050888A (zh) | 2010-12-13 | 2011-05-11 | 河北常山生化药业股份有限公司 | 一种依诺肝素钠的制备方法 |
CN103342761A (zh) | 2013-07-15 | 2013-10-09 | 河北常山生化药业股份有限公司 | 一种膜分离制备依诺肝素钠工艺 |
Non-Patent Citations (2)
Title |
---|
"Isolation and characterization of heparan sulfate from crude porcine intestinal mucosal peptidoglycan heparin", CARBOHYD. RES., vol. 276, 1995, pages 183 - 197 |
ANONYMOUS: "Protein Concentration and Diafiltration by Tangential Flow Filtration", MILLIPORE TECHNICAL BRIEF., 1 January 2003 (2003-01-01), XP055553019, Retrieved from the Internet <URL:http://wolfson.huji.ac.il/purification/PDF/dialysis/MILLIPORE_TFF.pdf> [retrieved on 20200220] * |
Also Published As
Publication number | Publication date |
---|---|
JP2022530321A (ja) | 2022-06-29 |
MA55388A (fr) | 2022-01-26 |
EP3943513A4 (en) | 2022-12-21 |
CA3134458A1 (en) | 2020-10-29 |
US20220112315A1 (en) | 2022-04-14 |
CO2021013320A2 (es) | 2022-03-18 |
MX2021011671A (es) | 2021-10-22 |
KR20220005441A (ko) | 2022-01-13 |
CL2021002647A1 (es) | 2022-05-13 |
EP3943513A1 (en) | 2022-01-26 |
ES2888148B2 (es) | 2022-11-14 |
PE20212330A1 (es) | 2021-12-14 |
IL286931A (en) | 2021-10-31 |
BR112021020048A2 (pt) | 2021-12-07 |
GEP20247598B (en) | 2024-02-26 |
ES2888148A1 (es) | 2021-12-30 |
CA3134458C (en) | 2023-11-21 |
AU2020263142A1 (en) | 2021-10-28 |
ZA202109022B (en) | 2023-10-25 |
SG11202111009WA (en) | 2021-11-29 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN103275246B (zh) | 一种那曲肝素钙生产方法 | |
KR100528551B1 (ko) | 이눌린생성물의제조방법 | |
BR112012003128B1 (pt) | Processos para recuperar um ácido inorgânico de licor residual aquoso, e para produzir celulose nanocristalina. | |
JP2886127B2 (ja) | 水溶性シクロデキストリン誘導体の浄化方法 | |
CN102731683A (zh) | 一种从肝素废液中分离天然低分子肝素的方法 | |
EA039639B1 (ru) | Способ экстракции и очистки гиалуроновой кислоты | |
WO2018043668A1 (ja) | ポリ硫酸ペントサンの製造方法 | |
ES2888148B2 (es) | Procedimiento de obtencion de heparinas de bajo peso molecular por filtracion de flujo tangencial | |
PL200677B1 (pl) | Sposób oczyszczania wysokocząsteczkowego kwasu hialuronowego | |
KR101638662B1 (ko) | 히알루론산 및/또는 그의 염의 정제 방법 | |
JPH0631144A (ja) | 酢酸セルロースまたは酢酸セルロース誘導体からなる貫通する内部空隙を有する中空糸の形の透析膜およびその製造法 | |
DE19750527C2 (de) | Cellulosische Trennmembran | |
WO2019000336A1 (zh) | 低分子肝素那曲肝素钙标准品库及其制备方法 | |
JPS59149901A (ja) | ヘパリンの精製および分別方法 | |
WO2007013123A1 (en) | Cyclodextrins for blood detoxification | |
CN112673027A (zh) | 通过切向流过滤获得低分子量肝素的方法 | |
OA20550A (en) | Method for obtaining low molecular weight heparins by tangential flow filtration. | |
WO2019000335A1 (zh) | 一种低分子肝素达肝素钠标准品库及其制备方法 | |
JP2893451B2 (ja) | 高分子量のヒアルロン酸を製造する方法 | |
JP5516835B2 (ja) | 多段積多層平膜 | |
JPH0734750B2 (ja) | エリスリトールの分離・回収方法 | |
JP3372638B2 (ja) | ウイルスの通過を阻止する物質からなる濾過助剤およびそれを使用した濾過方法 | |
WO2022062011A1 (zh) | 一种使用切向流超滤纯化低分子量岩藻糖化糖胺聚糖的方法 | |
CN102988989B (zh) | 一种代血浆的膜分离精制提纯方法 | |
CN114249843A (zh) | 一种使用切向流超滤纯化低分子量岩藻糖化糖胺聚糖的方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 20794489 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 3134458 Country of ref document: CA |
|
ENP | Entry into the national phase |
Ref document number: 15747 Country of ref document: GE |
|
ENP | Entry into the national phase |
Ref document number: 2021559706 Country of ref document: JP Kind code of ref document: A |
|
REG | Reference to national code |
Ref country code: BR Ref legal event code: B01A Ref document number: 112021020048 Country of ref document: BR |
|
ENP | Entry into the national phase |
Ref document number: 2020794489 Country of ref document: EP Effective date: 20211019 |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
ENP | Entry into the national phase |
Ref document number: 2020263142 Country of ref document: AU Date of ref document: 20200424 Kind code of ref document: A |
|
ENP | Entry into the national phase |
Ref document number: 112021020048 Country of ref document: BR Kind code of ref document: A2 Effective date: 20211005 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 521430496 Country of ref document: SA |