CN105777804B - A kind of method of aqueous two-phase system purification egg yolk lecithin - Google Patents
A kind of method of aqueous two-phase system purification egg yolk lecithin Download PDFInfo
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- CN105777804B CN105777804B CN201610221898.4A CN201610221898A CN105777804B CN 105777804 B CN105777804 B CN 105777804B CN 201610221898 A CN201610221898 A CN 201610221898A CN 105777804 B CN105777804 B CN 105777804B
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- 238000000034 method Methods 0.000 title claims abstract description 35
- JQWAHKMIYCERGA-UHFFFAOYSA-N (2-nonanoyloxy-3-octadeca-9,12-dienoyloxypropoxy)-[2-(trimethylazaniumyl)ethyl]phosphinate Chemical compound CCCCCCCCC(=O)OC(COP([O-])(=O)CC[N+](C)(C)C)COC(=O)CCCCCCCC=CCC=CCCCCC JQWAHKMIYCERGA-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 238000000746 purification Methods 0.000 title claims abstract description 18
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims abstract description 28
- 210000002969 egg yolk Anatomy 0.000 claims abstract description 14
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 claims abstract description 12
- 150000003904 phospholipids Chemical class 0.000 claims abstract description 9
- 239000000843 powder Substances 0.000 claims abstract description 8
- 150000002191 fatty alcohols Chemical class 0.000 claims abstract description 7
- 239000002994 raw material Substances 0.000 claims abstract description 7
- 238000013517 stratification Methods 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 44
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 31
- 235000019441 ethanol Nutrition 0.000 claims description 18
- 238000000926 separation method Methods 0.000 claims description 15
- 235000002639 sodium chloride Nutrition 0.000 claims description 15
- 238000003756 stirring Methods 0.000 claims description 14
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 10
- 150000003839 salts Chemical class 0.000 claims description 10
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 5
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 5
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 5
- 239000011780 sodium chloride Substances 0.000 claims description 5
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 claims description 4
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 claims description 4
- ZPWVASYFFYYZEW-UHFFFAOYSA-L dipotassium hydrogen phosphate Chemical compound [K+].[K+].OP([O-])([O-])=O ZPWVASYFFYYZEW-UHFFFAOYSA-L 0.000 claims description 2
- 229910000396 dipotassium phosphate Inorganic materials 0.000 claims description 2
- 235000019797 dipotassium phosphate Nutrition 0.000 claims description 2
- FBAFATDZDUQKNH-UHFFFAOYSA-M iron chloride Chemical compound [Cl-].[Fe] FBAFATDZDUQKNH-UHFFFAOYSA-M 0.000 claims description 2
- 229910000402 monopotassium phosphate Inorganic materials 0.000 claims description 2
- 235000019796 monopotassium phosphate Nutrition 0.000 claims description 2
- PJNZPQUBCPKICU-UHFFFAOYSA-N phosphoric acid;potassium Chemical compound [K].OP(O)(O)=O PJNZPQUBCPKICU-UHFFFAOYSA-N 0.000 claims description 2
- 235000005074 zinc chloride Nutrition 0.000 claims description 2
- 239000011592 zinc chloride Substances 0.000 claims description 2
- AQEFLFZSWDEAIP-UHFFFAOYSA-N di-tert-butyl ether Chemical compound CC(C)(C)OC(C)(C)C AQEFLFZSWDEAIP-UHFFFAOYSA-N 0.000 claims 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 claims 1
- 239000000243 solution Substances 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000003960 organic solvent Substances 0.000 abstract description 4
- 229910017053 inorganic salt Inorganic materials 0.000 abstract description 2
- 239000012266 salt solution Substances 0.000 abstract description 2
- 239000012071 phase Substances 0.000 description 43
- 239000000787 lecithin Substances 0.000 description 32
- 229940067606 lecithin Drugs 0.000 description 32
- IIZPXYDJLKNOIY-JXPKJXOSSA-N 1-palmitoyl-2-arachidonoyl-sn-glycero-3-phosphocholine Chemical compound CCCCCCCCCCCCCCCC(=O)OC[C@H](COP([O-])(=O)OCC[N+](C)(C)C)OC(=O)CCC\C=C/C\C=C/C\C=C/C\C=C/CCCCC IIZPXYDJLKNOIY-JXPKJXOSSA-N 0.000 description 30
- 235000010445 lecithin Nutrition 0.000 description 30
- WTJKGGKOPKCXLL-RRHRGVEJSA-N phosphatidylcholine Chemical compound CCCCCCCCCCCCCCCC(=O)OC[C@H](COP([O-])(=O)OCC[N+](C)(C)C)OC(=O)CCCCCCCC=CCCCCCCCC WTJKGGKOPKCXLL-RRHRGVEJSA-N 0.000 description 17
- 238000000605 extraction Methods 0.000 description 14
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 10
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- 239000002904 solvent Substances 0.000 description 7
- 238000000638 solvent extraction Methods 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 238000004440 column chromatography Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 239000008346 aqueous phase Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 5
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 239000003480 eluent Substances 0.000 description 4
- 239000004519 grease Substances 0.000 description 4
- 239000012528 membrane Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- JZNWSCPGTDBMEW-UHFFFAOYSA-N Glycerophosphorylethanolamin Natural products NCCOP(O)(=O)OCC(O)CO JZNWSCPGTDBMEW-UHFFFAOYSA-N 0.000 description 3
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000003814 drug Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 150000008104 phosphatidylethanolamines Chemical class 0.000 description 3
- 150000003905 phosphatidylinositols Chemical class 0.000 description 3
- 229940067626 phosphatidylinositols Drugs 0.000 description 3
- 239000011347 resin Substances 0.000 description 3
- 229920005989 resin Polymers 0.000 description 3
- 239000000741 silica gel Substances 0.000 description 3
- 229910002027 silica gel Inorganic materials 0.000 description 3
- RYCNUMLMNKHWPZ-SNVBAGLBSA-N 1-acetyl-sn-glycero-3-phosphocholine Chemical compound CC(=O)OC[C@@H](O)COP([O-])(=O)OCC[N+](C)(C)C RYCNUMLMNKHWPZ-SNVBAGLBSA-N 0.000 description 2
- CFWRDBDJAOHXSH-SECBINFHSA-N 2-azaniumylethyl [(2r)-2,3-diacetyloxypropyl] phosphate Chemical compound CC(=O)OC[C@@H](OC(C)=O)COP(O)(=O)OCCN CFWRDBDJAOHXSH-SECBINFHSA-N 0.000 description 2
- ZCYVEMRRCGMTRW-UHFFFAOYSA-N 7553-56-2 Chemical compound [I] ZCYVEMRRCGMTRW-UHFFFAOYSA-N 0.000 description 2
- 102000004190 Enzymes Human genes 0.000 description 2
- 108090000790 Enzymes Proteins 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- HVYWMOMLDIMFJA-DPAQBDIFSA-N cholesterol Chemical compound C1C=C2C[C@@H](O)CC[C@]2(C)[C@@H]2[C@@H]1[C@@H]1CC[C@H]([C@H](C)CCCC(C)C)[C@@]1(C)CC2 HVYWMOMLDIMFJA-DPAQBDIFSA-N 0.000 description 2
- 238000004587 chromatography analysis Methods 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 238000006911 enzymatic reaction Methods 0.000 description 2
- 238000004128 high performance liquid chromatography Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000011630 iodine Substances 0.000 description 2
- 229910052740 iodine Inorganic materials 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- 150000002978 peroxides Chemical class 0.000 description 2
- 102000004169 proteins and genes Human genes 0.000 description 2
- 108090000623 proteins and genes Proteins 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000013268 sustained release Methods 0.000 description 2
- 239000012730 sustained-release form Substances 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- JLPULHDHAOZNQI-ZTIMHPMXSA-N 1-hexadecanoyl-2-(9Z,12Z-octadecadienoyl)-sn-glycero-3-phosphocholine Chemical compound CCCCCCCCCCCCCCCC(=O)OC[C@H](COP([O-])(=O)OCC[N+](C)(C)C)OC(=O)CCCCCCC\C=C/C\C=C/CCCCC JLPULHDHAOZNQI-ZTIMHPMXSA-N 0.000 description 1
- 240000007124 Brassica oleracea Species 0.000 description 1
- 235000003899 Brassica oleracea var acephala Nutrition 0.000 description 1
- 235000011301 Brassica oleracea var capitata Nutrition 0.000 description 1
- 235000001169 Brassica oleracea var oleracea Nutrition 0.000 description 1
- 208000024172 Cardiovascular disease Diseases 0.000 description 1
- 230000005526 G1 to G0 transition Effects 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 125000001931 aliphatic group Chemical group 0.000 description 1
- 230000001093 anti-cancer Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000004071 biological effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 235000012000 cholesterol Nutrition 0.000 description 1
- 230000000536 complexating effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 201000010099 disease Diseases 0.000 description 1
- 208000037265 diseases, disorders, signs and symptoms Diseases 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 150000002170 ethers Chemical class 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 235000013373 food additive Nutrition 0.000 description 1
- 239000002778 food additive Substances 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 125000005456 glyceride group Chemical group 0.000 description 1
- -1 grease Chemical class 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 208000006454 hepatitis Diseases 0.000 description 1
- 231100000283 hepatitis Toxicity 0.000 description 1
- 230000002209 hydrophobic effect Effects 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 150000002632 lipids Chemical class 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000012046 mixed solvent Substances 0.000 description 1
- 239000005445 natural material Substances 0.000 description 1
- 229930014626 natural product Natural products 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000825 pharmaceutical preparation Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000002798 polar solvent Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 229940083466 soybean lecithin Drugs 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000000194 supercritical-fluid extraction Methods 0.000 description 1
- 230000008685 targeting Effects 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
- C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
- C07F9/02—Phosphorus compounds
- C07F9/06—Phosphorus compounds without P—C bonds
- C07F9/08—Esters of oxyacids of phosphorus
- C07F9/09—Esters of phosphoric acids
- C07F9/10—Phosphatides, e.g. lecithin
- C07F9/103—Extraction or purification by physical or chemical treatment of natural phosphatides; Preparation of compositions containing phosphatides of unknown structure
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biochemistry (AREA)
- General Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
Abstract
The invention discloses a kind of methods that aqueous two-phase system purifies egg yolk lecithin, it is characterised in that：Aqueous two-phase system is constituted by inorganic salt solution and fatty alcohol solution, yolk powder or yolk raw phospholipid are added as raw material in the system, stratification, ether or methyl tertiary butyl ether(MTBE) are added into lower layer's opacifying layer, secondary clearing again is concentrated to dryness, that is, obtains purifying egg yolk lecithin.For the present invention using the method mild condition of aqueous two-phase system purification egg yolk lecithin, product purity is high, and organic solvent usage amount and energy consumption etc. greatly reduce, to it is more environment-friendly, caused by pollute smaller, meet green circulation economy requirement.
Description
One, technical field
The present invention relates to a kind of aqueous two-phase systems to detach grease type impurity and phosphatide cpd in yolk powder, and further pure
Change the method for obtaining high-purity egg yolk lecithin.
Two, background technology
Egg yolk lecithin is a kind of important natural active product, prevents hepatitis, reduces cholesterol, prevention of cardiovascular disease
The functions such as disease and anticancer, suffer from a very wide range of application in numerous areas such as medicine, food, are that dosage is maximum single in the world
Food additives and health products.More importantly with Nano-technology Development, targeting, the development of sustained-release administration technology are led in pharmaceutical preparation
Domain is most important research and application direction by the sustained release targeted drug novel formulation of base material of phosphatide using more and more extensive, it is contemplated that
Future can be higher and higher to lecithin quality requirement, and demand can be increasing.
The method of purification lecithin is concentrated mainly on following aspects at present：
(1) solvent extraction
Solvent extraction be according to each component in mixed phosphatide in certain solvents different solubility, by lecithin and other
Component is detached, such as phosphatidyl choline (PC) dissolves in ether, chloroform, n-hexane low polar solvent and lower alcohol, micro-
It is dissolved in benzene, is practically insoluble in acetone, ethyl acetate.Solvent extraction mainly utilizes lower alcohol (C1 ~C4) detached, it commonly uses
Ethyl alcohol.Since phosphatidyl choline (PC) solubility in lower alcohol is big, and phosphatidyl-ethanolamine (PE) and phosphatidylinositols (PI)
It is small in lower alcohol solubility, therefore the difference of solubility can be utilized to obtain the purpose of separating-purifying.In addition, phosphatide is in acetone
It is insoluble, and other lipoid substances are all dissolved in acetone, accordingly, can dissolve other lipids in phosphatide with acetone and remove.
When being extracted, it is necessary to control the conditions such as temperature, solvent dosage, solvent strength, pH value, extraction times and factor.Solvent extracts
Following the example of has the characteristics that simple for process, of low cost, yield is high, with short production cycle, easy to automate.Guan Runling etc. is used should
Method has studied acetone deoiling temperature and extraction time, ethyl alcohol Extracting temperature and extraction time, different decolorising agent obtain lecithin
82% lecithin can be obtained in the influence of rate under best process conditions.
Although solvent extraction has above-mentioned many advantages, solvent extraction organic with that may be remained in final finished
Solvent easily causes organic solvent pollution, and solvent extraction only plays the purpose of enrichment PC, can not obtain higher purity, work
Industry is of limited application.
(2) supercritical CO2Extraction
Supercritical fluid has special dissolution to aliphatic acid, vegetable soda, ethers, ketone, glyceride etc., therefore can
Extraction and separation for this substance.With supercritical CO2For extractant, there is certain dissolubility to the grease in raw phospholipid,
And to phosphatide almost without dissolution, when using ethyl alcohol as entrainer, since ethyl alcohol is to the dissolving energy of each component in phosphatide
Power is different, maximum to the dissolubility of lecithin, therefore can achieve the purpose that separating-purifying, obtains the lecithin of high-purity.
Zhang Dequan etc. utilizes supercritical CO2Abstraction technique has studied extracting pressure, temperature, time, ethyl alcohol additive amount to lecithin extraction
The influence of rate can make the extraction yield of lecithin up to 93%, and purity is up to 78%.
But supercritical extraction method equipment investment is big, production capacity is small in unit volume process units, currently without work
Industry production application.
(3) column chromatography
Chromatography is current high-purity-lecithin separating-purifying common method.Column, which fills out adsorbent, at present silica gel, aluminium oxide, silicon
Puddle etc., common eluent select chloroform, low-carbon alcohols etc..In order to reach optimal separation effect, it is necessary to such as to column condition：Column
Geometry, fill method, filler particle size, temperature, amount of samples, flow velocity, eluent the factors such as composition selected
It selects and controls.Shao Youyuan etc. has studied the process conditions of alumina column chromatography method purifying, and result of study shows that spill elution is compared
It is good.B.De Meulenaer etc. use column chromatography and are purified to lecithin, are fixed phase with the silica gel of irregular shape,
Mobile phase is done with mixed solvent (hexane, isopropyl alcohol and water), the egg yolk lecithin that purity reaches 93% or more can be obtained.Yuanfa
Liu et al. uses ion exchange resin isolating and purifying for lecithin.D113-III resins are found by 10 kinds of resin Experimentals
The purifying for being used for lecithin can be obtained PC contents and reach 94% product, and a D113-III resin can at least be reused
Six times.Cao Dong etc. uses alundum (Al2O3) for stationary phase, has studied the ethanol solution of different volumes score to column chromatography for separation phosphorus
The influence of phosphatidylcholine, obtains product PC contents and yield is all higher than 90%, and eluent has no toxic side effect.
But column chromatography produces high-purity-lecithin, product batches are small, difficulty in mass production, and having as eluant, eluent
Solvent consumption is big, causes production cost high.
(4) compound sink of inorganic salts determines technology
Inorganic salts it is compound it is heavy determine technology be the property for utilizing lecithin that can generate precipitation in certain inorganic salts, lecithin
It is extracted from phosphatide, to achieve the purpose that detach with other phosphatide, remove protein and fat, greatly improves lecithin
Purity.Li Wei etc. proposes that applied metal salt precipitating reagent removes the new process of cephalin, and lecithin content in product is made to reach
85% or more.Wherein Zn2+And Fe3+To cephalin heavy, to determine effect preferable.
This method is although easy to operate, but larger for the control difficulty of deposition condition, it is difficult to stably obtain high-purity
Lecithin product.And easily remain inorganic metal ion in product, more difficulty is removed, unfavorable shadow is caused to the quality of product
It rings.
(5) other methods
Due to the great market demand and economic value of lecithin, both at home and abroad lecithin separating-purifying largely grind
Study carefully, also other a variety of process for separation and purification of developmental research.Such as membrane separation process, ethanol fractionation method, enzymatic method for refining and liquid phase color
Spectrum etc..Fangbo liu etc. carry out the de-oiling of lecithin using inorganic ceramic membrane ultrafiltration, have selected a hole size for 5nm's
Inorganic ceramic membrane improves the efficiency of lecithin de-oiling；UF uses continuous filter pattern in the case where transmembrane pressure is 0.25MPa；Finally
The yield that de-oiled lecithin obtains is about 84%.Membrane separation process is with low energy consumption, device is simple, operation is easy, it is new not generate
Pollution the advantages that, separation process generally carries out at normal temperatures, is particularly suitable for separating natural substance.But seperation film is not easy to regenerate,
Poor repeatability, expensive, industry is difficult to apply.The extraction fractional distillation such as Vilas V.Patil finds lecithin and solvent
The ratio of (ethyl alcohol) is 1:When 7, the PC products of high-purity can be obtained.Kelh etc. improves lecithin using enzymatic method for refining
The content of middle phosphatidyl choline, used enzyme are the phosphatidase in cabbage, and result of study is can will to contain phosphatide
Lecithin that phatidylcholine is 80% and containing phosphatidyl choline be 75% lecithin phosphatidylcholine content be respectively increased for
95% and 100%.
In conclusion existing phosphatide extraction purification technology all having some limitations property, it is difficult to extensive, low cost, ring
The production of the friendly progress high-purity phospholipid product in border.
Aqueous two phase extraction technique is the new separation technology to grow up the end of last century.Aqueous two-phase isolation technics and tradition
Organic-aqueous extraction principle it is similar, according to substance two it is alternate selectivity distribution.But the extraction property of double-aqueous phase system has
Institute is different, after substance to be separated enters double-aqueous phase system, due to making at the surface nature between phase substance and object, charge
With with various power (such as hydrophobic key, oxygen key and ionic bond) presence and environment influence so that object in upper and lower phase point
With concentration difference.To Mr. Yu's class or certain substance, select suitable double-aqueous phase system and rational separation condition, can obtain compared with
Good separating effect isolates and purifies to realize.
Mass transfer and equilibrium process speed between aqueous two-phase system are fast, organic efficiency is high, energy consumption is smaller, separating rate is fast,
It is easy to carry out continuous operation, equipment is simple, and can directly be connected with subsequent purification process, without carrying out specially treated；It is double
The alternate tension of aqueous phase system is significantly less than the alternate tension between organic solvent and water phase, and phase separation is mild, thus meeting
Keep the activity of most biomolecule.The factor for influencing double-aqueous phase system is more complicated, in a sense, can adopt
Multiple means are taken to improve selectivity or improve yield；The separation method is easy to amplify, and various separation parameters can be put in proportion
It is big and product yield does not reduce.Aqueous two phase extraction technique have been used to effective component of chinese medicine, natural products, enzyme, protein and
Other biological activity substance detaches.
Three, invention content
The present invention is to provide a kind of aqueous two-phase system purification yolk to avoid the deficiency of existing egg yolk lecithin purification technique
The method of lecithin, problem to be solved are：Aqueous two-phase system is constituted by inorganic salt solution and fatty alcohol aqueous solution, with this
System extraction and separation yolk powder or grease, free fatty and miscellaneous phosphatide in yolk raw phospholipid obtain purity and are more than 90%
High-purity egg yolk lecithin.
The present invention solves technical problem, adopts the following technical scheme that：
The method of aqueous two-phase system purification egg yolk lecithin of the present invention, feature are to include the following steps：
(1) it is added to the water by the inorganic salts for being dissolved in water and forms water phase one, the fatty alcohol by being dissolved in water, which is added to the water, forms water
Water phase one and water phase two are mixed and constitute immiscible aqueous two-phase system by phase two；
(2) yolk powder or yolk raw phospholipid are added as raw material in aqueous two-phase system, are stirred evenly, stratification, point
From lower layer's opacifying layer；
(3) ether or methyl tertiary butyl ether(MTBE) are added into opacifying layer, stirs evenly, stratification, detaches two-phase；By gained
Ether or methyl tert-butyl ether layers are concentrated in vacuo to do purifies egg yolk lecithin to get to target product.
The method of aqueous two-phase system purification egg yolk lecithin of the present invention, feature are lain also in：The inorganic salts for being dissolved in water
For at least one of potassium dihydrogen phosphate, ammonium sulfate, sodium chloride, zinc chloride, iron chloride, potassium hydrogen phosphate；The fat for being dissolved in water
Fat alcohol is at least one of ethyl alcohol and propyl alcohol.
The mass concentration of inorganic salts is 2%~40% in the water phase one；The concentration of fatty alcohol in the water phase two
It is 20%~80%；The volume ratio of water phase one and water phase two is 1 when constituting aqueous two-phase system:0.1~10；Raw material in step (2)
Mass volume ratio with aqueous two-phase system is 10~200g/L；Opacifying layer and ether or the body of methyl tertiary butyl ether(MTBE) in step (3)
Product is than being 1:3~3:1.
Whipping temp is 0~40 DEG C in step (2), and the whipping temp in step (3) is room temperature.
The condition of vacuum concentration is in step (3)：Vacuum degree≤- 0.06MPa, temperature≤45 DEG C.
The present invention purify egg yolk lecithin principle be：Utilize different component in yolk raw phospholipid such as grease, free-fat
Acid, phosphatidyl choline, phosphatidyl-ethanolamine, phosphatidylinositols are led because of self-molecules present polarity difference and complexing of metal ion difference
What is caused distributes the difference of concentration (CK) in the two-phase of aqueous two-phase system, detaches all kinds of impurity, under mild conditions, realizes mesh
Mark the purification of phospholipids phatidylcholine.
Compared with the prior art, beneficial effects of the present invention are embodied in：
1, the present invention is using the method mild condition of aqueous two-phase system purification egg yolk lecithin, and product purity is high, You Jirong
Agent usage amount and energy consumption etc. greatly reduce, to it is more environment-friendly, caused by pollute smaller, meet green circulation economy requirement.
2, method of the invention organic solvent usage amount compared with traditional solvent extraction substantially reduces and product purity
Higher, operation is greatly easy compared with column chromatography, and avoids the chromatographies such as silica gel, aluminium oxide and discard produce with solid dielectric
It is raw.
3, method of the invention can use more rudimentary lecithin materials such as yolk powder as the starting material of purification, warp
Cross simple extracting operation, you can obtain the higher egg yolk lecithin product of purity；With existing egg yolk lecithin purification technique
It compares, there is great cost advantage.
4, method of the invention has a relatively broad application, including soybean lecithin, synthetic phospholipid isolate and purify
It is carried out using this method.
Four, specific implementation mode
Embodiment 1
The present embodiment purifies egg yolk lecithin as follows：
(1) weigh 400g ammonium sulfate, at room temperature stirring be added 700g water, continue stirring until ammonium sulfate be completely dissolved, to
It is 1L to be mended in solution and add water to volume, obtains water phase one；
600g ethyl alcohol is weighed, 250g water is added in stirring at room temperature, continues to stir and evenly mix, and is mended into solution and adds water to volume and be
1L obtains water phase two；
Water phase one and water phase two are mixed and constitute immiscible aqueous two-phase system；
(2) it under stirring, is added 300g yolk powders as raw material in aqueous two-phase system, continues stirring 1 hour at room temperature, it is quiet
Set layering, separation lower layer's opacifying layer (ammonium sulfate solution layer)；
(3) ether of 1L is added into opacifying layer, is stirred at room temperature 1 hour, stratification, upper layer is that the ether of lecithin is molten
Liquid；Ether layer is detached, is concentrated to dryness at vacuum degree -0.08Pa, 40 DEG C of temperature, is obtained purifying products egg yolk lecithin 28g, carry
Take rate 93.3%.
Egg yolk lecithin is detected through HPLC obtained by the present embodiment, and phosphatidyl choline (PC) content is 81.2%.
Other indexs of egg yolk lecithin obtained by the present embodiment are：Acid value 0.75, iodine number 95, lysophosphatidyl choline content
It is 2.1%, peroxide value 1.1, moisture 1.2%.
Embodiment 2
The present embodiment purifies egg yolk lecithin as follows：
(1) weigh 300g sodium chloride, at room temperature stirring be added 700g water, continue stirring until sodium chloride be completely dissolved, to
It is 1L to be mended in solution and add water to volume, obtains water phase one；
600g ethyl alcohol is weighed, 250g water is added in stirring at room temperature, continues to stir and evenly mix, and is mended into solution and adds water to volume and be
1L obtains water phase two；
Water phase one and water phase two are mixed and constitute immiscible aqueous two-phase system；
(2) it under stirring, is added 300g yolk powders as raw material in aqueous two-phase system, continues stirring 1 hour at room temperature, it is quiet
Set layering, separation lower layer's opacifying layer (aqueous sodium chloride liquid layer)；
(3) ether of 1L is added into opacifying layer, is stirred at room temperature 1 hour, stratification, upper layer is that the ether of lecithin is molten
Liquid；Ether layer is detached, is concentrated to dryness at vacuum degree -0.08Pa, 40 DEG C of temperature, is obtained purifying products egg yolk lecithin 28g, carry
Take rate 93.3%.
Egg yolk lecithin is detected through HPLC obtained by the present embodiment, and phosphatidyl choline (PC) content is 80.5%.
Other indexs of egg yolk lecithin obtained by the present embodiment are：Acid value 1.50, iodine number 96, lysophosphatidyl choline content
It is 1.8%, peroxide value 2.0, moisture 0.8%.
Claims (3)
1. a kind of method of aqueous two-phase system purification egg yolk lecithin, it is characterised in that include the following steps：
(1) it is added to the water by the inorganic salts for being dissolved in water and forms water phase one, the fatty alcohol by being dissolved in water, which is added to the water, forms water phase two,
Water phase one and water phase two are mixed and constitute immiscible aqueous two-phase system；
The inorganic salts for being dissolved in water are in potassium dihydrogen phosphate, ammonium sulfate and sodium chloride, zinc chloride, iron chloride, potassium hydrogen phosphate
It is at least one；The fatty alcohol for being dissolved in water is at least one of ethyl alcohol and propyl alcohol；
The mass concentration of inorganic salts is 2%~40% in the water phase one；Fatty alcohol is a concentration of in the water phase two
20%~80%；The volume ratio of water phase one and water phase two is 1 when constituting aqueous two-phase system:0.1~10；
(2) yolk powder or yolk raw phospholipid are added as raw material in aqueous two-phase system, are stirred evenly, stratification, under separation
Layer opacifying layer；The mass volume ratio of raw material and aqueous two-phase system is 10~200g/L；
(3) ether or methyl tertiary butyl ether(MTBE) are added into opacifying layer, stirs evenly, stratification, detaches two-phase；By gained ether
Or methyl tert-butyl ether layers are concentrated in vacuo to do and purify egg yolk lecithin to get to target product；Opacifying layer and ether or methyl
The volume ratio of tertbutyl ether is 1:3~3:1.
2. the method for aqueous two-phase system purification egg yolk lecithin according to claim 1, it is characterised in that：In step (2)
Whipping temp is 0~40 DEG C, and the whipping temp in step (3) is room temperature.
3. the method for aqueous two-phase system purification egg yolk lecithin according to claim 1, it is characterised in that：In step (3)
The condition of vacuum concentration is：Vacuum degree≤- 0.06MPa, temperature≤45 DEG C.
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| CN1234713C (en) * | 2002-12-11 | 2006-01-04 | 深圳清华大学研究院 | Process of extracting phosphatidylcholine from soybean phosphatide |
| CN101538278B (en) * | 2009-05-11 | 2011-09-14 | 江南大学 | High-purity egg yolk lecithin and production method and applications thereof |
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