CN101812087A - Method for extracting high-purity phospholipid from sleeve-fish-processing waste - Google Patents
Method for extracting high-purity phospholipid from sleeve-fish-processing waste Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention, which belongs to the technical field of substance extraction, relates to a method for extracting high-purity phospholipid from sleeve-fish-processing waste. Fresh sleeve-fish-processing waste is first dried until the moisture content is less than or equal to 3 percent, and is ground to 10 to 80 meshes; the preprocessed powdery material is then loaded into an extraction kettle, and after the air is removed, extracting solvent CO2 is injected to set pressure; the supercritical extraction and separation of the extraction system is regulated as three processes, i.e. extraction, primary separation and secondary separation, raffinate is taken out of the extraction kettle after triglycercide and cholesterol are separated and removed, ethanol which is 4 to 10 times the weight of the raffinate is added in the raffinate according to a weight ratio to dissolve the raffinate, clear solution is taken out and concentrated, and is then washed by acetone, the obtained solid substance is dissolved in ethanol and then mixed with water, and precipitate which is obtained by centrifugation is dried, so that sleeve-fish phospholipid is obtained. The method has the advantages of less organic solvent dosage, little environment pollution, simple processing equipment, easy operation, automatic control, stable product quality, low production cost, good quality and high purity.
Description
Technical field:
The invention belongs to the material composition and extract preparing technical field, relate to a kind of method of from sleeve-fish-processing waste, extracting high-purity phospholipid, adopt supercritical CO
2Abstraction technique and equipment come out the effective constituent separation and Extraction in the natural product and carry out processing and preparing.
Background technology:
Phosphatide is a kind of lipid material of phosphorous acid group, is histiocytic ultimate constituent, has important biological function.The highly unsaturated fatty acids that contains in the phosphatide is the important source of human body polyenoic acid; Phosphatide has the cholesterol content of triglyceride that reduces in the blood, improves lipid metabolism and arteriosclerotic function; Phospholipid molecule is the soluble molecule of typically holding concurrently, has emulsification function preferably, it is the ultimate constituent of liposome, it is again the important component of total intravenous nutrition emulsion, has higher medical value, brain tonic, beauty treatment, anti-ageing, reducing blood-fat are arranged, protect the liver effect such as enrich blood, have a wide range of applications in each fields such as chemical industry, light industry, foodstuffs industry.Phosphatide, is mainly derived to extract from natural phant or animal and obtains by the synthetic except that on a small quantity, as the soybean phospholipid that extracts from soybean or extract the egg phospholipids that obtains from yolk.Squid is to have one of marine products kind of potentiality to be exploited most in the present sea going fisheries, and China squid annual production has in recent years reached more than 200,000 tons.In general, squid has head, foot, internal organ and the epidermis the like waste about 30%, and the internal organ that wherein account for squid body weight about 14% are rich in the crude fat of 20-30%, is the good source of extracting phosphatide.At present, the waste of processing squid is except that small part is used as the fodder additives utilization, and major part goes out of use and emergency burial, has both caused the huge waste of fishing resources, exists the hidden danger of environmental pollution again.Therefore, be raw material with the sleeve-fish-processing waste, therefrom extract the phosphatide of purifying high added value, have remarkable economical and be worth and social effect, it extracts and technological method for processing is just becoming the technology contents of probing in the industry.
At present, the method for extraction phosphatide mainly contains solvent-extraction process and supercritical extraction method from natural animal-plant.The extraction solvent of traditional solvent has alkanes, acetone, dme, C
1-C
3There are shortcomings such as the organic solvent consumption is big, extraction process time length, dissolvent residual height in the binary system of Fatty Alcohol(C12-C14 and C12-C18) or Fatty Alcohol(C12-C14 and C12-C18) and alkane, this method.The supercritical extraction method has simple, the easy handling of technology, and product purity and rate of recovery advantages of higher can overcome most of shortcoming that traditional solvent exists.At present, the supercritical extraction method has obtained good application in the extraction preparation of terrestrial organism phosphatide such as soybean phospholipid and egg phospholipids, but, do not see to be used for that particularly squid and processing waste thereof extract the open report of preparation phosphatide from marine animal.
Summary of the invention:
The objective of the invention is to overcome the shortcoming that prior art exists, seek to provide a kind of method for preparing high-purity phospholipid of from sleeve-fish-processing waste, extracting, this method adopts supercritical liquid extraction technique and equipment, extracts the effect of squid phosphatide by regulating parameters realizations such as solvent flux, extraction temperature, extracting pressure.
To achieve these goals, technical scheme of the present invention is carried out in normally used overcritical apparatus system, comprise that mainly raw materials pretreatment, charging, supercritical extraction remove triglyceride level and processes such as cholesterol, phosphatide separation and Extraction, specifically operate as follows:
(1) raw materials pretreatment: spray-dried or lyophilize was pulverized the 10-80 mesh sieve and was got powder raw material to moisture content≤3% with fresh sleeve-fish-processing waste;
(2) charging: pretreated sleeve-fish-processing waste powder raw material is packed in the extraction kettle of supercritical extraction unit system, behind the air in the remover system, in airtight extraction kettle, inject extraction solvent CO
2To setting pressure;
(3) supercritical extraction removes triglyceride level and cholesterol: the supercritical extraction process is divided into extraction, flash trapping stage and secondary and separates three parts, wherein, extracting pressure is 12-30MPa, extraction temperature is 35-60 ℃, and flash trapping stage pressure is 6-8MPa, and the flash trapping stage temperature is 30-60 ℃, the secondary separating pressure is 4-6MPa, the secondary separation temperature is 30-60 ℃, and the extraction time is 1.5-5h, CO
2Flow is 20-40Kg/Kg, with triglyceride level and cholesterol separation removal;
(4) phosphatide separation and Extraction: after extraction finishes, from extraction kettle, take out and slough the extract remainder of triglyceride level and cholesterol, weight ratio by extract remainder adds the dissolve with ethanol that 4-10 doubly measures, get and use washing with acetone when settled solution is concentrated into the 20%-40% of the weight that feeds intake, the solids of gained stirs with adding water behind the dissolve with ethanol again, again-45 ℃, the 20Pa condition is carried out lyophilize after centrifugal the throw out-20 ℃ precooling, and the gained dry product is a squid phosphatide.
Fresh sleeve-fish-processing waste raw material of the present invention is a particularly squid ovum of squid viscera, and squid comprises the animal of sea mollusk door Cephalopoda Decapoda Calamary sections such as squid, squid, Calamary, cuttlefish, Symeplectoteuthis oualaniensis, cuttle fish and inkfish and Sepiidae; Described drying means preferably freeze drying method; The extraction solvent CO that in extraction kettle, injects
2Through preheating, the extraction temperature of setting in its preheating temperature and the extraction kettle is all 35-60 ℃.
Supercritical extraction process of the present invention comprises simple dynamic extraction and static and dynamic in conjunction with two kinds of patterns of extraction, when adopting static state and dynamic combination extraction pattern, at first carry out static extracting, the time is 1-3.5h, carries out the dynamic extraction of 0.5-1.5h after static extracting finishes again.
The extract remainder slough fat and cholesterol that from extraction kettle, takes out of the present invention, when adding the dissolve with ethanol that 4-10 doubly measures by its weight ratio, used alcoholic acid weight percent concentration is 75-99.5%, preferred concentration is 90-95%.
The present invention makes product and comprises triglyceride level and cholesterol, squid phosphatide, squid protein powder.
The present invention compares with existing extraction phosphatide technology from sleeve-fish-processing waste and has the following advantages: the one, adopt supercritical CO
2Abstraction technique has realized that at first the high-level efficiency of triglyceride level and cholesterol removes in the sleeve-fish-processing waste, has significantly reduced the consumption of organic solvent, has reduced environmental pollution; The 2nd, remove the extract remainder after triglyceride level and the cholesterol, can obtain highly purified squid phosphatide through simple refinement treatment, its processing unit is simple, easy handling and control automatically, constant product quality, production cost is low; The 3rd, the squid phosphatide dissolvent residual that obtains is low, quality better, purity height.
Embodiment:
Below the present invention will be further described by specific embodiment.
Following examples are all carried out in common supercritical extraction unit system, and related equipment unit title is in the apparatus system should parts.
Embodiment 1:
Get squid viscera powder 1Kg and place supercritical CO
2In the extraction kettle, be preheated to design temperature after, CO
2Open to 20MPa through high-pressure pump, the beginning cycling extraction, the pressure of extraction kettle is 20MPa, 40 ℃ of temperature, flash trapping stage still pressure is 6MPa, 40 ℃ of the temperature of flash trapping stage still, secondary separating still pressure is 4MPa, 40 ℃ of the temperature of secondary separating still, CO
2Flow be 20Kg/Kg raw material .h, behind the cycling extraction 3h, in separator, collect glycerine three intoxicated and cholesterol, extract remainder is stayed in the extraction kettle, treat extraction finish, after system's step-down, extract remainder is taken out from extraction kettle, and with 95% ethanol 5L stirring and dissolving, the clear liquor vacuum and low temperature is concentrated into 1L, after the small amount of acetone washing, add 6L water again after adding 95% ethanol 8L dissolving, stir centrifugal, after precipitate is put-20 ℃ of pre-freezes, in-45 ℃, 20Pa carries out lyophilize, gets squid phospholipid prod 102g, and yield is 10.2% (to the squid viscera powder meter that feeds intake).
Embodiment 2:
Get squid ovum powder 2Kg and place supercritical CO
2In the extraction kettle, be preheated to design temperature after, CO
2Open to 25MPa through high-pressure pump, the beginning cycling extraction, the pressure of extraction kettle is 25MPa, 40 ℃ of temperature, flash trapping stage still pressure is 7MPa, 45 ℃ of the temperature of flash trapping stage still, secondary separating still pressure is 4MPa, 40 ℃ of the temperature of secondary separating still, CO
2Flow be 25Kg/Kg raw material .h, behind the cycling extraction 2h, in separator, collect glycerine three intoxicated and cholesterol, extract remainder is stayed in the extraction kettle, treat extraction finish, after system's step-down, extract remainder is taken out from extraction kettle, and with 95% ethanol 15L stirring and dissolving, the clear liquor vacuum and low temperature is concentrated into 4L, after the small amount of acetone washing, add 8L water again after adding 85% ethanol 12L dissolving, stir centrifugal, after precipitate is put-20 ℃ of pre-freezes, in-45 ℃, 20Pa carries out lyophilize, gets squid phospholipid prod 465g, and yield is 23.25% (to the squid ovum powder meter that feeds intake).
Embodiment 3:
Get Symeplectoteuthis oualaniensis ovum powder 5Kg and place supercritical CO
2In the extraction kettle, be preheated to design temperature after, CO
2Open to 30MPa through high-pressure pump, behind the employing static extracting 1h, the beginning cycling extraction, the pressure of extraction kettle is 30MPa, 40 ℃ of temperature, flash trapping stage still pressure is 8MPa, 40 ℃ of the temperature of flash trapping stage still, secondary separating still pressure is 6MPa, 35 ℃ of the temperature of secondary separating still, CO
2Flow be 30Kg/Kg raw material .h, behind the cycling extraction 1h, in separator, collect glycerine three intoxicated and cholesterol, extract remainder is stayed in the extraction kettle, treat extraction finish, after system's step-down, extract remainder is taken out from extraction kettle, and with 90% ethanol 40L stirring and dissolving, the clear liquor vacuum and low temperature is concentrated into 10L, after the small amount of acetone washing, add 20L water again after adding 95% ethanol 25L dissolving, stir centrifugal, after precipitate is put-20 ℃ of pre-freezes, in-45 ℃, 20Pa carries out lyophilize, gets squid phospholipid prod 1.265Kg, and yield is 25.3% (to the Symeplectoteuthis oualaniensis ovum powder meter that feeds intake).
Embodiment 4:
Get sea grape powder 3Kg and place supercritical CO
2In the extraction kettle, be preheated to design temperature after, CO
2Open to 15MPa through high-pressure pump, the beginning cycling extraction, the pressure of extraction kettle is 15MPa, 60 ℃ of temperature, flash trapping stage still pressure is 6MPa, 50 ℃ of the temperature of flash trapping stage still, secondary separating still pressure is 4MPa, 40 ℃ of the temperature of secondary separating still, CO
2Flow be 40Kg/Kg raw material .h, behind the cycling extraction 5h, in separator, collect glycerine three intoxicated and cholesterol, extract remainder is stayed in the extraction kettle, treat extraction finish, after system's step-down, extract remainder is taken out from extraction kettle, and with 75% ethanol 10L stirring and dissolving, the clear liquor vacuum and low temperature is concentrated into 3L, after the small amount of acetone washing, add 10L water again after adding 90% ethanol 15L dissolving, stir centrifugal, after precipitate is put-20 ℃ of pre-freezes, in-45 ℃, 20Pa carries out lyophilize, gets squid phospholipid prod 654g, and yield is 21.8% (to the sea grape powder meter that feeds intake).
The squid phosphatide that table 1 obtains for the technology of the present invention and the ratio of components of soybean phospholipid and egg phospholipids are, as can be seen from the table: the content of PC was up to 67.3% during squid phosphatide was formed, content than soybean phospholipid PC exceeds more than 4 times, basic content near PC in the egg phospholipids, belong to high-quality phospholipid prod, fully can the high egg phospholipids of alternative cost, be widely used in fields such as food, medicine, chemical industry, light industry.
The ratio of components of table 1 squid phosphatide, soybean phospholipid and egg phospholipids
*: Val (CL), phosphatidylethanolamine (PE), phosphatidylcholine (PC), (PI), phosphatidylserine (PS), sphingphospholipid (SM), lyso-phosphatidylcholine (LPC)
* :-do not detect.
Claims (4)
1. method of from sleeve-fish-processing waste, extracting high-purity phospholipid, in normally used overcritical apparatus system, carry out, comprise that mainly raw materials pretreatment, charging, supercritical extraction remove triglyceride level and processes such as cholesterol, phosphatide separation and Extraction, is characterized in that:
(1) raw materials pretreatment: spray-dried or lyophilize was pulverized the 10-80 mesh sieve and was got powder raw material to moisture content≤3% with fresh sleeve-fish-processing waste;
(2) charging: pretreated sleeve-fish-processing waste powder raw material is packed in the extraction kettle of supercritical extraction unit system, behind the air in the remover system, in airtight extraction kettle, inject extraction solvent CO
2To setting pressure;
(3) supercritical extraction removes triglyceride level and cholesterol: the supercritical extraction sepn process is divided into extraction, flash trapping stage and secondary and separates three parts, wherein, extracting pressure is 12-30MPa, extraction temperature is 35-60 ℃, and flash trapping stage pressure is 6-8MPa, and the flash trapping stage temperature is 30-60 ℃, the secondary separating pressure is 4-6MPa, the secondary separation temperature is 30-60 ℃, and the extraction time is 1.5-5h, CO
2Flow is 20-40Kg/Kg, with triglyceride level and cholesterol separation removal;
(4) phosphatide separation and Extraction: after extraction finishes, from extraction kettle, take out and slough the extract remainder of triglyceride level and cholesterol, weight ratio by extract remainder adds the dissolve with ethanol that 4-10 doubly measures, get and use washing with acetone when settled solution is concentrated into the 20%-40% of the weight that feeds intake, the solids of gained stirs with adding water behind the dissolve with ethanol again, again-45 ℃, the 20Pa condition is carried out lyophilize after centrifugal the throw out-20 ℃ precooling, and the gained dry product is a squid phosphatide.
2. the method for from sleeve-fish-processing waste, extracting high-purity phospholipid according to claim 1, it is characterized in that described fresh sleeve-fish-processing waste raw material is a particularly squid ovum of squid viscera, squid comprises squid, squid, Calamary, cuttlefish, Symeplectoteuthis oualaniensis, cuttle fish and inkfish; The extraction solvent CO that in extraction kettle, injects
2Through preheating, the extraction temperature of setting in its preheating temperature and the extraction kettle is all 35-60 ℃.
3. the method for from sleeve-fish-processing waste, extracting high-purity phospholipid according to claim 1, it is characterized in that described supercritical extraction process comprises simple dynamic extraction and static and dynamic in conjunction with two kinds of patterns of extraction, when adopting static state and dynamic combination extraction pattern, at first carry out static extracting, time is 1-3.5h, carries out the dynamic extraction of 0.5-1.5h after static extracting finishes again.
4. the method for from sleeve-fish-processing waste, extracting high-purity phospholipid according to claim 1, it is characterized in that the described extract remainder of sloughing fat and cholesterol that from extraction kettle, takes out, when adding the dissolve with ethanol that 4-10 doubly measures by its weight ratio, used alcoholic acid weight percent concentration is 75-99.5%.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103749940A (en) * | 2014-01-10 | 2014-04-30 | 上海海洋大学 | Comprehensive utilization method of saury internal organs |
| CN103864841A (en) * | 2014-03-12 | 2014-06-18 | 威海博宇食品有限公司 | Method for extracting and refining phospholipid from egg of aquatic animal |
| CN104961764A (en) * | 2015-06-02 | 2015-10-07 | 燕京理工学院 | Technology for extraction of phosphatidylcholine from clarias gariepinus leftover |
| CN105265743A (en) * | 2014-07-02 | 2016-01-27 | 九三粮油工业集团有限公司 | Blend phospholipids composition |
| CN106977541A (en) * | 2017-05-26 | 2017-07-25 | 贝因美婴童食品股份有限公司 | A kind of method for preparing long-chain polyunsaturated fatty acid phosphatide |
| CN107788428A (en) * | 2016-08-30 | 2018-03-13 | 威海博宇食品有限公司 | A kind of squid ovum food production process rich in DHA phosphatide |
| CN108823319A (en) * | 2018-04-17 | 2018-11-16 | 中国水产科学研究院南海水产研究所 | A method of identifying the medium-sized group of Symeplectoteuthis oualaniensis and miniature group using specific amplimer group |
| CN109603195A (en) * | 2018-12-04 | 2019-04-12 | 冠昊生物科技股份有限公司 | A kind of degreasing method of animal tissue and its application |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1483415A (en) * | 2003-07-31 | 2004-03-24 | 黑龙江大通生物技术有限公司 | Process for preparing frog lecithin capsule |
| CN101333229A (en) * | 2008-05-10 | 2008-12-31 | 中国海洋大学 | Process for extracting phospholipid rich-containing eicosapentaenoic acid and docosahexenoic acid |
-
2010
- 2010-05-07 CN CN201010164966A patent/CN101812087A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1483415A (en) * | 2003-07-31 | 2004-03-24 | 黑龙江大通生物技术有限公司 | Process for preparing frog lecithin capsule |
| CN101333229A (en) * | 2008-05-10 | 2008-12-31 | 中国海洋大学 | Process for extracting phospholipid rich-containing eicosapentaenoic acid and docosahexenoic acid |
Non-Patent Citations (2)
| Title |
|---|
| 《中国博士学位论文全文数据库工程科技I辑》 20090215 王琦 海产动物来源n-3PUFA磷脂的提取及生物活性研究 正文第39页第14行-第41页第23行，第56页第1行-第79页第21行 1-4 , 第2期 2 * |
| 《中国药理学通报》 20110228 杨玉红等 磷脂型DHA对肿瘤细胞凋亡的影响 第178页第1.4.1节 1-4 第27卷, 第2期 2 * |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103749940A (en) * | 2014-01-10 | 2014-04-30 | 上海海洋大学 | Comprehensive utilization method of saury internal organs |
| CN103749940B (en) * | 2014-01-10 | 2016-08-17 | 上海海洋大学 | A kind of saury internal organs method of comprehensive utilization |
| CN103864841A (en) * | 2014-03-12 | 2014-06-18 | 威海博宇食品有限公司 | Method for extracting and refining phospholipid from egg of aquatic animal |
| CN105265743A (en) * | 2014-07-02 | 2016-01-27 | 九三粮油工业集团有限公司 | Blend phospholipids composition |
| CN104961764A (en) * | 2015-06-02 | 2015-10-07 | 燕京理工学院 | Technology for extraction of phosphatidylcholine from clarias gariepinus leftover |
| CN107788428A (en) * | 2016-08-30 | 2018-03-13 | 威海博宇食品有限公司 | A kind of squid ovum food production process rich in DHA phosphatide |
| CN106977541A (en) * | 2017-05-26 | 2017-07-25 | 贝因美婴童食品股份有限公司 | A kind of method for preparing long-chain polyunsaturated fatty acid phosphatide |
| CN108823319A (en) * | 2018-04-17 | 2018-11-16 | 中国水产科学研究院南海水产研究所 | A method of identifying the medium-sized group of Symeplectoteuthis oualaniensis and miniature group using specific amplimer group |
| CN108823319B (en) * | 2018-04-17 | 2021-09-03 | 中国水产科学研究院南海水产研究所 | Method for identifying squid mesoscale group and squid micromodule group by using specific amplification primer group |
| CN109603195A (en) * | 2018-12-04 | 2019-04-12 | 冠昊生物科技股份有限公司 | A kind of degreasing method of animal tissue and its application |
| CN109603195B (en) * | 2018-12-04 | 2021-06-01 | 冠昊生物科技股份有限公司 | Animal tissue degreasing method and application thereof |
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