CN105542936A - Euphausia superba oil extraction method - Google Patents
Euphausia superba oil extraction method Download PDFInfo
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- CN105542936A CN105542936A CN201510943810.5A CN201510943810A CN105542936A CN 105542936 A CN105542936 A CN 105542936A CN 201510943810 A CN201510943810 A CN 201510943810A CN 105542936 A CN105542936 A CN 105542936A
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- antarctic krill
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- 238000000605 extraction Methods 0.000 title claims abstract description 60
- 241000239370 Euphausia superba Species 0.000 title claims abstract description 17
- 239000006227 byproduct Substances 0.000 claims abstract description 26
- 238000012545 processing Methods 0.000 claims abstract description 24
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 20
- 102000004895 Lipoproteins Human genes 0.000 claims abstract description 19
- 108090001030 Lipoproteins Proteins 0.000 claims abstract description 19
- 239000002904 solvent Substances 0.000 claims abstract description 19
- 238000004108 freeze drying Methods 0.000 claims abstract description 17
- 239000000843 powder Substances 0.000 claims abstract description 11
- 239000002994 raw material Substances 0.000 claims abstract description 11
- JEBFVOLFMLUKLF-IFPLVEIFSA-N Astaxanthin Natural products CC(=C/C=C/C(=C/C=C/C1=C(C)C(=O)C(O)CC1(C)C)/C)C=CC=C(/C)C=CC=C(/C)C=CC2=C(C)C(=O)C(O)CC2(C)C JEBFVOLFMLUKLF-IFPLVEIFSA-N 0.000 claims abstract description 10
- 235000013793 astaxanthin Nutrition 0.000 claims abstract description 10
- MQZIGYBFDRPAKN-ZWAPEEGVSA-N astaxanthin Chemical compound C([C@H](O)C(=O)C=1C)C(C)(C)C=1/C=C/C(/C)=C/C=C/C(/C)=C/C=C/C=C(C)C=CC=C(C)C=CC1=C(C)C(=O)[C@@H](O)CC1(C)C MQZIGYBFDRPAKN-ZWAPEEGVSA-N 0.000 claims abstract description 10
- 229940022405 astaxanthin Drugs 0.000 claims abstract description 10
- 239000001168 astaxanthin Substances 0.000 claims abstract description 10
- 238000001704 evaporation Methods 0.000 claims abstract description 10
- 238000001914 filtration Methods 0.000 claims abstract description 9
- 238000011282 treatment Methods 0.000 claims abstract description 3
- 241000238557 Decapoda Species 0.000 claims description 44
- 235000015067 sauces Nutrition 0.000 claims description 26
- 241000239366 Euphausiacea Species 0.000 claims description 24
- 229940106134 krill oil Drugs 0.000 claims description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- 239000000706 filtrate Substances 0.000 claims description 12
- 102000004169 proteins and genes Human genes 0.000 claims description 12
- 108090000623 proteins and genes Proteins 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 11
- 150000003904 phospholipids Chemical class 0.000 claims description 9
- 239000002244 precipitate Substances 0.000 claims description 9
- 108091005658 Basic proteases Proteins 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 4
- 238000010025 steaming Methods 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 2
- 239000004744 fabric Substances 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 239000006228 supernatant Substances 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 13
- 238000005119 centrifugation Methods 0.000 abstract description 4
- 239000000047 product Substances 0.000 abstract description 2
- 238000003912 environmental pollution Methods 0.000 abstract 1
- 230000007071 enzymatic hydrolysis Effects 0.000 abstract 1
- 238000006047 enzymatic hydrolysis reaction Methods 0.000 abstract 1
- 230000008020 evaporation Effects 0.000 abstract 1
- 235000019198 oils Nutrition 0.000 description 15
- 239000012153 distilled water Substances 0.000 description 6
- 238000011160 research Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 102000004190 Enzymes Human genes 0.000 description 3
- 108090000790 Enzymes Proteins 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000002481 ethanol extraction Methods 0.000 description 3
- 238000002386 leaching Methods 0.000 description 3
- 235000020777 polyunsaturated fatty acids Nutrition 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 108091005804 Peptidases Proteins 0.000 description 2
- 239000004365 Protease Substances 0.000 description 2
- 102100037486 Reverse transcriptase/ribonuclease H Human genes 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000004367 Lipase Substances 0.000 description 1
- 102000004882 Lipase Human genes 0.000 description 1
- 108090001060 Lipase Proteins 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- MBLBDJOUHNCFQT-LXGUWJNJSA-N aldehydo-N-acetyl-D-glucosamine Chemical compound CC(=O)N[C@@H](C=O)[C@@H](O)[C@H](O)[C@H](O)CO MBLBDJOUHNCFQT-LXGUWJNJSA-N 0.000 description 1
- 239000003963 antioxidant agent Substances 0.000 description 1
- 235000006708 antioxidants Nutrition 0.000 description 1
- 235000021466 carotenoid Nutrition 0.000 description 1
- 150000001747 carotenoids Chemical class 0.000 description 1
- 238000010411 cooking Methods 0.000 description 1
- 238000004925 denaturation Methods 0.000 description 1
- 230000036425 denaturation Effects 0.000 description 1
- 230000002255 enzymatic effect Effects 0.000 description 1
- 235000021323 fish oil Nutrition 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000007602 hot air drying Methods 0.000 description 1
- 230000000415 inactivating effect Effects 0.000 description 1
- 235000019421 lipase Nutrition 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 235000013372 meat Nutrition 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
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- 238000006467 substitution reaction Methods 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B1/00—Production of fats or fatty oils from raw materials
- C11B1/02—Pretreatment
- C11B1/025—Pretreatment by enzymes or microorganisms, living or dead
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23D—EDIBLE OILS OR FATS, e.g. MARGARINES, SHORTENINGS, COOKING OILS
- A23D9/00—Other edible oils or fats, e.g. shortenings, cooking oils
- A23D9/02—Other edible oils or fats, e.g. shortenings, cooking oils characterised by the production or working-up
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B1/00—Production of fats or fatty oils from raw materials
- C11B1/02—Pretreatment
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B1/00—Production of fats or fatty oils from raw materials
- C11B1/10—Production of fats or fatty oils from raw materials by extracting
- C11B1/102—Production of fats or fatty oils from raw materials by extracting in counter-current; utilisation of an equipment wherein the material is conveyed by a screw
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B1/00—Production of fats or fatty oils from raw materials
- C11B1/10—Production of fats or fatty oils from raw materials by extracting
- C11B1/108—Production of fats or fatty oils from raw materials by extracting after-treatment, e.g. of miscellae
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- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- Food Science & Technology (AREA)
- Polymers & Plastics (AREA)
- Biochemistry (AREA)
- Microbiology (AREA)
- Meat, Egg Or Seafood Products (AREA)
Abstract
The invention discloses a euphausia superba oil extraction method. The method comprises carrying out enzymatic hydrolysis on euphausia superba processing by-products as raw materials, carrying out filtration, carrying out centrifugation treatment, carrying out freeze drying to obtain lipoprotein powder rich in euphausia superba oil, carrying out three-stage countercurrent extraction on the freeze-dried lipoprotein powder through ethanol as an extraction solvent, removing the filter residues, and carrying out evaporation to remove the solvent so that the crude euphausia superba oil rich in phosphatide and astaxanthin is obtained. The euphausia superba oil extraction method prevents by-product waste-caused environmental pollution, produces a euphausia superba oil product with high added value and improves a return rate of investment of the euphausia superba industry.
Description
Technical Field
The invention belongs to the technical field of food processing, and relates to a method for extracting shrimp sauce from a processing byproduct of antarctic krill.
Background
Antarctic krill (Euphausia superba), also known as krill or Antarctic krill, is one of the largest number of individual biological sources on earth. The biological total amount of the antarctic krill in the antarctic sea is counted to be 4-15.5 hundred million tons. The fishing amount of the euphausia superba in 2010-2011 is only 21 ten thousand tons, which is far lower than the fishing amount (860 ten thousand tons) set by the antarctic marine organism resource protection society and is far lower than 0.1 percent of the total organism amount. In recent years, with the gradual depletion of traditional fishery resources worldwide, the huge antarctic krill resources in antarctic water areas are concerned by some countries with developed ocean fishery, and China also puts the antarctic krill resources into one of the main development varieties for the future development of ocean fishery.
Antarctic krill is nutritious, and it has been reported that the protein content of Antarctic krill is 17.4%, fat is 1.1%, and ash content is about 2.3%. Antarctic krill fat is rich in polyunsaturated fatty acids (PUFA), especially EPA and DHA of the n-3 series. These PUFAs with health functions are often present in phospholipid-bound form and are more easily absorbed and utilized by the human body. Researches find that the bioavailability of the shrimp sauce is superior to that of shrimp meat and fish oil. In addition, the shell of Antarctic krill contains rich Astaxanthin (Astaxanthin), which is a carotenoid, not only has strong oxidation resistance, but also has incomparable safety compared with artificially synthesized antioxidants, and many relevant research reports are reported at home and abroad.
In recent years, research on antarctic krill oil has become a hotspot at home and abroad. In industry, the shrimp sauce is extracted from whole shrimps by using an organic solvent. With the increasing utilization of antarctic krill resources, more and more waste is generated in the processing process, which not only causes adverse effects on the natural environment, but also wastes resources. Research finds that the fat content of the euphausia superba processing by-product is higher than that of the whole shrimp, reaches about 3.3 percent, and contains rich EPA and DHA. At present, whole shrimps are mainly used as raw materials for extracting krill oil at home and abroad, and research on processing byproducts of antarctic krill is relatively few.
Disclosure of Invention
This section is for the purpose of summarizing some aspects of embodiments of the invention and to briefly introduce some preferred embodiments. In this section, as well as in the abstract and the title of the invention of this application, simplifications or omissions may be made to avoid obscuring the purpose of the section, the abstract and the title, and such simplifications or omissions are not intended to limit the scope of the invention.
The present invention has been made in view of the above and/or the problems of the prior art in extracting krill oil from the processing by-products of antarctic krill.
Therefore, the invention aims to provide a method for preparing krill oil rich in phospholipids and astaxanthin by using euphausia superba processing by-products.
In order to solve the technical problems, the invention provides the following technical scheme: an extraction method of antarctic krill oil is characterized in that by-products of antarctic krill processing are used as raw materials, and after enzymolysis, filtration and centrifugation, the raw materials are frozen and dried to obtain lipoprotein powder rich in krill oil; extracting freeze-dried lipoprotein powder by adopting three-stage countercurrent extraction by using ethanol as an extraction solvent, removing filter residues, and evaporating to remove the solvent to obtain crude krill oil rich in phospholipid and astaxanthin; wherein, the enzymolysis: steaming and boiling the processing by-product at 100 ℃ for 5-10 min, then adding water according to the mass ratio of the processing by-product to the water of 1: 4, adjusting the temperature to 30-60 ℃, keeping the temperature for 10min, adjusting the pH to 8.0-8.5, adding 2000-5000U/g protein of alkaline protease, keeping out of the sun, and stirring for reaction for 1.5-3.5 h; and (3) centrifuging: firstly adjusting the pH value to 4.5 of the isoelectric point of shrimp protein, standing for 30min, centrifuging the filtrate for 15min at 3000 r/min-5000 r/min, separating the supernatant from the precipitate, and collecting paste precipitate; the three-stage countercurrent extraction: the extraction temperature is 50 ℃, the mass-volume ratio of the lipoprotein powder to the ethanol is 1: 9, and the single-stage extraction time is 0.5 h.
As a preferable embodiment of the extraction method of antarctic krill oil according to the present invention, wherein: the processing byproducts of the antarctic krill are the byproducts of the shell and the head of the antarctic krill obtained after the antarctic krill is extruded and meat-collected for four times by a meat-collecting machine.
As a preferable embodiment of the extraction method of antarctic krill oil according to the present invention, wherein: and (3) filtering: and separating residues after enzymolysis from the enzymolysis liquid by using 60-80-mesh silk cloth.
As a preferable embodiment of the extraction method of antarctic krill oil according to the present invention, wherein: and (3) freeze drying: freeze drying the centrifugal precipitate to obtain the shrimp oil-rich lipoprotein powder with the fat content of 50-60%.
As a preferable embodiment of the extraction method of antarctic krill oil according to the present invention, wherein: and (3) evaporating: the vacuum degree is more than or equal to 0.1MPa and more than or equal to 0.08MPa, the solvent is evaporated in vacuum at the temperature of 45-50 ℃, and the crude shrimp sauce is obtained.
As a preferable embodiment of the extraction method of antarctic krill oil according to the present invention, wherein: the pH value of the enzymolysis system is adjusted to 8.0-8.5, and KOH solution with the mass percentage of 20-50% is adopted for adjustment.
As a preferable embodiment of the extraction method of antarctic krill oil according to the present invention, wherein: the pH is adjusted to 4.5 of the isoelectric point of shrimp protein, and hydrochloric acid with the mass percentage of 10-50% is adopted for adjustment.
As a preferable embodiment of the extraction method of antarctic krill oil according to the present invention, wherein: the freeze drying is carried out, the freeze drying is carried out at the temperature of minus 10 ℃ to minus 50 ℃ to form a solid state, and then the water in the freeze drying is directly sublimated into a gas state without passing through the liquid state under the vacuum condition of 1.3 Pa to 5 Pa.
According to the invention, by combining enzymolysis and organic extraction methods, shrimp oil in the euphausia superba processing by-product is enriched and extracted, and about 2.5-3 g of lipoprotein can be obtained from 25g of euphausia superba processing by-product through enzymolysis and other treatments, so that the energy consumption required by the subsequent drying of raw materials and the solvent required in the extraction process are reduced. The method avoids the pollution of the waste byproducts to the environment, can produce the shrimp sauce product with high added value, and improves the return on investment of the euphausia superba industry.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the description of the embodiments will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without inventive exercise. Wherein:
FIG. 1 is a schematic diagram of a three-stage countercurrent extraction process of the present invention, wherein A is a schematic diagram of lipoprotein powder; b indicates an ethanol solvent; → schematic material trend;schematically collecting an extracting solution;
FIG. 2 is a block diagram of the process flow of the extraction method of Antarctic krill oil according to an embodiment of the present invention;
FIG. 3 is a schematic diagram showing the influence of the drying method selected by the present invention on the acid value of shrimp sauce.
Detailed Description
In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in detail below.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, but the present invention may be practiced in other ways than those specifically described and will be readily apparent to those of ordinary skill in the art without departing from the spirit of the present invention, and therefore the present invention is not limited to the specific embodiments disclosed below.
Furthermore, reference herein to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one implementation of the invention. The appearances of the phrase "in one embodiment" in various places in the specification are not necessarily all referring to the same embodiment, nor are separate or alternative embodiments mutually exclusive of other embodiments.
Example 1
(1) The Antarctic krill is fleshed for four times, and the obtained processing by-products are used as raw materials.
(2) Decocting raw materials at 100 deg.C for 10min, adding distilled water (mass ratio of 1: 4), adjusting temperature to 50 deg.C, maintaining for 10min, adjusting pH to 8.5, adding alkaline protease 3000U/g protein, performing enzymolysis for 2h, boiling for 10min to inactivate enzyme, cooling, filtering with 80 mesh silk yarn, and collecting filtrate.
(3) Adjusting the pH of the filtrate to 4.5, standing for 30min, centrifuging at 8000r/min to obtain paste precipitate, and freeze drying.
(4) Ethanol is used as an extraction solvent, shrimp sauce in freeze-dried lipoprotein is extracted by adopting a multi-stage countercurrent continuous leaching method, the extraction stages are 3 stages, the material-liquid ratio (w/V) of each stage is 1: 9, the material-liquid ratio (m: V) is 1: 9, and the extraction time is 30 min. And after extraction is finished, centrifuging to remove filter residues, and evaporating the filtrate in vacuum to recover the solvent to obtain crude shrimp oil, wherein the final extraction rate of the oil is about 75%, the phospholipid content in the shrimp oil is 23%, and the astaxanthin content is 1250 mug/g of shrimp oil. The final extraction rate of the oil refers to the percentage of the shrimp sauce obtained by ethanol extraction in the total amount of the shrimp sauce in the processing by-products.
Example 2
(1) The Antarctic krill is fleshed for four times, and the obtained processing by-products are used as raw materials.
(2) Decocting raw materials at 100 deg.C for 10min, adding distilled water (mass ratio of 1: 4), adjusting temperature to 30 deg.C, maintaining for 10min, adjusting pH to 8.5, adding alkaline protease 2000U/g protein, performing enzymolysis for 1h, boiling for 10min to inactivate enzyme, cooling, filtering with 80 mesh silk yarn, and collecting filtrate.
(3) Adjusting the pH of the filtrate to 4.5, standing for 30min, centrifuging at 8000r/min to obtain paste precipitate, and freeze drying.
(4) Ethanol is used as an extraction solvent, shrimp sauce in freeze-dried lipoprotein is extracted by adopting a multi-stage countercurrent continuous leaching method, the extraction stages are 3 stages, the material-liquid ratio (w/V) of each stage is 1: 9, the material-liquid ratio (m: V) is 1: 9, and the extraction time is 30 min. And after extraction is finished, centrifuging to remove filter residues, and evaporating the filtrate in vacuum to recover the solvent to obtain crude shrimp sauce, wherein the final extraction rate of the oil is about 60%, the phospholipid content in the shrimp sauce is 20%, and the astaxanthin content in the shrimp sauce is 1050 mu g/g. The final extraction rate of the oil refers to the percentage of the shrimp sauce obtained by ethanol extraction in the total amount of the shrimp sauce in the processing by-products.
Example 3
(1) The Antarctic krill is fleshed for four times, and the obtained processing by-products are used as raw materials.
(2) Steaming at 100 deg.C for 10min, adding distilled water (mass ratio of 1: 4), adjusting temperature to 60 deg.C, maintaining for 10min, adjusting pH to 8.5, adding alkaline protease 5000U/g protein, performing enzymolysis for 3 hr, boiling for 10min to inactivate enzyme, cooling, filtering with 80 mesh silk yarn, and collecting filtrate.
(3) Adjusting the pH of the filtrate to 4.5, standing for 30min, centrifuging at 8000r/min to obtain paste precipitate, and freeze drying.
(4) Ethanol is used as an extraction solvent, shrimp sauce in freeze-dried lipoprotein is extracted by adopting a multi-stage countercurrent continuous leaching method, the extraction stages are 3 stages, the material-liquid ratio (w/V) of each stage is 1: 9, the material-liquid ratio (m: V) is 1: 9, and the extraction time is 30 min. And after extraction is finished, centrifuging to remove filter residues, and evaporating the filtrate in vacuum to recover the solvent to obtain crude shrimp oil, wherein the final extraction rate of the oil is about 70%, the content of the phospholipid in the shrimp oil is 20%, and the content of the astaxanthin in the shrimp oil is 1020 mug/g. The final extraction rate of the oil refers to the percentage of the shrimp sauce obtained by ethanol extraction in the total amount of the shrimp sauce in the processing by-products.
In the embodiment, a method for cooking at high temperature for 5-10 min is adopted, and the method mainly has two purposes: inactivating lipase to prevent fat hydrolysis in enzymolysis; ② the protein denaturation is beneficial to the hydrolysis by the protease action.
If the volume of the added distilled water is too small, an enzymolysis system is not easy to stir, and the enzymolysis effect of the protease is influenced. If the volume of the added distilled water is more, the workload of operations such as filtration, centrifugation and the like is increased, so that the distilled water with the mass ratio of 1: 4 is selected to be added, and the workload of subsequent operations is reduced on the basis of ensuring the enzymolysis effect. The enzymolysis temperature, the enzymolysis time and the enzyme-substrate ratio are key factors influencing the yield of the lipoprotein and the shrimp sauce. If the enzymolysis is insufficient, the lipoprotein can not be separated from the shrimp shell sufficiently; if the enzymolysis is excessive, partial protein and fat can be separated, and a small amount of fat is miscible with water and is difficult to separate and collect. The most preferred enzymatic conditions are: reacting at 55 ℃ for 2h, wherein the addition amount of the alkaline protease is about 3000U/g protein. At this point the lipoproteins were enriched by approximately 85% of the shrimp sauce in the feed. The subsequent drying energy consumption and the dosage of the solvent can be greatly saved by the enzymolysis enrichment process.
The invention adopts a freeze-drying method, and the content of lipoprotein dry-based fat reaches 50 percent. The freeze drying can obviously reduce the influence of the drying modes such as the conventional hot air drying and the like on the oxidation of the shrimp sauce.
Ethanol is used as an extraction solvent, which is more beneficial to the extraction and enrichment of polar substances, namely phospholipid. The adopted series is three stages, the single-stage extraction condition is that the temperature is 50 ℃, the material-liquid ratio is 1: 9 (m: V), and the extraction time is 30 min. And after removing filter residues by centrifugation, evaporating the filtrate in vacuum at 45-50 ℃ and under the vacuum degree of more than or equal to 0.08MPa, and evaporating the solvent to dryness to obtain the crude shrimp sauce. The final extraction rate of the shrimp sauce can reach 75 percent through multi-stage countercurrent extraction, the phospholipid content in the shrimp sauce is 23 percent, and the astaxanthin content is 1250 mug/g of the shrimp sauce.
It should be noted that the above-mentioned embodiments are only for illustrating the technical solutions of the present invention and not for limiting, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications or equivalent substitutions may be made on the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention, which should be covered by the claims of the present invention.
Claims (8)
1. An extraction method of antarctic krill oil is characterized by comprising the following steps: taking euphausia superba processing by-products as raw materials, carrying out enzymolysis, filtration and centrifugal treatment, and carrying out freeze drying to obtain lipoprotein powder rich in shrimp oil; extracting freeze-dried lipoprotein powder by adopting three-stage countercurrent extraction by using ethanol as an extraction solvent, removing filter residues, and evaporating to remove the solvent to obtain crude krill oil rich in phospholipid and astaxanthin; wherein,
the enzymolysis: steaming and boiling the processing by-product at 100 ℃ for 5-10 min, then adding water according to the mass ratio of the processing by-product to the water of 1: 4, adjusting the temperature to 30-60 ℃, keeping the temperature for 10min, adjusting the pH of an enzymolysis system to 8.0-8.5, adding 2000-5000U/g protein of alkaline protease, keeping out of the sun, and stirring for reaction for 1.5-3.5 h;
and (3) centrifuging: adjusting the pH value to 4.5 of the isoelectric point of shrimp protein, standing for 30min, centrifuging the filtrate for 15min at 3000 r/min-5000 r/min, separating the supernatant from the precipitate, and collecting paste precipitate;
the three-stage countercurrent extraction: the extraction temperature is 50 ℃, the mass-volume ratio of the lipoprotein powder to the ethanol is 1: 9, and the single-stage extraction time is 0.5 h.
2. The extraction method of antarctic krill oil according to claim 1, characterized in that: the processing byproducts of the antarctic krill are the byproducts of the shell and the head of the antarctic krill obtained after the antarctic krill is extruded and meat-collected for four times by a meat-collecting machine.
3. The extraction process of antarctic krill oil according to claim 1 or 2, characterized in that: and (3) filtering: and separating residues after enzymolysis from the enzymolysis liquid by using 60-80-mesh silk cloth.
4. The extraction process of antarctic krill oil according to claim 1 or 2, characterized in that: and (3) freeze drying: freeze drying the centrifugal precipitate to obtain the shrimp oil-rich lipoprotein powder with fat content of 50-60%.
5. The extraction method of antarctic krill oil according to claim 4, characterized in that: and (3) evaporating: the vacuum degree is more than or equal to 0.1MPa and more than or equal to 0.08MPa, the solvent is evaporated in vacuum at the temperature of 45-50 ℃, and the crude shrimp sauce is obtained.
6. The extraction method of antarctic krill oil according to claim 1, characterized in that: the pH value of the enzymolysis system is adjusted to 8.0-8.5, and KOH solution with the mass percentage of 20-50% is adopted for adjustment.
7. The extraction method of antarctic krill oil according to claim 1, characterized in that: the pH is adjusted to 4.5 of the isoelectric point of shrimp protein, and hydrochloric acid with the mass percentage of 10-50% is adopted for adjustment.
8. The extraction method of antarctic krill oil according to claim 4, characterized in that: the freeze drying is carried out, the freeze drying is carried out at the temperature of minus 10 ℃ to minus 50 ℃ to form a solid state, and then the water in the freeze drying is directly sublimated into a gas state without passing through the liquid state under the vacuum condition of 1.3 Pa to 5 Pa.
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