CN115636729A - Method and device for purifying sclareol - Google Patents
Method and device for purifying sclareol Download PDFInfo
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- CN115636729A CN115636729A CN202211342182.1A CN202211342182A CN115636729A CN 115636729 A CN115636729 A CN 115636729A CN 202211342182 A CN202211342182 A CN 202211342182A CN 115636729 A CN115636729 A CN 115636729A
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- tank
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- sclareol
- filter cylinder
- interlayer
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- XVULBTBTFGYVRC-HHUCQEJWSA-N sclareol Chemical compound CC1(C)CCC[C@]2(C)[C@@H](CC[C@](O)(C)C=C)[C@](C)(O)CC[C@H]21 XVULBTBTFGYVRC-HHUCQEJWSA-N 0.000 title claims abstract description 64
- XVULBTBTFGYVRC-UHFFFAOYSA-N Episclareol Natural products CC1(C)CCCC2(C)C(CCC(O)(C)C=C)C(C)(O)CCC21 XVULBTBTFGYVRC-UHFFFAOYSA-N 0.000 title claims abstract description 32
- LAEIZWJAQRGPDA-UHFFFAOYSA-N Manoyloxid Natural products CC1(C)CCCC2(C)C3CC=C(C)OC3(C)CCC21 LAEIZWJAQRGPDA-UHFFFAOYSA-N 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000002904 solvent Substances 0.000 claims abstract description 49
- 238000001704 evaporation Methods 0.000 claims abstract description 36
- 239000007788 liquid Substances 0.000 claims abstract description 21
- 238000000746 purification Methods 0.000 claims abstract description 17
- 238000000855 fermentation Methods 0.000 claims abstract description 11
- 230000004151 fermentation Effects 0.000 claims abstract description 11
- 238000000227 grinding Methods 0.000 claims abstract description 11
- 239000000706 filtrate Substances 0.000 claims abstract description 9
- 239000000203 mixture Substances 0.000 claims abstract description 6
- 238000001914 filtration Methods 0.000 claims abstract description 5
- 238000002156 mixing Methods 0.000 claims abstract description 5
- 238000007598 dipping method Methods 0.000 claims abstract description 4
- 238000000926 separation method Methods 0.000 claims abstract description 4
- 239000007790 solid phase Substances 0.000 claims abstract description 4
- 238000005470 impregnation Methods 0.000 claims description 39
- 230000008020 evaporation Effects 0.000 claims description 24
- 239000011229 interlayer Substances 0.000 claims description 24
- 239000007921 spray Substances 0.000 claims description 20
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical group CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 12
- 238000005086 pumping Methods 0.000 claims description 12
- 239000010410 layer Substances 0.000 claims description 10
- 230000009471 action Effects 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 claims description 7
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 claims description 6
- 230000001580 bacterial effect Effects 0.000 claims description 6
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 6
- 239000011324 bead Substances 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 3
- 238000000605 extraction Methods 0.000 abstract description 7
- 239000000047 product Substances 0.000 abstract description 6
- 239000002994 raw material Substances 0.000 abstract description 3
- 210000004027 cell Anatomy 0.000 description 13
- 210000002421 cell wall Anatomy 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 238000002386 leaching Methods 0.000 description 5
- 238000011978 dissolution method Methods 0.000 description 4
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 3
- 235000014680 Saccharomyces cerevisiae Nutrition 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 108090000790 Enzymes Proteins 0.000 description 2
- 102000004190 Enzymes Human genes 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- 241001391944 Commicarpus scandens Species 0.000 description 1
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 1
- 241000235342 Saccharomycetes Species 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 210000000805 cytoplasm Anatomy 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000010362 genome editing Methods 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000002137 ultrasound extraction Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 210000005253 yeast cell Anatomy 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to a method for purifying sclareol, which comprises the following steps: 1) Carrying out solid-liquid separation on fermentation liquor to obtain a solid-phase strain, pretreating the strain, adding a solvent, grinding and crushing the strain, and filtering to obtain a filtrate; 2) Evaporating and crystallizing the filtrate to obtain sclareol; in the step 1), the pretreatment is to add partial solvent into the strain, perform dipping and mixing under the pressure condition, vacuumize the mixture and evaporate the solvent. The purification scheme of the invention has the advantages of low cost of raw materials and devices, short extraction process period and suitability for industrial purification of biologically fermented sclareol products.
Description
Technical Field
The invention relates to a sclareol purification method and a sclareol purification device, and belongs to the technical field of biosynthesis.
Background
The biological fermentation method is an important way for solving the problem of raw material limitation in the preparation of sclareol, and utilizes gene editing recombinant saccharomyces cerevisiae to ferment and metabolize glucose as a substrate to generate the sclareol. Sclareol is a water-insoluble substance, the product generally exists in the cytoplasm of yeast, and the content of fermentation liquor is very low. In the extraction of the product with a solvent, the yeast strain needs to be broken. In the prior art, methods for breaking the cell wall of the strain comprise a grinding method, an alkali dissolution method, an enzyme dissolution method and an ultrasonic method. The single grinding method has poor wall breaking effect and low yield, the alkali dissolution method can change the product property and affect the product quality, the enzyme dissolution method needs longer time and has good extraction effect by an ultrasonic method, for example, patent CN202210267083.5 discloses a method for extracting and purifying sclareol from sclareol fermentation liquor, namely, a plurality of ultrasonic extractions are adopted, and the yield is high. However, due to the ultrasonic attenuation factor, the effective ultrasonic action area is annular, and if the diameter of the extraction tank is too large, an ultrasonic blank area is formed on the peripheral wall of the tank. Therefore, the existing extraction means for preparing sclareol by a fermentation method are carried out in a laboratory and are not applied industrially.
Disclosure of Invention
In order to solve the problems, the invention firstly provides a sclareol purification method, which comprises the following steps:
1) Carrying out solid-liquid separation on fermentation liquor to obtain a solid-phase strain, pretreating the strain, adding a solvent, grinding and crushing the strain, and filtering to obtain a filtrate;
2) Evaporating and crystallizing the filtrate to obtain sclareol;
in the step 1), the pretreatment is to add partial solvent into the strain, perform dipping and mixing under the pressure condition, vacuumize the mixture and evaporate the solvent.
Furthermore, during pretreatment, the pressure is not lower than 0.5MPa when pressurizing, and the vacuum degree is not lower than-0.07 MPa when vacuumizing.
Further, in the step 1), the solvent is ethanol, acetone or n-hexane.
In order to realize the method, the invention discloses a purification device for producing sclareol, which comprises the following steps: comprises a centrifugal separator, a primary impregnation tank, an evaporation tank, a secondary impregnation tank, a bead mill, a filter and a crystallizer which are connected in sequence; the primary impregnation tank is provided with a compressed air interface; the evaporation tank is provided with a vacuumizing interface; the first-stage impregnation tank and the second-stage impregnation tank are provided with liquid inlet pipes which are connected to the solvent tank; the bottom of the first-stage impregnation tank is connected to the top of the evaporation tank through a connecting pipe, and the connecting pipe is provided with a feed valve.
Furthermore, a filter cylinder is arranged in the tank body of the primary impregnation tank, the upper end of the filter cylinder is closed, the lower end of the filter cylinder is opened, and the lower end of the filter cylinder is connected with the tank wall in a closed manner; a feed pipe is arranged in the middle of the tank body and is used for being connected with the centrifugal separator, and the feed pipe penetrates into the filter cylinder; the compressed air interface is arranged at the top of the tank body; the middle part of the tank body is provided with a liquid pumping pipe which is positioned above the joint of the filter cylinder and the tank wall and is connected to the secondary dipping tank.
Furthermore, an interlayer is arranged in the tank body of the evaporating tank, the interlayer comprises a conical cylinder, the bottom of the conical cylinder is provided with an atomizing spray head, a filter cylinder is arranged along the lower part of the interlayer in the tank body, and a vacuumizing interface is arranged on the tank wall below the interlayer; the inner wall of the tank body is also provided with a circle of spray heads, the spray heads face the filter cylinder, and the spray heads are connected with the solvent tank.
Furthermore, more than two layers of interlayers are arranged in the tank body of the evaporating tank, and a filter cylinder, a vacuumizing interface and a spray head are arranged below each layer of interlayer.
Furthermore, after the primary impregnation tank finishes impregnation, part of the solvent is pumped away through the liquid pumping pipe, and the amount of the solvent entering the evaporation tank is controlled.
Further, the working method comprises the following steps:
1) Separating the fermentation liquor in a centrifugal separator, adding the solid strains into a first-stage impregnation tank, adding a solvent, mixing, pressurizing at the same time, keeping the pressure at 0.5MPa, maintaining the pressure for 1 hour, opening a feed valve, and allowing the mixed liquor to enter the top of an evaporation tank under the action of pressure;
2) Opening the atomizing nozzle of the first interlayer, opening a first layer vacuumizing interface for vacuumizing, keeping the pressure for 10 minutes after the vacuum degree reaches-0.07 MPa, atomizing and evaporating the mixed liquid under the action of negative pressure, opening a first layer spray head for leaching the filter cylinder, and sequentially opening the atomizing nozzle, the vacuumizing interface and the spray head of the next interlayer after the completion; and finally, the leacheate enters a secondary impregnation tank, and a solvent is supplemented for impregnation.
The invention improves the scheme of grinding, crushing and extracting sclareol in the prior art, and the grinding method has poor effect of crushing cell walls because the cell walls of the saccharomycetes are softer. The wall breaking efficiency of the yeast cell wall can be greatly improved by adopting a grinding means after freezing by liquid nitrogen, but the cost is too high, and the method is only suitable for being carried out in a laboratory and is not suitable for industrial amplification. The improved method adopted by the invention is to presoak the strains by using the solvent under pressure before grinding, so that part of the solvent is permeated into cells, then vacuumizing is carried out, the solvent in the cells is evaporated into a gaseous state, the volume is expanded, the subsequent grinding and wall breaking are facilitated, and the extraction yield of the sclareol is improved. The purification scheme of the invention has the advantages of low cost of raw materials and devices, short extraction process period and suitability for industrial purification of biologically fermented sclareol products.
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a schematic structural view of a primary impregnation tank according to the present invention;
FIG. 3 is a schematic view of the construction of the evaporation can of the present invention.
Detailed Description
The following describes the embodiments of the present invention in detail with reference to specific examples.
Example 1
Referring to fig. 1-3, a sclareol purification method comprises the following steps:
1) Carrying out solid-liquid separation on fermentation liquor to obtain a solid-phase strain, pretreating the strain, adding a solvent, grinding and crushing the strain, and filtering to obtain a filtrate;
2) Evaporating and crystallizing the filtrate to obtain sclareol;
in the step 1), the pretreatment is to add the bacterial strain into a part of solvent, dip and mix under the condition of pressurization, vacuumize the mixture and evaporate the solvent.
During pretreatment, the pressure is not lower than 0.5MPa when pressurizing, and the vacuum degree is not lower than-0.07 MPa when vacuumizing.
In the scheme, the solvent is an organic solvent with a lower boiling point, such as ethanol, acetone or n-hexane; taking ethanol as an example, the boiling point is about 40 ℃ when the vacuum degree is-0.07 MPa. Under the pressurization condition, the permeability of the solvent to the bacterial strain cells is improved, and part of ethanol permeates into the cells. When the vacuum is pumped, the ethanol permeating into the cells of the strain is gasified, so that the cells are expanded rapidly, the cell walls of part of the cells are broken when the cells are expanded, and the expanded cells are easy to break when being ground subsequently, thereby improving the effect of breaking the cell walls. In order to accelerate the vaporization of the solvent, the container can be appropriately heated to a corresponding boiling point simultaneously when the vacuum is applied.
Example 2
As shown in fig. 1 to fig. 3, a purification apparatus for sclareol production: comprises a centrifugal separator 1, a primary impregnation tank 2, an evaporation tank 3, a secondary impregnation tank 4, a bead mill 5, a filter 6 and a crystallizer 7 which are connected in sequence; the primary impregnation tank is provided with a compressed air interface 201; the evaporation tank is provided with a vacuumizing interface 301; the first-stage impregnation tank and the second-stage impregnation tank are provided with liquid inlet pipes, and the liquid inlet pipes are connected to the solvent tank; the bottom of the first stage impregnation tank is connected to the top of the evaporation tank by a connecting pipe, which is provided with a feed valve 202. The compressed air interface is connected with the air compression system and used for providing pressure for the primary impregnation tank, the air compressor of the air compression system can provide pressure above 0.5MPa, and the air inlet of the air compressor is provided with the filter for filtering impurities in the air. The vacuum pumping interface is used for being connected with a vacuum pumping system, and a vacuum pump of the vacuum pumping system can provide vacuum degree of more than-0.07 MPa. The vacuum pumping system is provided with a condenser for recovering the evaporated solvent, and the recovered solvent is returned to the secondary impregnation tank or the solvent tank.
A filter cylinder 203 is arranged in the tank body of the primary impregnation tank, the upper end of the filter cylinder is closed, the lower end of the filter cylinder is opened, and the lower end of the filter cylinder is connected with the tank wall in a closed manner; a feed pipe 204 is arranged in the middle of the tank body and is used for being connected with the centrifugal separator, and the feed pipe penetrates into the filter cylinder; the compressed air interface 201 is arranged at the top of the tank body; the middle part of the tank body is provided with a liquid pumping pipe 205, the liquid pumping pipe is positioned above the joint of the filter cylinder and the tank wall, and the liquid pumping pipe 205 is connected to the secondary impregnation tank 4.
The purpose of the liquid withdrawal line is to control the amount of solvent entering the evaporation tank. When the amount of the solvent entering the evaporating pot is too large, the gasification speed of the solvent in the cells is slow, and the wall breaking effect is influenced. During solvent extraction, the strain is blocked by the filter cartridge and is prevented from being extracted.
An interlayer is arranged in the tank body of the evaporating tank 3, the interlayer comprises a conical barrel 302, the bottom of the conical barrel is provided with an atomizing nozzle 303, the caliber of the nozzle is 0.1-0.5 mm, a filter cartridge 304 is arranged along the lower part of the interlayer in the tank body, and a vacuumizing interface 301 is arranged on the tank wall below the interlayer; the inner wall of the tank body is also provided with a circle of spray heads 305 which face the filter cylinder and are connected with the solvent tank. And the mixed solution entering the evaporation tank is atomized, the solvent is quickly evaporated, after the atomization, the spray head sprays the solvent, the bacterial strains adhered to the filter cylinder are leached, the leaching solution finally enters the secondary impregnation tank to supplement the solvent for leaching, and then enters the bead mill to be ground and crushed, and the filtrate is filtered to be crystallized.
Example 3
As shown in fig. 3, on the basis of embodiment 2, the structure of the evaporation tank is improved in this embodiment, more than two layers of interlayers are arranged in the tank body of the evaporation tank, and a filter cartridge, a vacuum pumping interface and a spray header are arranged below each layer of interlayer.
When the evaporation tank with the structure works, the working method comprises the following steps:
1) Separating the fermentation liquor in a centrifugal separator, adding the solid bacterial strain into a primary impregnation tank, adding a solvent, mixing, pressurizing at the same time, keeping the pressure at 0.5MPa, maintaining the pressure for 1 hour, opening a feed valve, and allowing the mixed liquor to enter the top of an evaporation tank under the action of pressure;
2) Opening the atomizing nozzle of the first interlayer, opening a first layer vacuumizing interface for vacuumizing, keeping the pressure for 10 minutes after the vacuum degree reaches-0.07 MPa, atomizing and evaporating the mixed liquid under the action of negative pressure, opening a first layer spray head for leaching the filter cylinder, and sequentially opening the atomizing nozzle, the vacuumizing interface and the spray head of the next interlayer after the completion; finally, the leacheate enters a secondary impregnation tank, and a solvent is supplemented for impregnation.
The purpose of adopting the scheme is that the permeability of cell walls is improved through the strain subjected to the first vacuumizing evaporation treatment, the amount of the solvent penetrating into the cell is increased after the solvent is added, the wall breaking effect on the strain cells is better when the vacuumizing evaporation is carried out again, and the full expansion and the wall breaking of the strain cells are facilitated through multi-stage solvent leaching and vacuumizing evaporation.
Claims (9)
1. A sclareol purification method is characterized by comprising the following steps:
1) Carrying out solid-liquid separation on fermentation liquor to obtain a solid-phase strain, pretreating the strain, adding a solvent, grinding and crushing the strain, and filtering to obtain a filtrate;
2) Evaporating and crystallizing the filtrate to obtain sclareol;
in the step 1), the pretreatment is to add the bacterial strain into a part of solvent, dip and mix under the condition of pressurization, vacuumize the mixture and evaporate the solvent.
2. The method of purifying sclareol as claimed in claim 1, wherein: during pretreatment, the pressure is not lower than 0.5MPa when the pressure is pressurized, and the vacuum degree is not lower than-0.07 MPa when the vacuum is pumped.
3. The method of purifying sclareol as claimed in claim 1, wherein: in the step 1), the solvent is ethanol, acetone or n-hexane.
4. The utility model provides a sclareol production is with purification device which characterized in that: comprises a centrifugal separator, a primary impregnation tank, an evaporation tank, a secondary impregnation tank, a bead mill, a filter and a crystallizer which are connected in sequence; the primary impregnation tank is provided with a compressed air interface; the evaporation tank is provided with a vacuumizing interface; the first-stage impregnation tank and the second-stage impregnation tank are provided with liquid inlet pipes which are connected to the solvent tank; the bottom of the first-stage impregnation tank is connected to the top of the evaporation tank through a connecting pipe, and the connecting pipe is provided with a feed valve.
5. The purification apparatus for sclareol production as claimed in claim 4, wherein: a filter cylinder is arranged in the tank body of the primary impregnation tank, the upper end of the filter cylinder is closed, the lower end of the filter cylinder is opened, and the lower end of the filter cylinder is connected with the tank wall in a closed manner; a feed pipe is arranged in the middle of the tank body and is used for being connected with the centrifugal separator, and the feed pipe penetrates into the filter cylinder; the compressed air interface is arranged at the top of the tank body; the middle part of the tank body is provided with a liquid pumping pipe which is positioned above the joint of the filter cylinder and the tank wall and is connected to the secondary dipping tank.
6. The purification apparatus for sclareol production as claimed in claim 4, wherein: an interlayer is arranged in the tank body of the evaporation tank, the interlayer comprises a conical cylinder, an atomizing spray head is arranged at the bottom of the conical cylinder, a filter cylinder is arranged in the tank body along the lower part of the interlayer, and a vacuumizing interface is arranged on the tank wall below the interlayer; the inner wall of the tank body is also provided with a circle of spray heads, the spray heads face the filter cylinder, and the spray heads are connected with the solvent tank.
7. The purification apparatus for sclareol production as claimed in claim 6, wherein: more than two layers of interlayers are arranged in the tank body of the evaporating tank, and a filter cylinder, a vacuumizing interface and a spray header are arranged below each layer of interlayer.
8. The purification apparatus for sclareol production as claimed in claim 4, wherein: after the primary impregnation tank finishes impregnation, part of the solvent is pumped away through a liquid pumping pipe, and the amount of the solvent entering the evaporation tank is controlled.
9. The purification apparatus for sclareol production as claimed in claim 7, wherein the working method comprises the steps of:
1) Separating the fermentation liquor in a centrifugal separator, adding the solid bacterial strain into a primary impregnation tank, adding a solvent, mixing, pressurizing at the same time, keeping the pressure at 0.5MPa, maintaining the pressure for 1 hour, opening a feed valve, and allowing the mixed liquor to enter the top of an evaporation tank under the action of pressure;
2) Opening the atomizing nozzle of the first interlayer, opening a first vacuumizing interface to vacuumize, maintaining the pressure for 10 minutes after the vacuum degree reaches-0.07 MPa, atomizing and evaporating the mixed liquid under the action of negative pressure, opening a first spray header to drip a filter cylinder, and sequentially opening the atomizing nozzle, the vacuumizing interface and the spray header of the next interlayer after the mixed liquid is completely atomized and evaporated; finally, the leacheate enters a secondary impregnation tank, and a solvent is supplemented for impregnation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211342182.1A CN115636729A (en) | 2022-10-31 | 2022-10-31 | Method and device for purifying sclareol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211342182.1A CN115636729A (en) | 2022-10-31 | 2022-10-31 | Method and device for purifying sclareol |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101622357A (en) * | 2007-03-06 | 2010-01-06 | 花王株式会社 | Method for production of microbial fermentation product |
| CN102503775A (en) * | 2011-10-19 | 2012-06-20 | 蒲县洁舒康香料香精有限公司 | Production process of sclareol |
| CN103215135A (en) * | 2013-04-07 | 2013-07-24 | 安徽嘉旗粮油工程技术有限公司 | Method for synchronously extracting sage clary essential oil and sclareol from sage clary |
| CN112679314A (en) * | 2020-12-29 | 2021-04-20 | 西安天美生物科技股份有限公司 | Preparation process of sclareol |
| CN114573421A (en) * | 2022-03-17 | 2022-06-03 | 北京理工大学 | Method for extracting and purifying sclareol from sclareol fermentation liquor |
-
2022
- 2022-10-31 CN CN202211342182.1A patent/CN115636729A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101622357A (en) * | 2007-03-06 | 2010-01-06 | 花王株式会社 | Method for production of microbial fermentation product |
| CN102503775A (en) * | 2011-10-19 | 2012-06-20 | 蒲县洁舒康香料香精有限公司 | Production process of sclareol |
| CN103215135A (en) * | 2013-04-07 | 2013-07-24 | 安徽嘉旗粮油工程技术有限公司 | Method for synchronously extracting sage clary essential oil and sclareol from sage clary |
| CN112679314A (en) * | 2020-12-29 | 2021-04-20 | 西安天美生物科技股份有限公司 | Preparation process of sclareol |
| CN114573421A (en) * | 2022-03-17 | 2022-06-03 | 北京理工大学 | Method for extracting and purifying sclareol from sclareol fermentation liquor |
Non-Patent Citations (1)
| Title |
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| 崔春: "食品蛋白质控制酶解技术", 中国轻工业出版社, pages: 391 - 393 * |
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