CN112778084A - Extraction process of sclareol - Google Patents
Extraction process of sclareol Download PDFInfo
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- CN112778084A CN112778084A CN202110130480.3A CN202110130480A CN112778084A CN 112778084 A CN112778084 A CN 112778084A CN 202110130480 A CN202110130480 A CN 202110130480A CN 112778084 A CN112778084 A CN 112778084A
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- extraction
- sclareol
- solvent
- flat
- continuous
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- 238000000605 extraction Methods 0.000 title claims abstract description 104
- 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 102
- 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 51
- 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 51
- 239000002904 solvent Substances 0.000 claims abstract description 48
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 42
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 30
- 239000003208 petroleum Substances 0.000 claims description 20
- 239000002994 raw material Substances 0.000 claims description 20
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 claims description 9
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 9
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 9
- 238000000034 method Methods 0.000 claims description 9
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 claims description 6
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 6
- 239000003960 organic solvent Substances 0.000 claims description 5
- 239000000843 powder Substances 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 2
- 239000007788 liquid Substances 0.000 abstract description 12
- 230000001276 controlling effect Effects 0.000 description 12
- 238000001035 drying Methods 0.000 description 9
- 235000002911 Salvia sclarea Nutrition 0.000 description 8
- 244000182022 Salvia sclarea Species 0.000 description 8
- 239000000463 material Substances 0.000 description 6
- 244000124853 Perilla frutescens Species 0.000 description 4
- 235000004348 Perilla frutescens Nutrition 0.000 description 4
- 238000005086 pumping Methods 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 238000004364 calculation method Methods 0.000 description 3
- 239000010633 clary sage oil Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 229940112950 sage extract Drugs 0.000 description 3
- 239000001691 salvia sclarea Substances 0.000 description 3
- DOIRQSBPFJWKBE-UHFFFAOYSA-N dibutyl phthalate Chemical group CCCCOC(=O)C1=CC=CC=C1C(=O)OCCCC DOIRQSBPFJWKBE-UHFFFAOYSA-N 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 235000013599 spices Nutrition 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 241000233866 Fungi Species 0.000 description 1
- 244000061176 Nicotiana tabacum Species 0.000 description 1
- 235000002637 Nicotiana tabacum Nutrition 0.000 description 1
- IMKJGXCIJJXALX-SHUKQUCYSA-N Norambreinolide Chemical compound CC([C@@H]1CC2)(C)CCC[C@]1(C)[C@@H]1[C@]2(C)OC(=O)C1 IMKJGXCIJJXALX-SHUKQUCYSA-N 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 125000003158 alcohol group Chemical group 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- IMKJGXCIJJXALX-UHFFFAOYSA-N ent-Norambreinolide Natural products C1CC2C(C)(C)CCCC2(C)C2C1(C)OC(=O)C2 IMKJGXCIJJXALX-UHFFFAOYSA-N 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 235000013355 food flavoring agent Nutrition 0.000 description 1
- 230000012010 growth Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000010813 internal standard method Methods 0.000 description 1
- 229930002697 labdane diterpene Natural products 0.000 description 1
- 239000002304 perfume Substances 0.000 description 1
- 230000008635 plant growth Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229940096995 sclareolide Drugs 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2602/00—Systems containing two condensed rings
- C07C2602/02—Systems containing two condensed rings the rings having only two atoms in common
- C07C2602/04—One of the condensed rings being a six-membered aromatic ring
- C07C2602/10—One of the condensed rings being a six-membered aromatic ring the other ring being six-membered, e.g. tetraline
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
The invention discloses an extraction process of sclareol, and relates to the technical field of plant extraction. According to the extraction process of sclareol, the extracted feed liquid is concentrated and the solvent is recovered to obtain the sclareol extract, wherein the content of the sclareol is not lower than 30%, the average content is 50-60%, the extraction yield is more than 90%, the extraction yield is high, the extraction amount is large, and the extraction efficiency is high.
Description
Technical Field
The invention relates to the technical field of plant extraction, and particularly relates to a process for extracting sclareol.
Background
Sclareol is a labdane diterpene ditertiary alcohol, is a spice commonly used for cosmetics, perfume and food flavoring, and is a natural raw material for synthesizing high-grade ambergris spice ambergris ether and tobacco flavoring agent sclareolide. Because of its strong antibacterial activity and its regulating action for fungus growth and plant growth, sclareol can also be used in the field of agricultural chemicals. However, the traditional extraction method of sclareol has low extraction efficiency and low extraction yield, and the waste is large.
Disclosure of Invention
Aiming at the problems, the invention aims to provide a novel extraction process technology, which meets the ever-growing demand of the market for sclareol, improves the economic value of sclareol and reduces the production cost of sclareol, and the specific scheme is as follows:
a process for extracting sclareol comprises continuously extracting sclareol with organic solvent as solvent, recovering solvent, and making into sclareol product; the mass ratio of the raw materials to the solvent is 1: 2-5; the flat-turn continuous extraction is based on a flat-turn continuous extraction principle or is carried out by using flat-turn continuous extraction equipment manufactured based on the flat-turn continuous extraction principle;
the solvent is selected from one or a mixture of two or more of petroleum ether, cyclohexane, heptane, n-hexane, methanol, toluene, ethanol, acetone and water.
Preferably, the horizontal rotation continuous extraction equipment is a horizontal rotation annular continuous extractor, a horizontal rotation fan-shaped continuous extractor or a horizontal rotation crawler continuous extractor. For example, it is composed of rotor, false bottom, track, material liquid collecting grid, sprayer and rotator, and the whole equipment is sealed by casing. Because the power consumption of the flat-turn continuous extraction equipment is much less than that of other extraction equipment during operation, and the multi-stage countercurrent extraction is adopted, the solvent circulation times are more, the dosage is less, the energy consumption is relatively reduced, the residue of effective components is lower, the extraction yield is high, the extraction amount is large, and the extraction efficiency is high. The flat-turning continuous extraction equipment can realize full-line automatic control of feeding, extraction, solvent recovery, material drying and the like, can greatly reduce the labor intensity, improve the production conditions, and has the advantages of less investment, large extraction amount, high automation degree and the like compared with the traditional extraction.
Preferably, the particle size of the raw material is not more than 2 cm, and the powder degree is not less than 20 meshes.
Preferably, the extraction temperature of said continuous extraction with flat rotation is between 30 ℃ and 100 ℃.
Preferably, the extraction time of the continuous extraction by rotation is 30 to 120 minutes.
Preferably, the solvent is selected from petroleum ether or methanol, the extraction temperature is 45-70 ℃, and the extraction time is 60-120 minutes.
Preferably, the solvent is selected from petroleum ether or methanol, the extraction temperature is 60 +/-5 ℃, and the extraction time is 90 minutes.
Preferably, the raw material is fresh or dried flower, stem, leaf of Perilla frutescens Britt Var Acuta Thunb, or oven-dried residue after extraction of Perilla frutescens Britt Var Acuta L.Var.Var.Var.Var.Var.Var.Var.Var.Va.
Preferably, the content of sclareol in the sclareol product is not less than 30%.
The extraction equipment involved in the invention is a horizontal rotation type continuous extractor, or equipment such as a ring-shaped continuous extractor, a fan-shaped continuous extractor, a crawler-type continuous extractor and the like based on the principle of the horizontal rotation type continuous extractor. The extraction method has the advantages of low residue of effective components, high extraction yield, large extraction amount, and high extraction efficiency.
The extracted feed liquid is concentrated to recover the solvent to obtain the sclareol extract, the content of the sclareol is not less than 30 percent, the average content is 50 to 60 percent, the extraction yield is more than 90 percent, and the extraction yield of the traditional method is generally less than 90 percent. (the extraction yield is calculated by the net content of sclareol in the obtained sclareol extract, and the content is detected by gas phase)
Detailed Description
In order to make the technical problems, technical solutions and advantageous effects to be solved by the present application more clearly apparent, the present application is further described in detail below with reference to the embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the present application and are not intended to limit the present application.
Example 1
The sclareol product is prepared by taking sclareol as a raw material and an organic solvent as a solvent, continuously extracting through flat rotation, and recovering the solvent.
The mass ratio of the raw materials to the solvent is 1: 2-5; the solvent is selected from one or a mixture of two or more of petroleum ether, cyclohexane, heptane, n-hexane, methanol, toluene, ethanol, acetone and water; the raw materials are fresh or dried flowers, stems and leaves of the clary sage herb or dried residues after clary sage oil extraction, the granularity of the raw materials is not more than 2 centimeters, and the powder degree is not less than 20 meshes.
The flat-turn continuous extraction is based on a flat-turn continuous extraction principle or uses flat-turn continuous extraction equipment manufactured based on the flat-turn continuous extraction principle; the extraction temperature of the horizontal rotation continuous extraction is 30-100 ℃, and the extraction time is 30-120 minutes.
Example 2
The sclareol product is prepared by taking sclareol as a raw material and an organic solvent as a solvent, continuously extracting through flat rotation, and recovering the solvent.
The mass ratio of the raw materials to the solvent is 1: 3-4; the solvent is selected from one of petroleum ether or methanol; the raw materials are fresh or dried flowers, stems and leaves of the clary sage herb or dried residues after clary sage oil extraction, the granularity of the raw materials is not more than 2 centimeters, and the powder degree is not less than 20 meshes.
The horizontal rotation continuous extraction is to adopt a horizontal rotation annular continuous extractor, a horizontal rotation fan-shaped continuous extractor or a horizontal rotation crawler continuous extractor for extraction; the extraction temperature of the horizontal rotation continuous extraction is 45-70 ℃, and the extraction time is 60-120 minutes.
Example 3
The sclareol product is prepared by taking sclareol as a raw material and an organic solvent as a solvent, continuously extracting through flat rotation, and recovering the solvent.
The mass ratio of the raw materials to the solvent is 1: 3-4; the solvent is selected from one of petroleum ether or methanol; the raw materials are fresh or dried flowers, stems and leaves of the clary sage herb or dried residues after clary sage oil extraction, the granularity of the raw materials is not more than 2 centimeters, and the powder degree is not less than 20 meshes.
The horizontal rotation continuous extraction is to adopt a horizontal rotation type annular continuous extractor for extraction; the extraction temperature of the continuous extraction by flat turning is 60 +/-5 ℃, and the extraction time is 90 minutes.
In the following examples, the determination method of the sclareol content in the sclareol extract is a meteorological internal standard method, and the specific conditions are as follows: the instrument is an Agilent gas detector and a capillary gas chromatographic column, the model is DB-624, and the internal standard substance is dibutyl phthalate. The temperature of the column oven is 250 ℃, the temperature of the injection port is 270 ℃, and the temperature of the detector is 280 ℃.
The calculation method of the extraction yield comprises the following steps: the sclareol content of the sclareol hay was generally about 1.8% to 2.0% (specifically, the average content was 1.9% in the test, which is calculated from the difference in the production area and the water content of the sclareol hay, and thus, some results were found to be greater than 100%). The calculation method of the extracted sclareol comprises the following steps: the weight of the extract obtained by extraction is multiplied by the content of the extract. The calculation method of the extraction yield comprises the following steps: the extracted sclareol was divided by the weight of the hay and divided by the average content of 1.9.
Example 4
Uniformly adding 500Kg of crushed clary sage hay into a feed inlet of a horizontal rotation type continuous extractor, adding 1300Kg of petroleum ether into a feed liquid circulating spray port of the extractor in a solvent feed inlet at the other end by a pump, controlling the chain speed of the extractor to be not less than 0.3 r/min, controlling the extraction temperature of the extractor to be 60 ℃, and controlling the extraction time to be 120 min according to the amount of materials and solvents; pumping the feed liquid into a solvent recovery tank to recover the solvent, drying the residue in a drying chamber and recovering the solvent, and removing the residual petroleum ether in a concentration kettle under reduced pressure to obtain 19.4Kg of Perilla frutescens extract with the content of 48.3 percent and the extraction yield of 98.6 percent.
Example 5
Uniformly adding 5000Kg of crushed clary sage hay into a feed inlet of a flat-rotating continuous extractor, adding 16500Kg of petroleum ether into a feed liquid circulating spray port of the extractor in a solvent feed inlet at the other end by a pump, controlling the chain speed of the extractor to be not less than 0.3 r/min, controlling the extraction temperature of the extractor to be 60 ℃, and controlling the extraction time to be 90 min according to the amount of materials and solvents; pumping the feed liquid into a solvent recovery tank to recover the solvent, drying the residue in a drying chamber to recover the solvent, and removing residual petroleum ether in a concentration kettle under reduced pressure to obtain 186.1Kg of Perilla frutescens extract with the content of 50.2% and the extraction yield of 98.3%.
Example 6
Adding 10000Kg of crushed clary sage hay into a feed inlet of a horizontal rotation type continuous extractor uniformly, adding 3300000Kg of petroleum ether into a feed liquid circulating spray port of the extractor in a solvent feed inlet at the other end by a pump, controlling the chain speed of the extractor to be not less than 0.3 r/min, controlling the extraction temperature of the extractor to be 60 ℃, and controlling the extraction time to be 30 min according to the amount of materials and solvents; pumping the feed liquid into a solvent recovery tank to recover the solvent, drying the residue in a drying chamber and recovering the solvent, and removing residual petroleum ether in a concentration kettle under reduced pressure to obtain 372.6Kg of clary sage extract with the content of 49.7% and the extraction yield of 97.5%.
Example 7
Uniformly adding 5000Kg of crushed clary sage hay into a feed inlet of a horizontal rotation type continuous extractor, adding 16500Kg of methanol into a feed liquid circulating spray opening of the extractor in a solvent feed inlet at the other end by a pump, controlling the chain speed of the extractor to be not less than 0.3 r/min, controlling the extraction temperature of the extractor to be 60 ℃, and controlling the extraction time to be 90 min according to the amount of materials and solvents; pumping the feed liquid into a solvent recovery tank to recover the solvent, drying the residue in a drying chamber to recover the solvent, and removing residual petroleum ether in a concentration kettle under reduced pressure to obtain 198.4Kg of clary sage extract with the content of 48.8 percent and the extraction yield of 101.9 percent.
Comparative example tank extraction
Adding 500Kg of crushed clary sage hay into an extraction tank, adding 1000Kg of petroleum ether, heating to 65 ℃ for extraction for 120 minutes, transferring the feed liquid into a concentration kettle, and recovering the petroleum ether; adding 1000Kg of petroleum ether, heating to 65 deg.C, extracting for 90 min, and removing residual petroleum ether under reduced pressure to obtain 17.2Kg of clary sage extract with sclareol content of 45.7% and extraction yield of 82.7%.
The technical contents of the present invention are further illustrated by the examples, so as to facilitate the understanding of the reader, but the embodiments of the present invention are not limited thereto, and any technical extension or re-creation based on the present invention is protected by the present invention.
Claims (9)
1. A process for extracting sclareol is characterized in that sclareol is used as a raw material, an organic solvent is used as a solvent, and the sclareol product is prepared after the continuous extraction through flat turning and the recovery of the solvent; the mass ratio of the raw materials to the solvent is 1: 2-5; the flat-turn continuous extraction is based on a flat-turn continuous extraction principle or is carried out by using flat-turn continuous extraction equipment manufactured based on the flat-turn continuous extraction principle;
the solvent is selected from one or a mixture of two or more of petroleum ether, cyclohexane, heptane, n-hexane, methanol, toluene, ethanol, acetone and water.
2. The process of extracting sclareol according to claim 1, wherein the flat-turn continuous extraction apparatus is a flat-turn endless continuous extractor, a flat-turn fan-shaped continuous extractor, or a flat-turn caterpillar continuous extractor.
3. The process of extracting sclareol as claimed in claim 2, wherein the raw material has a particle size of not more than 2 cm and a powder size of not less than 20 mesh.
4. The extraction process of sclareol as claimed in claim 3, wherein the extraction temperature of the continuous extraction by rotating horizontally is in the range of 30 ℃ to 100 ℃.
5. The process of extracting sclareol as claimed in claim 4, wherein the extraction time of the continuous extraction by rotating horizontally is 30-120 min.
6. The extraction process of sclareol as claimed in claim 5, wherein the solvent is selected from petroleum ether or methanol, the extraction temperature is 45-70 deg.C, and the extraction time is 60-120 min.
7. The extraction process of sclareol as claimed in claim 6, wherein the solvent is selected from petroleum ether or methanol, the extraction temperature is 60 ± 5 ℃ and the extraction time is 90 minutes.
8. The extraction process of sclareol as claimed in claim 7, wherein the raw material is fresh or dried flowers, stems, leaves of sclareol, or oven-dried residue after extraction of sclareol.
9. The process of extracting sclareol as claimed in claim 1, wherein the content of sclareol in the sclareol product is not less than 30%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110130480.3A CN112778084A (en) | 2021-01-29 | 2021-01-29 | Extraction process of sclareol |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202110130480.3A CN112778084A (en) | 2021-01-29 | 2021-01-29 | Extraction process of sclareol |
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| CN112778084A true CN112778084A (en) | 2021-05-11 |
Family
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Family Applications (1)
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| CN202110130480.3A Pending CN112778084A (en) | 2021-01-29 | 2021-01-29 | Extraction process of sclareol |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101229992A (en) * | 2008-01-10 | 2008-07-30 | 华东理工大学 | Method for preparing sclaveol by sclaveol concrete |
| CN101323559A (en) * | 2008-08-05 | 2008-12-17 | 延安禾馨生物制品有限公司 | Preparing process of sclareol |
| CN101391940A (en) * | 2008-10-27 | 2009-03-25 | 西安应化生物技术有限公司 | Method for separating sclareol |
| 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 |
-
2021
- 2021-01-29 CN CN202110130480.3A patent/CN112778084A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101229992A (en) * | 2008-01-10 | 2008-07-30 | 华东理工大学 | Method for preparing sclaveol by sclaveol concrete |
| CN101323559A (en) * | 2008-08-05 | 2008-12-17 | 延安禾馨生物制品有限公司 | Preparing process of sclareol |
| CN101391940A (en) * | 2008-10-27 | 2009-03-25 | 西安应化生物技术有限公司 | Method for separating sclareol |
| 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 |
Non-Patent Citations (1)
| Title |
|---|
| 王沛: "《药物制剂设备》", 1 November 2016 * |
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Application publication date: 20210511 |