CN109180516B - Method for extracting and separating high-purity capsaicin substances from capsicum by using double-aqueous-phase immersion system - Google Patents
Method for extracting and separating high-purity capsaicin substances from capsicum by using double-aqueous-phase immersion system Download PDFInfo
- Publication number
- CN109180516B CN109180516B CN201810938091.1A CN201810938091A CN109180516B CN 109180516 B CN109180516 B CN 109180516B CN 201810938091 A CN201810938091 A CN 201810938091A CN 109180516 B CN109180516 B CN 109180516B
- Authority
- CN
- China
- Prior art keywords
- phase
- aqueous
- capsaicin
- extracting
- separating
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C231/00—Preparation of carboxylic acid amides
- C07C231/22—Separation; Purification; Stabilisation; Use of additives
- C07C231/24—Separation; Purification
Abstract
The invention relates to a method for extracting and separating high-purity capsaicin substances from capsicum by using a double-aqueous-phase impregnation system, which has the advantages of simple process operation, low equipment cost, cheap macroporous resin, low consumption of extraction phase, environmental protection, cyclic use of D101 macroporous resin, ionic liquid and UCON-50-HB-5100, low production cost, high treatment capacity, capability of obtaining the high-purity capsaicin substances without column chromatography separation, effective improvement of the purification efficiency of the capsaicin substances and suitability for large-scale industrial production.
Description
Technical Field
The invention belongs to the technical field of separation and purification of natural functional components, and relates to a method for extracting and separating high-purity capsaicin substances from capsicum by using a two-aqueous-phase immersion system.
Background
The natural capsaicin material is widely applied to the fields of military affairs, light chemical industry, food, medicine and the like, and the utilization of the capsicum in China is also concentrated in the primary processing food industry. In the aspect of deep processing of the capsicum, whether the scale or the technology is different from the similar industries at abroad, the demand of the domestic market for the capsicum base material is mainly met by import. At present, the separation and purification of high-purity capsaicin substances are still relatively tedious and time-consuming work.
The traditional separation means generally has the problems of low separation efficiency, large solvent consumption, high production cost and the like. The emerging simulated moving bed chromatography or counter-current chromatography is also required to prepare a crude product based on the traditional separation means and then further purify the crude product, and has the defects of small treatment capacity, long production period, expensive equipment and the like, so that the method is not beneficial to large-scale industrial production.
The double water phase extraction technology is a promising technology and has the advantages of short extraction time, low energy consumption, good biocompatibility, easy amplification and the like. At present, the technology has been widely applied to primary recovery and purification processes of various biological products. The aqueous two-phase impregnating resin is a separation resin with excellent performance which combines ion exchange resin and aqueous two-phase extraction technology. Similar to conventional solvent-impregnated extraction, the extractant in the aqueous two-phase impregnated resin is distributed in a uniform liquid layer, even in a monomolecular layer, over the entire surface of the pores of the resin. The target extract can be uniformly absorbed in the whole resin particles in the extraction process, and the impregnating resin has the advantages of less extractant loss, large loading capacity, quick phase separation, convenient use and the like. The double-aqueous-phase immersion extraction technology constructed by the invention has the advantages of less consumption of an extracting agent, easiness in recovery, high extraction rate, high phase separation speed, no need of centrifugal equipment, convenience in operation, large treatment capacity, easiness in expansion and the like, and can effectively reduce the energy consumption problem of extraction and separation of high-purity capsaicin substances.
Disclosure of Invention
The invention provides a novel method for extracting and separating high-purity capsaicin substances from hot peppers by using a two-aqueous-phase immersion system, aiming at the problems of low separation efficiency, high solvent consumption, high production cost and the like of the traditional separation means.
In order to achieve the purpose, the invention is realized by adopting the following technical scheme:
according to the invention, the commercially available pod pepper is used as a raw material, the raw material is dried by an oven at 45 ℃, then is placed in a crusher to be crushed, and the chili powder is placed in a reagent bottle for later use.
A method for extracting and separating high-purity capsaicin substances from hot peppers by using a two-aqueous-phase immersion system comprises the following steps:
(1) preparing a random copolymer (UCON-50-HB-5100) of ethylene oxide and propylene oxide containing ionic liquid (1-ethyl-3-methyl imidazole hydrogen sulfate, 1-ethyl-3-methyl imidazole acetate and 1-ethyl-3-methyl imidazole bromide)/ammonium sulfate aqueous two-phase system, and respectively taking out an upper phase and a lower phase for later use;
(2) placing the D101 macroporous resin and the upper phase of the double-water-phase system in the step (1) in a conical flask according to the mass ratio of 1 (5-20) (w/w) for mixing, standing the mixed system at room temperature, performing ultrasonic treatment, filtering by using a funnel, placing the D101 macroporous resin impregnated resin between two pieces of dried filter paper to remove liquid on the surface of the D101 macroporous resin impregnated resin, obtaining a D101 double-water-phase impregnated extraction system, and placing the D101 double-water-phase impregnated extraction system in a sealing bag for later use;
(3) adding chilli powder into the aqueous two-phase system in the step (1), mixing with the aqueous two-phase D101 dipping and extracting system in the step (2), and oscillating at constant temperature;
(4) after extraction, filtering and taking out the D101 aqueous two-phase immersion extraction system in the step (3), and placing the system in a dilute alkali solution for oscillation; filtering and taking out the D101 macroporous resin (which can be recycled), and heating the solution until UCON-50-HB-5100 is separated out (which can be recycled);
(5) concentrating the capsaicin dilute alkali solution obtained in the step (4) until the content of the capsaicin compound is more than 35%, adjusting the pH value of the aqueous solution to 7.0 by using dilute hydrochloric acid, and standing and crystallizing at the temperature of 4-6 ℃ to obtain capsaicin substance crystals.
As a further preferable scheme of the invention, the aqueous solution crystallized in the step (5) is placed in a rotary evaporator for rotary evaporation to obtain the ionic liquid for recycling.
In a further preferred embodiment of the present invention, in the step (1), the ionic liquid is any one of 1-ethyl-3-methylimidazole hydrogensulfate, 1-ethyl-3-methylimidazole acetate, and 1-ethyl-3-methylimidazole bromide.
As a further preferable scheme of the invention, the aqueous two-phase system in the step (1) comprises the following components: the mass fraction of the random copolymer of ethylene oxide and propylene oxide is 16-20%; the mass fraction of ammonium sulfate is 12-15%; the mass fraction of the ionic liquid is between 8 and 15 percent, the balance is Beritent-Labbson buffer solution with the pH value of 4 to 9, and the operating temperature is 25 ℃.
As a further preferable scheme of the invention, in the step (2), the mass ratio of the D101 macroporous resin to the upper phase of the double water phase system is 1:15, and the mixed system stands for 24 hours at room temperature and then is subjected to ultrasonic treatment for 2 hours.
As a further preferable scheme of the invention, the constant-temperature shaking time in the step (3) is 0.5 to 3 hours.
As a further preferable scheme of the invention, in the step (4), the D101 aqueous two-phase immersion extraction system is placed in a dilute alkali solution with the pH value of 10 to be oscillated for 1 h; filtering to obtain D101 macroporous resin, heating the solution to 60 ℃, and separating out UCON-50-HB-5100.
Compared with the prior art, the invention has the advantages and positive effects that:
the method has the advantages of simple process operation, low equipment cost, cheap macroporous resin, low extraction phase consumption, environmental friendliness, cyclic use of the D101 macroporous resin, the UCON-50-HB-5100 and the ionic liquid, low production cost, high treatment capacity, capability of obtaining the high-purity capsaicin substance without column chromatography separation, effective improvement on the purification efficiency of the capsaicin substance and suitability for large-scale industrial production.
Detailed Description
In order that the above objects, features and advantages of the present invention may be more clearly understood, the present invention will be further described with reference to specific embodiments. It should be noted that the embodiments and features of the embodiments of the present application may be combined with each other without conflict.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, however, the present invention may be practiced in other ways than those specifically described herein, and thus the present invention is not limited to the specific embodiments of the present disclosure.
Example 1, the following procedure was used to extract and isolate high purity capsaicin.
(1) Respectively weighing 5.0g of 1-ethyl-3-methylimidazole bisulfate, 5.0g of UCON-50-HB-51009.0 g and 7.0g of ammonium sulfate in a test tube by using an analytical balance, adding a Beriten-Labishon buffer solution with the pH value of 4 (room temperature) until the total weight is 50g, configuring a two-aqueous-phase system with the system components of 10% (w/w) of 1-ethyl-3-methylimidazole bisulfate, 10% (w/w) of UCON-50-HB-510018% (w/w) and 14% (w/w) of ammonium sulfate, placing the system in an oscillator, oscillating for 10min at the temperature of 25 ℃, centrifuging for 5min by using a centrifuge at the rotating speed of 2000 r/min, and respectively taking out the upper phase and the lower phase of the system for later use after the centrifugation is finished.
(2) And (2) placing the D101 macroporous resin and the phase of the aqueous two-phase system in the step (1) in a conical flask according to the mass ratio of 1:15 (w/w) for mixing, standing the mixed system at room temperature for 24 hours, then carrying out ultrasonic treatment for 2 hours, then filtering by using a funnel, placing the D101 impregnated resin between two pieces of dry filter paper to remove liquid on the surface of the D101 impregnated resin, and placing the prepared D101 aqueous two-phase impregnated extraction system in a sealing bag for later use.
(3) And (3) adding chilli powder into the lower aqueous two-phase system in the step (1), mixing with the aqueous two-phase D101 dipping and extracting system in the step (2), and oscillating at constant temperature for 1 hour.
(4) And (4) after the extraction is finished, filtering and taking out the D101 aqueous two-phase dipping extraction system in the step (3), and placing the dipping extraction system in a dilute alkali solution with the pH value of 10 for oscillation for 1 hour. Filtering to take out the D101 macroporous resin (which can be recycled), and heating the solution to 60 ℃ to precipitate UCON-50-HB-5100 (which can be recycled). The high performance liquid chromatography determines that the recovery rate of the capsaicin in the dilute alkali solution reaches 95.0 percent.
(5) Concentrating the capsaicin diluted solution obtained in the step (4) until the content of the capsaicin compound is more than 35%, adjusting the pH of the aqueous solution to 7.0 by using diluted hydrochloric acid, standing and crystallizing at the temperature of 4-6 ℃ to obtain capsaicin substance crystals with the purity of 97.5% and the recovery rate of 89.0%.
(6) And (5) placing the aqueous solution crystallized in the step (5) into a rotary evaporator for rotary evaporation to obtain ionic liquid for recycling.
Example 2, the following procedure was used to extract and isolate high purity capsaicin.
(1) Respectively weighing 4.0g of 1-ethyl-3-methylimidazole acetate, 4.0g of UCON-50-HB-510016.0 g and 7.5g of ammonium sulfate in a test tube by using an analytical balance, adding a birutan-robioson buffer solution with the pH value of 9 (room temperature) to 50g, configuring a two-aqueous-phase system with the components of 8% (w/w) of 1-ethyl-3-methylimidazole hydrogen sulfate, 8% (w/w) of UCON-50-HB-510016% (w/w) and 15% (w/w) of ammonium sulfate, placing the system in an oscillator, oscillating for 10min at the temperature of 25 ℃, centrifuging for 5min at the rotating speed of 2000 revolutions per minute by using a centrifuge, and respectively taking out the upper phase and the lower phase of the system for later use after the centrifugation is finished.
(2) And (2) placing the D101 macroporous resin and the phase of the aqueous two-phase system in the step (1) in a conical flask according to the mass ratio of 1:15 (w/w) for mixing, standing the mixed system at room temperature for 24 hours, then carrying out ultrasonic treatment for 2 hours, then filtering by using a funnel, placing the D101 impregnated resin between two pieces of dry filter paper to remove liquid on the surface of the D101 impregnated resin, and placing the prepared D101 aqueous two-phase impregnated extraction system in a sealing bag for later use.
(3) And (3) adding chilli powder into the lower aqueous two-phase system in the step (1), mixing with the aqueous two-phase D101 dipping and extracting system in the step (2), and oscillating at constant temperature for 1 hour.
(4) And (4) after the extraction is finished, filtering and taking out the D101 aqueous two-phase dipping extraction system in the step (3), and placing the dipping extraction system in a dilute alkali solution with the pH value of 10 for oscillation for 1 hour. Filtering to take out the D101 macroporous resin (which can be recycled), and heating the solution to 60 ℃ to precipitate UCON-50-HB-5100 (which can be recycled). The high performance liquid chromatography determines that the recovery rate of the capsaicin in the dilute alkali solution reaches 93.0 percent.
(5) Concentrating the capsaicin dilute solution obtained in the step (4) until the content of the capsaicin compound is more than 35%, adjusting the pH of the aqueous solution to 7.0 by using dilute hydrochloric acid, standing and crystallizing at the temperature of 4-6 ℃ to obtain capsaicin substance crystals with the purity of 99.5% and the recovery rate of 87.4%.
(6) And (5) placing the aqueous solution crystallized in the step (5) into a rotary evaporator for rotary evaporation to obtain ionic liquid for recycling.
Example 3, the following procedure was used to extract and isolate high purity capsaicin.
(1) 15.0g of 1-ethyl-3-methyl imidazole bromide, 15.0g of UCON-50-HB-510010.0 g and 7.0g of ammonium sulfate are respectively weighed by an analytical balance and placed in a test tube, a biriten-robioson buffer solution with the pH value of 4 is added to 50g, a two-water-phase system with the components of 15% (w/w) of 1-ethyl-3-methyl imidazole hydrogen sulfate, 15% (w/w) of UCON-50-HB-510020% (w/w) and 12% (w/w) of ammonium sulfate is configured, the system is placed in an oscillator to be oscillated for 10min at the temperature of 25 ℃, then a centrifuge is used for centrifuging for 5min at the rotating speed of 2000 revolutions per minute, and the upper phase and the lower phase of the system are respectively taken out for standby after the centrifugation is finished.
(2) And (2) placing the D101 macroporous resin and the phase of the aqueous two-phase system in the step (1) in a conical flask according to the mass ratio of 1:15 (w/w) for mixing, standing the mixed system at room temperature for 24 hours, then carrying out ultrasonic treatment for 2 hours, then filtering by using a funnel, placing the D101 impregnated resin between two pieces of dry filter paper to remove liquid on the surface of the D101 impregnated resin, and placing the prepared D101 aqueous two-phase impregnated extraction system in a sealing bag for later use.
(3) And (3) adding chilli powder into the lower aqueous two-phase system in the step (1), mixing with the aqueous two-phase D101 dipping and extracting system in the step (2), and oscillating at constant temperature for 1 hour.
(4) And (4) after the extraction is finished, filtering and taking out the D101 aqueous two-phase dipping extraction system in the step (3), and placing the dipping extraction system in a dilute alkali solution with the pH value of 10 for oscillation for 1 hour. Filtering to take out the D101 macroporous resin (which can be recycled), and heating the solution to 60 ℃ to precipitate UCON-50-HB-5100 (which can be recycled). The high performance liquid chromatography determines that the recovery rate of the capsaicin in the dilute alkali solution reaches 92.6 percent.
(5) Concentrating the capsaicin dilute solution obtained in the step (4) until the content of the capsaicin compound is more than 35%, adjusting the pH of the aqueous solution to 7.0 by using dilute hydrochloric acid, standing and crystallizing at the temperature of 4-6 ℃ to obtain capsaicin substance crystals with the purity of 92.5% and the recovery rate of 87.1%.
(6) And (5) placing the aqueous solution crystallized in the step (5) into a rotary evaporator for rotary evaporation to obtain ionic liquid for recycling.
Example 4, the following procedure was used to extract and isolate high purity capsaicin.
(1) 15.0g of 1-ethyl-3-methyl imidazole bromide, 15.0g of UCON-50-HB-510010.0 g and 7.0g of ammonium sulfate are respectively weighed by an analytical balance and placed in a test tube, a biriten-robioson buffer solution with the pH value of 4 is added to 50g, a two-water-phase system with the components of 15% (w/w) of 1-ethyl-3-methyl imidazole hydrogen sulfate, 15% (w/w) of UCON-50-HB-510020% (w/w) and 12% (w/w) of ammonium sulfate is configured, the system is placed in an oscillator to be oscillated for 10min at the temperature of 25 ℃, then a centrifuge is used for centrifuging for 5min at the rotating speed of 2000 revolutions per minute, and the upper phase and the lower phase of the system are respectively taken out for standby after the centrifugation is finished.
(2) And (2) placing the D101 macroporous resin and the phase of the aqueous two-phase system in the step (1) in a conical flask according to the mass ratio of 1:20 (w/w) for mixing, standing the mixed system at room temperature for 24 hours, then carrying out ultrasonic treatment for 2 hours, then filtering by using a funnel, placing the D101 impregnated resin between two pieces of dry filter paper to remove liquid on the surface of the D101 impregnated resin, and placing the prepared D101 aqueous two-phase impregnated extraction system in a sealing bag for later use.
(3) And (3) adding chilli powder into the lower aqueous two-phase system in the step (1), mixing with the aqueous two-phase D101 dipping and extracting system in the step (2), and oscillating at constant temperature for 1.5 hours.
(4) And (4) after the extraction is finished, filtering and taking out the D101 aqueous two-phase dipping extraction system in the step (3), and placing the dipping extraction system in a dilute alkali solution with the pH value of 10 for oscillation for 1 hour. Filtering to take out the D101 macroporous resin (which can be recycled), and heating the solution to 65 ℃ to precipitate UCON-50-HB-5100 (which can be recycled). The high performance liquid chromatography determines that the recovery rate of the capsaicin in the dilute alkali solution reaches 92.6 percent.
(5) Concentrating the capsaicin dilute solution obtained in the step (4) until the content of the capsaicin compound is more than 35%, adjusting the pH of the aqueous solution to 7.0 by using dilute hydrochloric acid, standing and crystallizing at the temperature of 4-6 ℃ to obtain capsaicin substance crystals with the purity of 92.8% and the recovery rate of 87.4%.
(6) And (5) placing the aqueous solution crystallized in the step (5) into a rotary evaporator for rotary evaporation to obtain ionic liquid for recycling.
Example 5, this example utilizes recovered UCON-50-HB-5100 and ionic liquid, other parameters and material addition are identical to those in example 1, finally the obtained capsaicin dilute solution is concentrated to the content of the capsaicin compound of more than 35%, the pH of the aqueous solution is adjusted to 7.0 by dilute hydrochloric acid, standing and crystallizing at 4-6 ℃ to obtain capsaicin material crystals with the purity of 97.4% and the recovery rate of 89.1%.
Example 6, this example recovered UCON-50-HB-5100, D101 macroporous resin and ionic liquid of example 5, all other parameters and substance addition were exactly the same as in example 5, and finally the obtained diluted capsaicin solution was concentrated to a capsaicin content of 35% or more, the pH of the aqueous solution was adjusted to 7.0 with diluted hydrochloric acid, and standing crystallization was carried out at 4-6 ℃ to obtain capsaicin crystals with a purity of 97.5% and a recovery of 89.0%.
The above description is only a preferred embodiment of the present invention, and not intended to limit the present invention in other forms, and any person skilled in the art may apply the above modifications or changes to the equivalent embodiments with equivalent changes, without departing from the technical spirit of the present invention, and any simple modification, equivalent change and change made to the above embodiments according to the technical spirit of the present invention still belong to the protection scope of the technical spirit of the present invention.
Claims (7)
1. A method for extracting and separating capsaicin substances from hot peppers by using a two-aqueous-phase immersion system is characterized by comprising the following steps:
(1) preparing a random copolymer of ethylene oxide and propylene oxide containing ionic liquid/ammonium sulfate aqueous two-phase system, and respectively taking out an upper phase and a lower phase for later use;
(2) placing the D101 macroporous resin and the upper phase of the double-water-phase system in the step (1) in a conical flask according to the mass ratio of 1 (5-20) for mixing, standing the mixed system at room temperature, performing ultrasonic treatment, filtering by using a funnel, placing the D101 macroporous resin impregnated resin between two pieces of dried filter paper to remove liquid on the surface of the D101 macroporous resin impregnated resin to obtain a D101 double-water-phase impregnated extraction system, and placing the D101 double-water-phase impregnated extraction system in a sealing bag for later use;
(3) adding chilli powder into the aqueous two-phase system in the step (1), mixing with the aqueous two-phase D101 dipping and extracting system in the step (2), and oscillating at constant temperature;
(4) after extraction, filtering and taking out the D101 aqueous two-phase immersion extraction system in the step (3), and placing the system in a dilute alkali solution for oscillation; filtering and taking out the D101 macroporous resin, and heating the solution until a random copolymer of ethylene oxide and propylene oxide is separated out;
(5) concentrating the capsaicin dilute alkali solution obtained in the step (4) until the content of the capsaicin compound is more than 35%, adjusting the pH value of the aqueous solution to 7.0 by using dilute hydrochloric acid, and standing and crystallizing at the temperature of 4-6 ℃ to obtain capsaicin substance crystals.
2. The method for extracting and separating the capsaicin materials from the peppers by using the aqueous two-phase immersion system according to claim 1, wherein the aqueous solution crystallized in the step (5) is placed in a rotary evaporator for rotary evaporation to obtain the ionic liquid for recycling.
3. The method for extracting and separating capsaicin from chili peppers by using an aqueous two-phase immersion system according to claim 1 or 2, wherein the ionic liquid in the step (1) is any one of 1-ethyl-3-methylimidazole hydrogen sulfate, 1-ethyl-3-methylimidazole acetate and 1-ethyl-3-methylimidazole bromide.
4. The method for extracting and separating the capsaicin from the peppers by using the aqueous two-phase immersion system according to claim 1 or 2, wherein the aqueous two-phase system in the step (1) comprises the following components: the mass fraction of the random copolymer of ethylene oxide and propylene oxide is 16-20%; the mass fraction of ammonium sulfate is 12-15%; the mass fraction of the ionic liquid is between 8 and 15 percent, the balance is Beritent-Labbson buffer solution with the pH value of 4 to 9, and the operating temperature is 25 ℃.
5. The method for extracting and separating the capsaicin substances from the peppers by using the aqueous two-phase impregnation system according to claim 1 or 2, wherein the mass ratio of the D101 macroporous resin to the aqueous two-phase system in the step (2) is 1:15, and the mixed system is stood for 24 hours at room temperature and then is subjected to ultrasonic treatment for 2 hours.
6. The method for extracting and separating capsaicin from chili peppers by using an aqueous two-phase immersion system according to claim 1 or 2, wherein the shaking time at constant temperature in step (3) is 0.5 to 3 hours.
7. The method for extracting and separating the capsaicin substances from the peppers by using the aqueous two-phase immersion system as claimed in claim 1 or 2, wherein the D101 aqueous two-phase immersion extraction system in the step (4) is placed in a dilute alkali solution with the pH value of 10 for 1 hour; filtering and taking out the D101 macroporous resin, heating the solution to 60 ℃, and precipitating the random copolymer of the ethylene oxide and the propylene oxide.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810938091.1A CN109180516B (en) | 2018-08-17 | 2018-08-17 | Method for extracting and separating high-purity capsaicin substances from capsicum by using double-aqueous-phase immersion system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810938091.1A CN109180516B (en) | 2018-08-17 | 2018-08-17 | Method for extracting and separating high-purity capsaicin substances from capsicum by using double-aqueous-phase immersion system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109180516A CN109180516A (en) | 2019-01-11 |
| CN109180516B true CN109180516B (en) | 2021-03-02 |
Family
ID=64918582
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810938091.1A Active CN109180516B (en) | 2018-08-17 | 2018-08-17 | Method for extracting and separating high-purity capsaicin substances from capsicum by using double-aqueous-phase immersion system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109180516B (en) |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1105591C (en) * | 1999-03-17 | 2003-04-16 | 浙江大学 | Double-water phase distribution and temperature-change solvent counter-extraction process to extract scutellaria flavonoid |
| CN104030935B (en) * | 2014-06-25 | 2015-12-30 | 齐鲁工业大学 | A kind of method of reversed-phase resin purifying capsaicin monomer |
| US10898537B2 (en) * | 2015-07-31 | 2021-01-26 | Delivra Inc. | Transdermal formulations for delivery of capsaicinoids |
| CN107036863A (en) * | 2017-04-28 | 2017-08-11 | 华南理工大学 | A kind of method of glyoxaline ion liquid double-aqueous phase system separation and concentration tetracycline |
-
2018
- 2018-08-17 CN CN201810938091.1A patent/CN109180516B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN109180516A (en) | 2019-01-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103933871B (en) | A kind of preparation method of high stability all-silica MFI type molecular screen membrane | |
| CN104593447B (en) | A kind of energy-conservation preparation technology of high-quality powdered glucose | |
| CN107746142A (en) | Washery slag acid waste water Zero emission method in a kind of Titanium White Production By Sulfuric Acid Process | |
| CN106831951A (en) | A kind of purification process of oxytocin | |
| CN101492484B (en) | Synthetic circulation production process for guanine nucleoside | |
| CN102304134B (en) | Process method for extracting dihydroartemisinin from waste mother liquor in production of dihydroartemisinin | |
| CN109180516B (en) | Method for extracting and separating high-purity capsaicin substances from capsicum by using double-aqueous-phase immersion system | |
| CN102807497A (en) | Method for recovering chloroacetic acid method glycine catalyst methenamine | |
| CN101538179B (en) | Method for preparing compound amino acid organic liquid fertilizer | |
| CN110092772B (en) | Blueberry anthocyanin high-selectivity separation method and separation material | |
| CN103304677B (en) | A kind of method of separation and purification Rhizoma amorphophalli glucomannan | |
| CN105776239A (en) | Preparation method of hierarchical pore AFI structured aluminum phosphate molecular sieve | |
| CN101973983A (en) | Method for extracting orientins from Chinese globeflower flowers | |
| CN108558765A (en) | A kind of ether functional ionic liquids and preparation method thereof | |
| CN104450822A (en) | Method for producing theaflavin from tea polyphenol production wastewater | |
| CN102321125B (en) | Process for extracting gallotannic acid from galla chinensis | |
| CN111018939A (en) | Rapid refining method of tea saponin | |
| CN104974356B (en) | A kind of method that fulvic acid substance is extracted from diatomite | |
| CN113274975B (en) | Chloride ion adsorbent and preparation method and application method thereof | |
| CN104151439A (en) | Preparation method of paecilomyces hepialid mycelium polysaccharide | |
| CN106492764A (en) | A kind of Preparation method and use of folic acid MOFs materials | |
| CN104974036A (en) | Purifying method of crude trimesic acid | |
| CN106854212A (en) | A kind of unformed preparation method of Prezista | |
| CN103708507B (en) | A kind of preparation method of food-grade potassium carbonate | |
| CN106745293B (en) | A kind of preparation method of high-purity rehenic acid ammonium |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |