CN105647647A - Energy-saving agilawood essential oil extraction complete plant and low-temperature extraction technique thereof - Google Patents
Energy-saving agilawood essential oil extraction complete plant and low-temperature extraction technique thereof Download PDFInfo
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- CN105647647A CN105647647A CN201610003890.0A CN201610003890A CN105647647A CN 105647647 A CN105647647 A CN 105647647A CN 201610003890 A CN201610003890 A CN 201610003890A CN 105647647 A CN105647647 A CN 105647647A
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- 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
- C11B9/00—Essential oils; Perfumes
- C11B9/02—Recovery or refining of essential oils from raw materials
- C11B9/025—Recovery by solvent extraction
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/02—Solvent extraction of solids
- B01D11/0215—Solid material in other stationary receptacles
- B01D11/0219—Fixed bed of solid material
-
- 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
- C11B9/00—Essential oils; Perfumes
- C11B9/02—Recovery or refining of essential oils from raw materials
- C11B9/027—Recovery of volatiles by distillation or stripping
Abstract
The invention relates to an energy-saving agilawood essential oil extraction complete plant and a low-temperature extraction technique thereof, belonging to the field of extraction. A solvent turnover tank for supplying a solvent to an extraction tank is arranged in the complete plant; a solvent outlet of the solvent turnover tank is connected with a solvent inlet of the extraction tank; a stirring device and a heat exchanger are arranged in the extraction tank; a liquid discharge port of the extraction tank is connected to an extract inlet of a concentrating tank; a gas discharge port for gasifying the depressurized solvent is arranged in the concentrating tank, and connected with a vacuum pump and a compressor; a liquefied hot solvent pipeline in the compressor is connected to the heat exchanger of the extraction tank through the concentrating tank; and a regenerated solvent outlet of the heat exchanger of the extraction tank is connected with a reflux inlet of the solvent turnover tank. The complete plant cyclically utilizes the solvent, and the heat of the solvent removal is removed by the compressor, thereby lowering the plant pressure of the agilawood essential oil, lowering the energy consumption, ensuring the quality of the essential oil, and enhancing the use value of the essential oil.
Description
Technical field
The present invention relates to a kind of complete set of equipments and extraction process, extract complete set of equipments and low-temperature extraction technique particularly to a kind of energy-saving agilawood essential oil, belong to extraction field.
Background technology
Lignum Aquilariae Resinatum is a kind of timber, spice and Chinese medicine. The resin with strong fragrance, after being subject to wound or fungal infection stimulation, can be secreted in a large number in position, Lignum Aquilariae Resinatum plant pith. These are partly because density is very big, and be otherwise known as " water precipitating is fragrant ". Lignum Aquilariae Resinatum has promoting the circulation of QI to relieve pain, warming middle-JIAO to arrest vomiting, effect of helping inspiration to relieve asthma. It is usually used in chest and abdomen feeling of distension and oppression pain, gastrofrigid vomiting singultus, QI rising in reverse order of suffering from a deficiency of the kidney dyspnea with rapid respiration. Agilawood essential oil is to be refined after distillation extraction by precious Lignum Aquilariae Resinatum, is the elite place of Lignum Aquilariae Resinatum. Human body is had multi-efficiency by agilawood essential oil, for instance: improve gas field, pressure of releiving, sleeping anti-strongly fragrant, conditioning body and mind and promote health new city metabolism etc. Non-renewable due to natural agilawood, the linaloe oil after refinement just more seems rare and precious.
Agilawood essential oil extraction equipment common at present mainly has two kinds, and one therein is carbon dioxide supercritical fluid extraction method, and an other class is vapor extraction method, and both prior aries are respectively present following shortcoming substantially:
In carbon dioxide supercritical fluid extraction method, the general pressure of operating pressure using extraction equipment to reach 20-30Mpa, this high pressure container extracts, the energy needed on the one hand is relatively more, it addition, the equipment run under this high pressure is susceptible to fault, and there is certain danger, the investment of high pressure container is also big, it is also difficult to form large-scale commercial production. The second production technology is steam distillation, and this method is to carry out steam distilled at high operating temperatures, there is problems of operation temperature high, extract effective ingredient is caused and to a certain degree decomposes, and yield is relatively low, and its property of medicine is corresponding also low.
Summary of the invention
In view of carbon dioxide supercritical fluid extraction method pressure is big, equipment investment is high and it is high to there is certain danger, steam distillation operation temperature, extract effective ingredient can cause and to a certain degree decompose, the problems such as yield is relatively low, the present invention provides a kind of energy-saving agilawood essential oil to extract complete set of equipments and low-temperature extraction technique, reduce the equipment pressure of agilawood essential oil, reduce energy consumption, it is ensured that extract the quality of quintessence oil, improve the use value of quintessence oil.
The technical scheme is that a kind of energy-saving agilawood essential oil extracts complete set of equipments, including compressor, vacuum pump and solvent pump, described complete set of equipments arranges the solvent non-conservation tank of oriented extractor supply solvent, solvent non-conservation tank solvent outlet is connected with extractor solvent inlet, extractor includes agitating device, heat-exchanger rig, heating jacket, extractor is provided with leakage fluid dram, leakage fluid dram is connected to concentration tank extract import, the air vent that after being provided with decompression on concentration tank, solvent gasifies, air vent and vacuum pump, compressor connects, the concentrated tank of hot solvent pipeline carrying out compressor is connected to extractor heat-exchanger rig, extractor heat-exchanger rig is connected with solvent non-conservation tank refluxing opening, compressor heat solvent pipe is additionally coupled to heating jacket, it is connected to solvent pump between solvent non-conservation tank solvent outlet and extractor solvent inlet, described solvent non-conservation tank refluxing opening is arranged on solvent non-conservation tank top, solvent outlet is arranged on bottom solvent non-conservation tank, the top of described extractor is provided with charging aperture, solvent inlet, gas outlet, bottom is provided with heating jacket, leakage fluid dram, discharge gate, described gas outlet is respectively through extraction valve, pressed gas valve and vacuum pump, connect between compressor, the top of described concentration tank is provided with extract import, air vent, air vent is provided with air bleeding valve, periphery is provided with hot solvent import and liquid flux outlet, bottom is provided with quintessence oil outlet, hot solvent import is connected to compressor, liquid flux outlet is connected with the heat-exchanger rig in extractor in turn, solvent non-conservation tank refluxing opening.
A kind of agilawood essential oil low-temperature extraction technique, complete set of equipments is extracted including the energy-saving agilawood essential oil described in 1-5, it is characterized in that: described agilawood essential oil extraction process is, the thin slice that Lignum Aquilariae Resinatum wooden plane becomes 0.25��0.3mm adds extractor, according to material, solvent ratios is that the ratio of 1:1 ~ 3 adds propane or butane or 134a solvent in Lignum Aquilariae Resinatum raw material, through soaking, stirring, heating, extract under an increased pressure, extraction times 1-3 time, each extraction time 10-200 minute, then, solvent pump is utilized to be extracted in concentration tank by the extract in extractor, solvent is made to gasify through decompression, realize quintessence oil to separate with solvent, the solvent of gasification utilizes compressor compresses to liquefy, concentrated tank, heat-exchanger rig in extractor imparts heat to concentration tank, the material of heating is needed in extractor, the solvent simultaneously liquefied is cooled down, it is recovered in turnover solvent tank, gas-solvent in extractor under pressure, is fed directly to compressor compresses and becomes liquid, then concentrated tank, heat-exchanger rig condensing cooling, be recovered in solvent non-conservation tank recycle, when the pressure in extractor is 0MPa, utilize vacuum pump to be extracted out by internal gas, then deliver to compressor liquefaction, through concentration tank, heat-exchanger rig condensing cooling, returning in solvent non-conservation tank and recycle, in concentration tank, non-vaporized liquid is agilawood essential oil, discharges from quintessence oil outlet.
Further, in extraction, the temperature of heating is 30-60 DEG C, and extracting pressure is 0.3-1.6Mpa; Thickening temperature 35��70 DEG C, operating pressure 1.6��-0.08MPa;
Further, in extractor, the heat source in precipitation, concentration tank is to utilize compressor air-discharging, gas compression liquefaction liberated heat.
The present invention has the advantages that: add set by arranging agitating device in extractor, arranging heating bottom extractor, under stress can carry out extracting quintessence oil to Lignum Aquilariae Resinatum heating material, stirring, can the solvent in solvent non-conservation tank be joined in extractor by arranging solvent pump, solvent pump can also be utilized to extract extract and to deliver to concentration tank, through decompression in concentration tank, being gasified by solvent, through the solvent of gasification, available compressor makes solvent liquefaction, solvent through liquefaction, heat-exchanger rig through concentration tank and extractor, further condensing cooling liquefies completely, may return to solvent non-conservation tank recycles, by utilizing compressor air-discharging, gas compression liquefaction liberated heat is as extractor, concentration tank heat source, thermal source can be made full use of and reduce heating-up temperature, reduce energy consumption, save the energy, by soaking under an increased pressure, stirring Lignum Aquilariae Resinatum material, the yield of quintessence oil can be improved, by utilizing pressure reducing mode that solvent gasification can be made to separate with quintessence oil, by the solvent after gasification is utilized compressor compresses, the solvent after gasification can be made again to become liquid through cooling heat transferring, return in solvent non-conservation tank, be conducive to recycling, this complete set of equipments can reduce the equipment pressure of agilawood essential oil, reduce energy consumption, ensure to extract the quality of quintessence oil, improve the use value of quintessence oil.
Accompanying drawing explanation
The structural representation of Fig. 1 present invention
Label declaration: 1: solvent outlet, 2: regenerated solvent exports, 3: discharge gate, 4: leakage fluid dram, 4a: tapping valve, 5: regenerated solvent entrance, 6: liquid flux exports, 7: quintessence oil exports, 8: hot solvent import, 9: air valve, 10: extraction valve, 11: pressed gas valve, 12: air vent, 12a: air bleeding valve, 13: extract import, 13a: extract liquid feed valve, 14: solvent inlet, 15: charging aperture, 16: gas outlet, 16a: air outlet valve, 17: refluxing opening, 18: solvent non-conservation tank, 19: extractor, 20: solvent pump, 21: concentration tank, 22: compressor, 23: vacuum pump.
Detailed description of the invention
It is divided into pressure at solvent gas liquefaction process at below 0MPa of the quintessence oil of more than 0MPa and solvent separation process and pressure during extraction; The solvent gas liquefaction process of more than 0MPa solvent gas liquefaction process and below 0MPa it is also classified into during precipitation. Rely on the pressed gas pressure of self in extractor 19 that gas is delivered to compressor 22 during more than 0MPa to liquefy; When the pressure in extractor 19 arrives below 0MPa, it is necessary to carry out extracting the gas in extractor 19 by vacuum pump 23, then gas is delivered to compressor 22 liquefy. But, when extract processes, extract needs to carry out the separation of quintessence oil and solvent, and during separation, solvent can gasify under gasification temperature, and quintessence oil keeps liquid, and the solvent after gasification carries out liquefying again, gas direct liquefaction in extractor 19. The solvent of post liquefaction returns in solvent non-conservation tank 18.
The technical scheme is that a kind of energy-saving agilawood essential oil extracts complete set of equipments, including compressor 22, vacuum pump 23 and solvent pump 20, described complete set of equipments arranges oriented extractor 19 and supplies the solvent non-conservation tank 18 of solvent, solvent non-conservation tank 18 solvent outlet 1 is connected with extractor 19 solvent inlet 14, extractor 19 is provided with agitating device, heat-exchanger rig, the leakage fluid dram 4 of extractor 19 is connected to concentration tank 21 extract import 13, mixed liquor through the liquid extracted and solvent enters in concentration tank 21, the molten air vent 12 that after being provided with decompression on concentration tank 21, solvent gasifies, air vent 12 is provided with air bleeding valve 12a, air vent 12 respectively with vacuum pump 23, compressor 22 connects, the concentrated tank 21 of compressor 22 hot solvent pipeline is connected to the heat-exchanger rig of extractor 19, solvent becomes regenerated solvent after condensation, the regenerated solvent outlet 2 of extractor 19 heat-exchanger rig is connected with solvent non-conservation tank 18 refluxing opening 17, regenerated solvent returns in solvent non-conservation tank 18 and is circulated utilization.
Being connected to solvent pump 20 between solvent outlet 1 and extractor 19 solvent inlet 14 of solvent non-conservation tank 18, described solvent non-conservation tank 18 refluxing opening 17 is arranged on the top of solvent non-conservation tank 18, and solvent outlet 1 is arranged on the bottom of solvent non-conservation tank 18.
The top of described extractor 19 is provided with charging aperture 15, solvent inlet 14, gas outlet 16, and bottom is provided with heating jacket, leakage fluid dram 4, discharge gate 3, described gas outlet 16 are connected with between vacuum pump 23, compressor 22 respectively through extraction valve 10, pressed gas valve 11.
Described concentration tank 21 top is provided with extract import 13, air vent 12, air vent 12 is provided with air bleeding valve 12a, concentration tank 21 periphery is provided with hot solvent import 8 and liquid flux outlet 6, bottom is provided with quintessence oil outlet 7, hot solvent import 8 is connected to compressor 22, and liquid flux outlet 6 is connected with the heat-exchanger rig in extractor, solvent non-conservation tank 18 refluxing opening 17 in turn.
A kind of agilawood essential oil low-temperature extraction technique, complete set of equipments is extracted including above-mentioned energy-saving agilawood essential oil, described agilawood essential oil extraction process is: Lignum Aquilariae Resinatum wooden plane becomes the thin slice of 0.25��0.3mm add extractor 19, according to material, solvent ratios is that the ratio of 1:1 ~ 3 adds propane in Lignum Aquilariae Resinatum raw material, butane or 134a equal solvent, through soaking, stirring, heating, extract under an increased pressure, extraction times 1-3 time, each extraction time 10-200 minute, then, solvent pump 20 is utilized to be extracted in concentration tank 21 by the extract in extractor 19, solvent is made to gasify through decompression, realize quintessence oil to separate with solvent, the solvent of gasification utilizes compressor 22 to compress and liquefy, concentrated tank 21, heat-exchanger rig condensing cooling in extractor 19, it is recovered in solvent non-conservation tank 18,Gas-solvent in extractor 19 under pressure, is fed directly to compressor 22 and is compressed into liquid, then concentrated tank 21, heat-exchanger rig condensing cooling, be recovered in solvent non-conservation tank 18 recycle; When the pressure in extractor 19 is 0MPa, utilize vacuum pump 23 to be extracted out by internal gas, then deliver to compressor liquefaction, through concentration tank 21, heat-exchanger rig condensing cooling, returning in solvent non-conservation tank 18 and recycle, in concentration tank 21, non-vaporized liquid is agilawood essential oil, exports 7 discharges from quintessence oil.
Further, in extraction, the temperature of heating is 30-60 DEG C, and extracting pressure is 0.3-1.6Mpa; Thickening temperature 35��70 DEG C, operating pressure 1.6��-0.08MPa.
Further, extractor 19 precipitation, concentration tank 21 heat source are to utilize compressor 22 aerofluxus, gas compression liquefaction liberated heat.
Embodiment
(1) thin slice that Lignum Aquilariae Resinatum wooden plane becomes 0.25��0.3mm adds extractor from charging aperture 15;
(2) close the valve on charging aperture 15 and all pipelines of extractor 19, utilize vacuum pump 23 to extractor 19 evacuation;
(3) adopt with propane or butane or 134a for solvent from solvent non-conservation tank 18 by material with weight of solvent than the ratio for 1:3, start solvent pump 20, solvent through solvent outlet 1, addition solvent in the solvent inlet 14 incense drug material powder in extractor 19;
(4) heating jacket arranged to extractor 19 bottom side passes into steam heating, and heating, to 40 DEG C, is soaked 30 minutes, utilized agitating device to be stirred during immersion;
(5) above-mentioned (2)-(4) step 1-3 time is repeated;
(6) start solvent pump 20, open the tapping valve 4a connected on leakage fluid dram 4 and the extract liquid feed valve 13a arranged in concentration tank 21 extract import 13, extract is injected in concentration tank 21;
(7) extract in concentration tank 21 is reduced pressure, solvent gasification in extract, solvent after gasification air bleeding valve 12a on air vent 12 enters compressor 22, solvent gas is compressed into liquid, liquid flux flows to from concentration tank 21 hot solvent import 8, exporting 6 through concentration tank 21 from liquid flux, enter extractor 19 heat-exchanger rig from regenerated solvent entrance 5, export 2 from the regenerated solvent heat-exchanger rig and deliver to refluxing opening 17, the solvent of post liquefaction returns in solvent non-conservation tank 18;
(8) after in concentration tank 21, pressure reduces to 0Mpa, closing presure gas trap 11, open air valve 9, start vacuum pump 23, solvent gas through vacuum pump 23, deliver to compressor 22 and liquefy, concentrated tank 21 hot solvent import 8 enters concentration tank 21, same as described above, the solvent of post liquefaction is delivered to extractor 19 from concentration tank 21 liquid flux outlet 6 and is entered extractor 19 heat-exchanger rig from regenerated solvent entrance 5, exporting 2 from the regenerated solvent heat-exchanger rig and deliver to refluxing opening 17, the solvent of post liquefaction returns in solvent non-conservation tank 18; So in concentration tank 21, temperature of liquid reaches 45 DEG C, and pressure reaches-0.08Mpa, and evaporation terminates, and in tank, liquid is object quintessence oil;
(9) the gas part in drained extractor 19, utilize compressor 22 aerofluxus, the Lignum Aquilariae Resinatum raw material taken in tank 19 is heated carrying out precipitation treatment by gas compression liquefaction liberated heat, the air outlet valve 16a arranged from the gas outlet 16 extractor 19, entering compressor 22 through compressor 22 pressed gas valve 11 to liquefy, same concentrated tank 21 solvent liquid entrance is condensed into liquid after entering concentration tank 21, extractor 19 heat-exchanger rig heat exchange and enters solvent non-conservation tank 18 from refluxing opening 17;
(10) after in extractor 19, pressure reduces to 0Mpa, close compressor 22 pressed gas valve 11, open the air valve 9 between vacuum pump 23 and compressor 22, start vacuum pump 23, solvent gas liquefies to compressor 22 through vacuum pump 23, concentrated tank 21 hot solvent import 8, enter concentration tank 21, again from liquid flux export 6 entrance regenerated solvent entrances 5, after extractor 19 heat-exchanger rig heat exchange, condensed fluid is delivered to refluxing opening 17 from regenerated solvent outlet 2 and is entered solvent tank, until temperature reaches 45 DEG C in extractor 19, pressure reaches-0.08Mpa precipitation termination;
(11) the Lignum Aquilariae Resinatum material through extracting is got rid of from extractor 19 discharge gate 3.
Set is added by arranging agitating device in extractor, arranging heating bottom extractor 19, under stress can carry out extracting quintessence oil to Lignum Aquilariae Resinatum heating material, stirring, can the solvent in solvent non-conservation tank 18 be joined in extractor 19 by arranging solvent pump 20, solvent pump 20 can also be utilized to extract extract and to deliver to concentration tank 21, through decompression in concentration tank, being gasified by solvent, through the solvent of gasification, available compressor 22 makes solvent liquefaction, solvent through liquefaction, through concentration tank 21 and heat-exchanger rig, further condensing cooling liquefies completely, may return to solvent non-conservation tank 18 recycles, by utilizing compressor 22 aerofluxus, gas compression liquefaction liberated heat is as extractor 19, concentration tank 21 heat source, thermal source can be made full use of, reduce heating-up temperature, reduce energy consumption, save the energy, by soaking under an increased pressure, stirring Lignum Aquilariae Resinatum material, the yield of quintessence oil can be improved, by utilizing pressure reducing mode that solvent gasification can be made to separate with quintessence oil, by utilizing compressor 22 to compress the solvent after gasification, the solvent after gasification can be made again to become liquid through cooling heat transferring, return in solvent non-conservation tank 18, be conducive to recycling, this complete set of equipments can reduce the equipment pressure of agilawood essential oil, reduce energy consumption, ensure to extract the quality of quintessence oil, improve the use value of quintessence oil.
Claims (8)
1. an energy-saving agilawood essential oil extracts complete set of equipments, including compressor, vacuum pump and solvent pump, it is characterized in that: described complete set of equipments arranges the solvent non-conservation tank of oriented extractor supply solvent, solvent non-conservation tank solvent outlet is connected with extractor solvent inlet, extractor includes agitating device, heat-exchanger rig, heating jacket, extractor is provided with leakage fluid dram, leakage fluid dram is connected to concentration tank extract import, the air vent that after being provided with decompression on concentration tank, solvent gasifies, air vent and vacuum pump, compressor connects, the concentrated tank of hot solvent pipeline carrying out compressor is connected to extractor heat-exchanger rig, extractor heat-exchanger rig is connected with solvent non-conservation tank refluxing opening, compressor heat solvent pipe is additionally coupled to heating jacket.
2. the energy-saving agilawood essential oil of one according to claim 1 extracts complete set of equipments, it is characterised in that: it is connected to solvent pump between solvent non-conservation tank solvent outlet and extractor solvent inlet.
3. the energy-saving agilawood essential oil of one according to claim 1 extracts complete set of equipments, it is characterised in that: described solvent non-conservation tank refluxing opening is arranged on solvent non-conservation tank top, and solvent outlet is arranged on bottom solvent non-conservation tank.
4. the energy-saving agilawood essential oil of one according to claim 1 extracts complete set of equipments, it is characterized in that: the top of described extractor is provided with charging aperture, solvent inlet, gas outlet, bottom is provided with heating jacket, leakage fluid dram, discharge gate, described gas outlet are connected with between vacuum pump, compressor respectively through extraction valve, pressed gas valve.
5. the energy-saving agilawood essential oil of one according to claim 1 extracts complete set of equipments, it is characterized in that: the top of described concentration tank is provided with extract import, air vent, air vent is provided with air bleeding valve, periphery is provided with hot solvent import and liquid flux outlet, bottom is provided with quintessence oil outlet, hot solvent import is connected to compressor, and liquid flux outlet is connected with the heat-exchanger rig in extractor, solvent non-conservation tank refluxing opening in turn.
6. an agilawood essential oil low-temperature extraction technique, complete set of equipments is extracted including the energy-saving agilawood essential oil described in any one in claim 1-5, it is characterized in that: described agilawood essential oil extraction process is, the thin slice that Lignum Aquilariae Resinatum wooden plane becomes 0.25��0.3mm adds extractor, according to material, solvent ratios is that the ratio of 1:1 ~ 3 adds propane or butane or 134a solvent in Lignum Aquilariae Resinatum raw material, through soaking, stirring, heating, extract under an increased pressure, extraction times 1-3 time, each extraction time 10-200 minute, then, solvent pump is utilized to be extracted in concentration tank by the extract in extractor, solvent is made to gasify through decompression, realize quintessence oil to separate with solvent, the solvent of gasification utilizes compressor compresses to liquefy, concentrated tank, heat-exchanger rig in extractor imparts heat to concentration tank, the material of heating is needed in extractor, the solvent simultaneously liquefied is cooled down, it is recovered in turnover solvent tank, gas-solvent in extractor under pressure, is fed directly to compressor compresses and becomes liquid, then concentrated tank, heat-exchanger rig condensing cooling, be recovered in solvent non-conservation tank recycle, when the pressure in extractor is 0MPa, utilize vacuum pump to be extracted out by internal gas, then deliver to compressor liquefaction, through concentration tank, heat-exchanger rig condensing cooling, returning in solvent non-conservation tank and recycle, in concentration tank, non-vaporized liquid is agilawood essential oil, discharges from quintessence oil outlet.
7. a kind of agilawood essential oil low-temperature extraction technique according to claim 6, it is characterised in that: in extraction, the temperature of heating is 30-60 DEG C, and extracting pressure is 0.3-1.6MPa; Thickening temperature 35��70 DEG C, operating pressure 1.6��-0.08MPa.
8. a kind of agilawood essential oil low-temperature extraction technique according to claim 6, it is characterised in that: in extractor, the heat source in precipitation, concentration tank is to utilize compressor air-discharging, gas compression liquefaction liberated heat.
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| CN106635422A (en) * | 2016-12-13 | 2017-05-10 | 郑存义 | Flowering plant essential oil vacuum extraction process and device |
| CN108179067A (en) * | 2018-01-18 | 2018-06-19 | 谢向东 | A kind of raising agilawood essential oil oil yield automatic separation equipment and its process |
| CN109248467A (en) * | 2018-10-30 | 2019-01-22 | 安阳晶森生物科技有限公司 | A kind of technique extracting total-tanshinone from Radix Salviae Miltiorrhizae |
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| CN112358913A (en) * | 2020-10-27 | 2021-02-12 | 广西民族大学 | Method and device for processing liquidized gas through liquid precipitation and separation |
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