CN112745986B - Method and device for extracting essential oil by steam distillation - Google Patents
Method and device for extracting essential oil by steam distillation Download PDFInfo
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- CN112745986B CN112745986B CN202011478882.4A CN202011478882A CN112745986B CN 112745986 B CN112745986 B CN 112745986B CN 202011478882 A CN202011478882 A CN 202011478882A CN 112745986 B CN112745986 B CN 112745986B
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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
- C11B9/027—Recovery of volatiles by distillation or stripping
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- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
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Abstract
The utility model belongs to the technical field of essential oil preparation, and discloses a method and a device for extracting essential oil by steam distillation. The device comprises a distillation kettle, a deoiling tower, an oil-water separator, a heat exchanger and a heater, wherein a gas outlet at the top of the distillation kettle is connected with the lower part of the deoiling tower, the bottom of the deoiling tower is connected with the heat exchanger, the heat exchanger is connected with the oil-water separator, a water layer water gap of the oil-water separator is connected with the heat exchanger, the heat exchanger is connected with the heater, and the heater is connected with the top of the deoiling tower. The oil-containing vapor enters from the lower part of the deoiling tower, and fully contacts with the aqueous layer solution for adsorption and absorption in the ascending process, so that the removal effect of essential oil is improved. The energy consumption is reduced, and the water consumption is reduced.
Description
Technical Field
The utility model belongs to the technical field of essential oil preparation, and particularly relates to a method and a device for extracting essential oil by steam distillation.
Background
The disclosure of this background section is only intended to increase the understanding of the general background of the utility model and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art already known to those of ordinary skill in the art.
The essential oil is volatile aromatic substance extracted from flower, leaf, stem, root or fruit of plant by steam distillation, extrusion, cold soaking or solvent extraction.
Steam distillation techniques are commonly used for extraction of essential oils and are also commonly used in the chemical industry as a mixture separation technique. Steam distillation is commonly used in the following various special cases: (1) essential oil is extracted from plant leaves and stems, and volatile oil and natural medicine are extracted from Chinese medicinal materials. (2) Benzene compounds are recovered in the coal tar and petroleum industries. (3) Steam distillation is combined with solvent extraction (or solid phase adsorption) to measure the amount of material. (4) Deodorization and acidity reduction of fatty acids, edible oils and polyesters (high boiling substances). (5) A small amount of volatile impurity components are separated from the bulk organics. (6) Recovering the high boiling point material. (7) Distilled materials are unstable in their boiling point range or react with other components.
The steam distillation device mainly comprises a distillation kettle, a condenser, an oil-water separator, and a pipeline and a valve which are connected between the distillation kettle, the condenser and the oil-water separator. The separation principle is as follows: when water is present with a compound that is not (or is not) soluble in water, the vapor pressure of the entire system should be the sum of the vapor pressures of the components according to Dalton's partial pressure law.
The steam distillation has the advantages of simple equipment, easy operation, large treatment capacity and the like. However, the traditional steam distillation method has the disadvantages of large solid-to-liquid ratio, long distillation time and high energy consumption, and is easy to separate out oil-soluble essential oil and water-soluble essential oil because the oil-soluble essential oil and the water-soluble essential oil are not mutually dissolved, so that the extraction efficiency is low. The traditional steam distillation method is difficult to severely emulsify condensate distilled from certain essential oil, oil-water separation is difficult, the condensate is required to be kept stand for 2-3 days for oil-water separation, and sometimes, the condensate is required to be refrigerated and then is centrifugally separated by a high-speed centrifugal machine or a water layer after oil-water separation is re-distilled, and certain thermosensitive components in the essential oil are decomposed due to long-time heating extraction, so that the quality of the essential oil is adversely affected.
There are many applications of steam distillation improvement technology in industry, and related literature and patent reports are available. As proposed in the patent of the utility model of the circulating steam distillation apparatus (application number: 201220420855.6), the prior art has the following disadvantages: water is added into a distillation kettle in the system continuously to supplement water consumption, so that the continuous distillation is affected, and the operation time is prolonged; a large amount of steam condensate water is generated in the distillation process, and organic waste water is formed due to organic matters; the water temperature of the steam condensate water can still be close to 100 ℃, and the steam condensate water contains more heat and cannot be recovered, so that the energy consumption is increased.
Disclosure of Invention
In view of the above problems in the prior art, it is an object of the present utility model to provide a method and apparatus for extracting essential oils by steam distillation.
In order to solve the technical problems, the technical scheme of the utility model is as follows:
in a first aspect, a device for extracting essential oil by steam distillation comprises a distillation kettle, a deoiling tower, an oil-water separator, a heat exchanger and a heater, wherein a gas outlet at the top of the distillation kettle is connected with the lower part of the deoiling tower, the bottom of the deoiling tower is connected with the heat exchanger, the heat exchanger is connected with the oil-water separator, a water layer outlet of the oil-water separator is connected with the heat exchanger, the heat exchanger is connected with the heater, and the heater is connected with the top of the deoiling tower.
The water layer of the oil-water separator contains a small amount of essential oil, after being heated by the heat exchanger and the heater, the temperature is increased, and the essential oil enters the deoiling tower to adsorb the essential oil in the oil-containing vapor, thereby being beneficial to separating the essential oil in the oil-containing vapor.
The oil-containing vapor enters from the lower part of the deoiling tower, and fully contacts with the aqueous layer solution for adsorption and absorption in the ascending process, so that the removal effect of essential oil is improved.
In some embodiments of the utility model, the top of the deoiling column is connected to a still. The steam obtained from the top of the deoiling tower returns to the distillation still, the temperature of the steam is higher, and the steam can be repeatedly used for extracting plant essential oil after returning to the distillation still.
In some embodiments of the utility model, the oil-water separator is connected to the heat exchanger by a circulation pump.
In some embodiments of the utility model, the still pot is connected to the deoiling column by a steam exhaust fan.
In a second aspect, a method for extracting essential oil by steam distillation comprises the following specific steps:
placing plants in a distillation kettle, introducing water vapor into the distillation kettle to obtain oil-containing water vapor, and discharging the oil-containing water vapor from the distillation kettle into a deoiling tower;
the oil-containing water vapor is absorbed in the deoiling tower to obtain an oil-containing solution and water vapor, the water vapor is discharged from the top of the deoiling tower, the oil-containing solution is discharged from the bottom of the deoiling tower and enters an oil-water separator, and the oil-containing solution and the water layer solution are separated;
the aqueous layer solution enters the deoiling tower after being heated for adsorption deoiling of the oil-containing water vapor.
And (3) introducing the aqueous layer solution obtained in the oil-water separator into a deoiling tower to separate essential oil from the oil-containing water vapor. Separating essential oil and water vapor in the water vapor, dissolving the essential oil into the water layer solution, and discharging the water vapor from the top of the deoiling tower. This achieves reuse of the aqueous layer solution.
The temperature of the water layer solution is lower when the water layer solution is discharged from the oil-water separator, and the temperature of the water layer solution is increased through heat exchange and heating, so that the effect of the water layer solution on adsorbing essential oil is improved after the water layer solution reaches a higher temperature.
The method for removing essential oil by the oil-containing steam in the prior art comprises the following steps: condensing the water vapor containing oil, and separating to obtain essential oil. However, the stationary separation requires a long time, and the separation is not complete, and re-centrifugal separation or re-distillation is required. And the water layer obtained by standing separation, if the water layer is used for extracting essential oil, the water layer needs to be heated again to be water vapor, so that the energy consumption is increased. Therefore, the method does not need the operation step of condensing the oil-containing vapor, and realizes the function of energy conservation.
In some embodiments of the utility model, a packing is disposed in the deoiling tower, and the packing is stainless steel theta mesh ring packing.
Further, the height of the filler section is 1-1.5 m, the top of the filler section is 0.1-0.3 m away from the top of the deoiling tower, and the bottom of the filler section is 0.6-1.0 m away from the bottom of the deoiling tower.
The deoiling tower is filled with stuffing, and the oil-containing steam enters the deoiling tower to separate essential oil through adsorption. The oil-containing water vapor contains oil-soluble essential oil and water-soluble essential oil, and the oil-soluble essential oil is insoluble with water, so that the oil-soluble essential oil is easy to separate, is dissolved in the water layer solution in the process of contacting the water layer solution, and is discharged from the bottom of the deoiling tower.
The essential oil is removed by utilizing the principle of gas absorption in the deoiling tower.
In some embodiments of the utility model, the temperature within the still pot is 60-100 ℃.
After the essential oil is removed from the deoiling tower by the oil-containing vapor obtained from the distilling still, the temperature of the obtained essential oil solution is still higher, the obtained water layer solution exchanges heat with the essential oil solution in a heat exchanger after passing through the oil-water separator, the temperature of the water layer solution is increased, and then the water layer solution is heated by a heater and is further increased to 95-105 ℃ so as to keep the circulation quantity of the vapor.
In some embodiments of the utility model, the heater is connected to the deoiling column or to both the deoiling column and the still.
In some embodiments of the utility model, the distillation still is under vacuum or atmospheric conditions.
In some embodiments of the utility model, the aqueous layer contains 0.5 to 8 percent (mass percent) of sodium chloride or sodium sulfate in the oil-water separator. The water layer in the oil-water separator contains sodium chloride or sodium sulfate, so that the oil-water separation effect is good, the water layer is circularly used for removing essential oil in water vapor, the emission of organic wastewater is reduced, and the environment protection is facilitated.
In some embodiments of the utility model, the temperature of the aqueous layer solution after being heated in the heater is 95-105 ℃. Aqueous solutions at temperatures in this range have better absorption of essential oils from oily water vapor. Meanwhile, in order to maintain the amount of steam circulated back into the still, heating to the above temperature range is required. Or after the aqueous layer solution is heated and gasified, a part of the steam is introduced into the distillation still, and the amount of the steam in the distillation still is maintained.
One or more of the technical schemes of the utility model has the following beneficial effects:
the water vapor obtained in the deoiling tower is discharged from the top of the deoiling tower and returned to the distillation kettle for recycling, so that the distilled water consumption is saved, and the energy is saved.
The water layer solution is utilized in the deoiling tower, and the gas adsorption principle is utilized, so that the essential oil is fully removed.
The speed of the water vapor can be controlled by the vapor exhaust fan, and when the controlled circulation speed is higher, the efficiency is greatly improved. The circulation speed is increased, and basically only the power consumption of the exhaust fan is increased, and condensation and vaporization steps are not needed, so that only a small amount of electric energy is consumed, and the efficiency is greatly improved.
Drawings
The accompanying drawings, which are included to provide a further understanding of the utility model and are incorporated in and constitute a part of this specification, illustrate embodiments of the utility model and together with the description serve to explain the utility model.
FIG. 1 is a block diagram of an apparatus for extracting essential oils by steam distillation;
wherein, 101-distilling still; 102-a steam valve; 103-a steam exhaust fan; 104-a deoiling tower; 105-heat exchanger; 106-an oil-water separator; 107-overflow pipe; 108-a circulating pump; 109-a heater; 110-a back pressure valve; 111-safety valve.
Detailed Description
It should be noted that the following detailed description is illustrative and is intended to provide further explanation of the utility model. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this utility model belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments in accordance with the present application. As used herein, the singular is also intended to include the plural unless the context clearly indicates otherwise, and furthermore, it is to be understood that the terms "comprises" and/or "comprising" when used in this specification are taken to specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof.
The utility model will be further illustrated by the following examples
The device for extracting essential oil by steam distillation comprises a distillation kettle 101, a deoiling tower 104, an oil-water separator 106, a heat exchanger 105 and a heater 109, wherein a gas outlet of the distillation kettle 101 is connected with the lower part of the deoiling tower 104 through a steam exhaust fan 103, the bottom of the deoiling tower 104 is connected with the heat exchanger 105, the heat exchanger 105 is connected with the oil-water separator 106, a water layer outlet of the oil-water separator 106 is connected with the heat exchanger 105 through a circulating pump 108, the heat exchanger 105 is connected with the heater 109, and the heater 109 is connected with the top of the deoiling tower 104. The top of the deoiling column 104 is connected with the distillation still 101 through a back pressure valve 110. The bottom of the distillation still 101 is provided with a steam valve 102, the upper part of the deoiling tower 104 is provided with a safety valve 111, and the upper part of the oil-water separator 106 is provided with an overflow pipe 107.
The tower height of the deoiling tower 104 is 2.2 meters, the inner diameter is 0.12 meter, the stainless steel theta net ring packing with the diameter and the height of 4mm is filled, the height of the packing section is 1.5 meters, the top of the packing section is 0.1 meter away from the tower top of the deoiling tower 104, and the bottom of the packing section is 0.6 meter away from the tower bottom of the deoiling tower 104; the feed inlet at the lower portion of the deoiling column 104 is 0.1 meter below the lower end of the packed section of the deoiling column 104.
A method for extracting essential oil by steam distillation adopts a process flow shown in figure 1, 10kg of rose with 83.0 percent of water content (mass percent) is filled in a distillation kettle 101 with a volume of 100 liters as a raw material, steam enters the distillation kettle 101 from the bottom of the distillation kettle 101 through a steam valve 102 for steam distillation, and steam containing essential oil is discharged from the top of the distillation kettle 101;
the water vapor containing essential oil enters the deoiling tower 104 from the lower part of the deoiling tower 104 through a steam exhaust fan 103 (a variable frequency high temperature resistant blower) to remove essential oil, is discharged from the top of the deoiling tower 104 in a water vapor form, enters the distillation kettle 101 from the bottom of the distillation kettle 101 through a back pressure valve 110, and is continuously extracted;
the solution containing essential oil in the deoiling tower 104 is discharged from the bottom of the deoiling tower 104, enters a heat exchanger 105 for cooling, then enters an oil-water separator 106, and the essential oil layer is led out through an overflow pipe 107 to obtain essential oil, and is dried by anhydrous sodium sulfate with the mass of 50 percent of the essential oil and then is stored;
the circulating pump 108 adopts YT600-1J type industrial peristaltic pump produced by Langerhans constant flow pump Co., ltd, the water layer in the oil-water separator 106 enters the heater 109 to be gasified partially at a speed of 5 liters/min after passing through the circulating pump 108 and the heat exchanger 105, then enters the deoiling tower 104 from the upper part of the deoiling tower 104 to carry out gas-liquid mass transfer so as to remove essential oil in water vapor, the solution containing the essential oil is discharged from the bottom of the deoiling tower 104, and the water vapor rising along with the deoiling tower 104 in the gas phase part is discharged from the top of the deoiling tower 104 and enters the distillation kettle 101 through the back pressure valve 110;
the steam valve 102 is closed.
The steam discharge rate from the top of the still 101 was controlled to 3.6 cubic meters per hour by adjusting the steam discharge fan 103.
The temperature in the still pot 101 was set to 95℃by adjusting the back pressure valve 110.
The temperature of the water layer solution after being heated in the heater is 100 ℃, and the liquid level of the bottom of the deoiling tower 104 and the oil-water separator 106 is stabilized by controlling the gasification proportion of the water layer in the oil-water separator 106 into the heater 109.
The aqueous layer in the oil-water separator contained 4% by mass of sodium chloride.
The top of the deoiling tower 104 is provided with a safety valve 111.
The device was run for 10 hours to give 4.50g of essential oil, 1.5kg of steam was consumed, and 10.5 degrees of electrical energy was consumed.
The method for extracting the essential oil by steam distillation realizes the recycling of steam, and has obvious energy-saving effect; the circulation rate of steam is controlled by adjusting the steam exhaust fan, so that the efficiency of extracting essential oil is improved; the water layer in the oil-water separator contains sodium chloride, so that the oil-water separation effect is good, the water layer is circularly used for removing essential oil in water vapor, the emission of organic wastewater is reduced, and the environment protection is facilitated.
In this embodiment, a single distillation still is used for extracting essential oil by steam distillation, and a plurality of distillation still in series may be used for extracting essential oil by steam distillation to improve efficiency.
In this embodiment, the aqueous layer solution is heated by the heater and then enters the deoiling tower entirely or enters the distillation still partially through gasification.
Example 2:
the points of the present embodiment that are the same as those of embodiment 1 are not described in detail, and the difference is that:
the height of the filler section in the deoiling tower 104 is 1.4 m, the top of the filler section is 0.2 m away from the top of the deoiling tower 104, and the bottom of the filler section is 0.6 m away from the bottom of the deoiling tower 104.
10kg of spearmint having a water content of 83.5% by mass was charged into a distillation still 101 having a capacity of 100 liters as a raw material.
The temperature of the aqueous layer solution after being heated in the heater was 105 ℃. The temperature in the distillation still 101 was set to 100℃by adjusting the back pressure valve 110.
The aqueous layer in the oil-water separator contained 0.5% by mass of sodium chloride.
The device was run for 11 hours to obtain 51.4g of essential oil, 1.6kg of steam was consumed, and 11.8 degrees of electric energy was consumed.
Example 3:
the points of the present embodiment that are the same as those of embodiment 2 are not described in detail, and the difference is that:
the height of the filler section in the deoiling tower 104 is 1.3 m, the top of the filler section is 0.3 m away from the top of the deoiling tower 104, and the bottom of the filler section is 0.6 m away from the bottom of the deoiling tower 104.
The exhaust fan 103 is a German MZ 2C NT type diaphragm pump manufactured by Vacuubrand corporation of Germany; the steam discharge rate from the top of the still 101 was controlled to 1.8 cubic meters per hour by adjusting the steam discharge fan 103.
The temperature of the aqueous layer solution after being heated in the heater was 95 ℃. The temperature in the distillation still 101 was set to 60℃by adjusting the back pressure valve 110.
The aqueous layer in the oil-water separator contained 8% by mass of sodium chloride.
The device was run for 12 hours to give 58.2g of essential oil, 1.4kg of steam was consumed, and 13.1 degrees of electric energy was consumed.
In the embodiment, the essential oil is extracted by steam distillation under vacuum, so that the yield of the essential oil is improved.
Example 4:
the points of the present embodiment that are the same as those of embodiment 3 are not described in detail, and the difference is that:
the height of the filler section in the deoiling tower 104 is 1.2 m, the top of the filler section is 0.3 m from the top of the deoiling tower 104, and the bottom of the filler section is 0.7 m from the bottom of the deoiling tower 104.
10kg of lavender having a water content of 85.0% by mass was charged into a distillation still 101 having a capacity of 100 liters as a raw material.
The temperature of the aqueous layer solution after being heated in the heater was 96 ℃. The temperature in the still pot 101 was set to 70℃by adjusting the back pressure valve 110.
The aqueous layer in the oil-water separator contained 0.5% by mass of sodium sulfate.
The device was run for 12 hours to give 53.5g of essential oil, 1.5kg of steam was consumed, and 12.4 degrees of electrical energy was consumed.
Example 5:
the points of the present embodiment that are the same as those of embodiment 4 are not described in detail, and the difference is that:
the height of the filler section in the deoiling tower 104 is 1.0 m, the top of the filler section is 0.2 m away from the top of the deoiling tower 104, and the bottom of the filler section is 1.0 m away from the bottom of the deoiling tower 104.
The temperature of the aqueous layer solution after being heated in the heater was 97 ℃. The temperature in the distillation still 101 was set to 80℃by adjusting the back pressure valve 110.
The aqueous layer in the oil-water separator contained 8% by mass of sodium sulfate.
The device was run for 12 hours to obtain 51.8g of essential oil, 1.5kg of steam was consumed, and 12.0 degrees of electric energy was consumed.
The above description is only of the preferred embodiments of the present utility model and is not intended to limit the present utility model, but various modifications and variations can be made to the present utility model by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (8)
1. A device for extracting essential oil by steam distillation, which is characterized in that: the device comprises a distillation kettle, a deoiling tower, an oil-water separator, a heat exchanger and a heater, wherein a gas outlet at the top of the distillation kettle is connected with the lower part of the deoiling tower, the bottom of the deoiling tower is connected with the heat exchanger, the heat exchanger is connected with the oil-water separator, a water layer water gap of the oil-water separator is connected with the heat exchanger, the heat exchanger is connected with the heater, and the heater is connected with the top of the deoiling tower; the top of the deoiling tower is connected with the distillation kettle;
in the oil-water separator, the water layer contains 0.5% -8% of sodium chloride or sodium sulfate;
the temperature of the water layer liquid in the heater after being heated is 95-105 ℃.
2. The apparatus for extracting essential oil by steam distillation as claimed in claim 1, wherein: the oil-water separator is connected with the heat exchanger through a circulating pump.
3. The apparatus for extracting essential oil by steam distillation as claimed in claim 1, wherein: the distillation still is connected with the deoiling tower through a steam exhaust fan.
4. A method for extracting essential oil by steam distillation using the apparatus for extracting essential oil by steam distillation according to any one of claims 1 to 3, characterized in that: the method comprises the following specific steps:
placing plants in a distillation kettle, introducing water vapor into the distillation kettle to obtain oil-containing water vapor, and discharging the oil-containing water vapor from the distillation kettle into a deoiling tower;
the oil-containing water vapor is absorbed in the deoiling tower to obtain an oil-containing solution and water vapor, the water vapor is discharged from the top of the deoiling tower, the oil-containing solution is discharged from the bottom of the deoiling tower and enters an oil-water separator, and the oil-containing solution and the water layer solution are separated;
the aqueous layer solution enters the deoiling tower after being heated for adsorption deoiling of the oil-containing water vapor.
5. The method for extracting essential oil by steam distillation as claimed in claim 4, wherein: the deoiling tower is provided with a filler which is stainless steel theta net ring filler.
6. The method for extracting essential oil by steam distillation as claimed in claim 4, wherein: the height of the filling section is 1-1.5 m, the top of the filling section is 0.1-0.3 m away from the top of the deoiling tower, and the bottom of the filling section is 0.6-1.0 m away from the bottom of the deoiling tower.
7. The method for extracting essential oil by steam distillation as claimed in claim 5, wherein: the temperature in the distillation still is 60-100 ℃.
8. The method for extracting essential oil by steam distillation as claimed in claim 1, wherein: the distillation kettle is under vacuum condition or normal pressure condition.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103058909A (en) * | 2012-12-13 | 2013-04-24 | 中国电器科学研究院有限公司 | Recycling process for N-methyl pyrrolidone |
| CN205957756U (en) * | 2016-06-06 | 2017-02-15 | 克拉玛依金鑫油田环保工程有限公司 | Mixed steam spray cooling tower of profit and mixed steam cooling device of sled dress formula profit |
| CN109207262A (en) * | 2018-10-17 | 2019-01-15 | 武汉轻工大学 | The extraction element and extracting method of volatile plant essence oil |
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| CN201506783U (en) * | 2009-09-28 | 2010-06-16 | 潍坊中业化学有限公司 | Refining castor oil dehydration device |
| CN103466749B (en) * | 2012-06-06 | 2015-11-25 | 陈晗 | A kind of method of oil content in effective elimination aqueous solution |
| CN106433984B (en) * | 2016-10-10 | 2017-08-25 | 罗定市荣兴香料有限公司 | A kind of equipment for extraction of essential oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103058909A (en) * | 2012-12-13 | 2013-04-24 | 中国电器科学研究院有限公司 | Recycling process for N-methyl pyrrolidone |
| CN205957756U (en) * | 2016-06-06 | 2017-02-15 | 克拉玛依金鑫油田环保工程有限公司 | Mixed steam spray cooling tower of profit and mixed steam cooling device of sled dress formula profit |
| CN109207262A (en) * | 2018-10-17 | 2019-01-15 | 武汉轻工大学 | The extraction element and extracting method of volatile plant essence oil |
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