Patent Description:
Various active plant substances, for example, alkaloids, glucosides, volatile oils, resins, lipids, tannins, etc., have been used for pharmaceutical applications. Essential oils and oleoresins are used in a wide variety of consumer goods such as detergents, soaps, toilet products, cosmetics, pharmaceuticals, perfumers, confectionery food products, soft drinks, distilled alcoholic beverages, and insecticides. The production and consumption of essential oils and perfumes worldwide are rapidly growing.

Production technology is essential to the improvement of yield and quality of essential oils. Traditional technologies pertaining to essential oil processing are still widely used in many parts of the world. Water distillation, water and steam distillation, steam distillation, cohobation, maceration and enfleurage are the most commonly used methods. When oil yield from distillation is poor, maceration may be a preferred method. Distillation methods are good for powdered almonds, rose petals and rose blossoms, whereas solvent extraction is suitable for expensive, delicate and thermally unstable materials such as jasmine, tuberose, and hyacinth. In general, water distillation is the most favored method of plant essential oil extraction.

Essential oils can be derived from one or more plant parts, for example, flowers, leaves, stems, bark, wood, roots, seeds, fruits, rhizomes, and gums or oleoresin exudations. However, some plants such as those of Cannabis genus require additional treatments to improve the final yield and composition of the extraction. In addition, it is desirable to increase the yield of essential oils (and in particular, terpenes contained therein) and oleoresins (and in particular, resin alcohols, resin acids and resin phenolics contained therein).

<CIT> relates to the recovery of a solvent, especially a hydrofluorocarbon (HFC) solvent used in the extraction of components from materials of natural origin (biomass).

<CIT> relates to systems for extracting solute from source materials, such as extracting terpenoids, flavonoids, and/or other components from (<NUM>) cannabis, hemp, and/or derivatives thereof and (<NUM>) other botanical substances such as terpene-bearing plants and/or fruits and/or extracting psilocin, baeocystin, and/or norbaeocystin from psilocibe mushrooms and/or derivatives thereof.

<CIT> relates to methods for extracting oils from oil bearing materials.

The present invention and its preferred embodiments are apparent from the appendant set of claims.

In one aspect, this disclosure provides an apparatus (or system) for extracting essential oils and oleoresins from a plant material, comprising a circulation pump, a discharging pump, an extraction module, a reservoir, a first evaporator, and a first condenser. The discharge pump is fluidly connected to the circulation pump. The extraction module includes at least one extraction vessel for receiving the plant material. The at least one extraction vessel has a lower part fluidly connected to the discharge pump and an upper part fluidly connected to the circulation pump. The lower and upper parts are configured with a lower filter and an upper filter, respectively. The reservoir is fluidly connected to the discharge pump, and the reservoir is configured to store a solvent containing a C1 to C4 fluorinated hydrocarbon. The first evaporator is fluidly connected to the circulation pump. The first condenser is fluidly connected to the circulation pump, and to the reservoir. In a short loop circulation mode the discharge pump pumps a solution comprising the solvent and one or more active components of the plant material dissolved therein from the bottom of the at least one extraction vessel, passing through the circulation pump and then back to the top of the at least one extraction vessel. A short loop circulation comprises the discharge pump, the extraction module and the circulation pump without the first evaporator, the reservoir and the first condenser and a long loop circulation comprises the discharge pump, the extraction module, the circulation pump, the first evaporator, the reservoir and the first condenser.

According to certain embodiments of this disclosure, in a long loop circulation mode the discharge pump pumps the solution comprising the solvent and one or more active components of the plant material dissolved therein from the bottom of the at least one extraction vessel, passing through the circulation pump, and then fed into the first evaporator where the solvent is gasified, and the circulation pump pumps the gasified solvent to the first condenser. In one embodiment, the apparatus (or system) further comprises a vapor pump for facilitating vaporization of the solvent. The vapor pump is fluidly connected to the top of the at least one extraction vessel, to the circulation pump, and to the first condenser.

According to certain embodiments of this disclosure, the first evaporator and the first condenser are fluidly connected via a heat pump.

An apparatus (or system) of this disclosure may further comprise a vapor pump for facilitating vaporization of the solvent. The vapor pump is fluidly connected to the top of the at least one extraction vessel, to the circulation pump, and to the first condenser.

According to certain embodiments of this disclosure, the apparatus (or system) further comprises a second condenser fluidly connected to the vapor pump and to the reservoir. In one embodiment of this disclosure, in a long loop circulation mode the vapor pump pumps a vapor of the solvent from the top of the at least one extraction vessel to the second condenser.

In some other embodiments, the apparatus (or system) further comprises a second evaporator fluidly connected to the first evaporator. According to one embodiment of this disclosure, the first evaporator is configured to work at a temperature lower than that of the second evaporator, and the first evaporator is configured to work at a pressure lower than that of the second evaporator. In addition, the second evaporator may be fluidly connected to the reservoir.

According to certain embodiments of this disclosure, the first evaporator and the first condenser are fluidly connected via a heat pump. In some other embodiments, the second evaporator and the first condenser are fluidly connected via the heat pump. According to one embodiment of this disclosure, in a long loop circulation mode the discharge pump pumps a solution comprising the solvent and one or more active components of the plant material dissolved therein from the bottom of the at least one extraction vessel, passing through the circulation pump, and then fed into the first and second evaporators where the solvent is gasified, and the heat pump liquefies the gasified solvent and send the liquefied solvent into the first condenser.

According to certain embodiments of this disclosure, the short loop circulation mode is performed at a flow rate of <NUM> to <NUM>/min (in and out of the at least one extraction vessel). Further, the short loop circulation mode may be performed for about <NUM> minutes at about <NUM> or for about <NUM> minutes at about <NUM>.

In another aspect, this disclosure provides an apparatus (or system) for extracting essential oils and oleoresins from a plant material, comprising a circulation pump, a discharging pump, an extraction pump, a reservoir, a first evaporator, a second evaporator, a first condenser, a second condenser, and a vapor pump. The discharge pump fluidly is connected to the circulation pump. The extraction module includes a first extraction vessel and a second extraction vessel, the first extraction vessel has a first lower part fluidly connected to the discharge pump and a first upper part fluidly connected to the circulation pump, and the second extraction vessel has a second lower part fluidly connected to the discharge pump and a second upper part fluidly connected to the circulation pump. The reservoir is fluidly connected to the discharge pump, and the reservoir is configured to store a solvent containing a C1 to C4 fluorinated hydrocarbon. The first evaporator is fluidly connected to the circulation pump. The second evaporator is fluidly connected to the first evaporator. The first condenser is fluidly connected to the circulation pump, and to the reservoir. The second condenser is fluidly connected to the reservoir. The vapor pump is configured for facilitating vaporization of the solvent, and the vapor pump is fluidly connected to the first upper part of the first extraction vessel, to the second upper part of the second extraction vessel, to the circulation pump, to the first condenser, and to the second condenser.

According to certain embodiments of this disclosure, the first lower part and first upper part are configured with a lower filter and an upper filter, respectively.

According to certain embodiments of this disclosure, the second lower part and second upper part are configured with a lower filter and an upper filter, respectively.

According to certain embodiments of this disclosure, the first evaporator is configured to work at a temperature lower than that of the second evaporator, and the first evaporator is configured to work at a pressure lower than that of the second evaporator.

According to certain embodiments of this disclosure, the first evaporator and the first condenser are fluidly connected via a heat pump. In some other embodiments, the second evaporator and the first condenser are fluidly connected via the heat pump. According to one embodiment of this disclosure, the vapor pump pumps a vapor of the solvent from the top of the first extraction vessel to the second condenser; and the discharge pump pumps a solution comprising the solvent and one or more active components of the plant material dissolved therein from the bottom of the second extraction vessel, passing through the circulation pump, and then fed into the first and second evaporators where the solvent is gasified, and the heat pump liquefied the gasified solvent and send the liquefied solvent into the first condenser.

In still another aspect, this disclosure features a method for extracting essential oils and oleoresins from a plant material using an apparatus (or system) of this disclosure.

Providing an apparatus comprising a circulation pump; a discharge pump fluidly connected to the circulation pump; an extraction module including at least one extraction vessel for receiving the plant material, the at least one extraction vessel having a lower part fluidly connected to the discharge pump and an upper part fluidly connected to the circulation pump, wherein the lower and upper parts are configured with a lower filter and an upper filter, respectively; a reservoir fluidly connected to the discharge pump, the reservoir being storing a solvent containing a C1 to C4 fluorinated hydrocarbon; a first evaporator fluidly connected to the circulation pump; and a first condenser fluidly connected to the circulation pump, and to the reservoir, the method comprises: extracting one or more active components from a plant material placed in the at least one extraction vessel through a short loop circulation, wherein in the short loop circulation the discharge pump pumps a solution comprising the solvent and one or more active components of the plant material dissolved therein from the bottom of the at least one extraction vessel, passing through the circulation pump, and then back to the top of the at least one extraction vessel; and extracting the plant material remained in the at least one extraction vessel through a long loop circulation, wherein in the long loop circulation the discharge pump pumps a solution comprising the solvent and one or more active components of the plant material dissolved therein from the bottom of the at least one extraction vessel, passing through the discharging pump and then through the circulation pump, and then fed into the first evaporator where the solvent is gasified, and the circulation pump pumps the gasified solvent to the first condenser.

The foregoing summary, as well as the following detailed description of the invention, will be better understood when read in conjunction with the appended drawing. In the drawings:.

Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by a person skilled in the art to which this invention belongs.

As used herein, the singular forms "a", "an", and "the" include plural referents unless the context clearly dictates otherwise. Thus, for example, reference to "a sample" includes a plurality of such samples and equivalents thereof known to those skilled in the art.

The term "about" as used herein when referring to a measurable value such as a temperature, an amount, a temporal duration, and the like, is meant to encompass variations of and from the specified value, in particular variations of +/-<NUM>% or less, preferably +/-<NUM>% or less, more preferably +/-<NUM>% or less, and still more preferably +/-<NUM>% or less of and from the specified value, insofar such variations are appropriate to perform in the disclosed invention. It is to be understood that the value to which the modifier "about" refers is itself also specifically, and preferably, disclosed.

Referring to <FIG>, <FIG> and <FIG>, there is shown an apparatus <NUM> for extracting essential oils and oleoresins from a plant material. The apparatus <NUM> comprises a circulation pump <NUM>, a discharge pump <NUM>, an extraction module <NUM>, a reservoir <NUM>, first evaporator <NUM>, and a first condenser <NUM>.

As shown in <FIG>, <FIG> and <FIG>, the discharge pump <NUM> is fluidly connected to the circulation pump <NUM>. The extraction module <NUM> includes at least one extraction vessel <NUM> for receiving the plant material. The reservoir <NUM> is fluidly connected to the discharge pump <NUM>. The first evaporator <NUM> is fluidly connected to the circulation pump <NUM>. The first condenser <NUM> is fluidly connected to the circulation pump <NUM>, and to the reservoir <NUM>. The vapor pump <NUM> is provided for facilitating vaporization of solvent, and the vapor pump <NUM> is fluidly connected to the top of the at least one extraction vessel <NUM>, to the circulation pump <NUM>, and to the first condenser <NUM>. The at least one extraction vessel <NUM> has a lower part <NUM> and an upper part <NUM>. The lower part <NUM> is fluidly connected to the discharge pump <NUM>, and the upper part <NUM> is fluidly connected to the circulation pump <NUM>. The lower and upper parts <NUM>, <NUM> are configured with a lower filter <NUM> and an upper filter <NUM>, respectively. The reservoir <NUM> is configured to store a solvent containing one or more C1 to C4 fluorinated hydrocarbon. For example, the C1 to C4 fluorinated hydrocarbon can be, but not limited to <NUM>,<NUM>,<NUM>,<NUM>-tetrafluoroethane.

As shown in <FIG>, in a short loop circulation S the discharge pump <NUM> pumps a solution comprising the solvent and one or more active components of the plant material dissolved therein from the bottom of the at least one extraction vessel <NUM>, passing through the circulation pump <NUM>, and then back to the top of the at least one extraction vessel <NUM>.

As shown in <FIG>, in a long loop circulation L the discharge pump <NUM> pumps the solution comprising the solvent and one or more active components of the plant material dissolved therein from the bottom of the at least one extraction vessel <NUM>, passing first through the discharge pump <NUM> and then through circulation pump <NUM>, and then fed into the first evaporator <NUM> where the solvent is gasified, and the circulation pump <NUM> pumps the gasified solvent to the first condenser <NUM>. This is called batch extraction loop.

As shown in <FIG>, in another long loop circulation L the discharge pump <NUM> pumps a solution comprising the solvent and one or more active components of the plant material dissolved therein from the top of the at least one extraction vessel <NUM>, passing through the circulation pump <NUM>, and then fed into the first evaporator <NUM> where the solvent is gasified, and the circulation pump <NUM> pumps the gasified solvent to the first condenser <NUM>. This is called continues extraction loop.

The reservoir <NUM> is configured to store a liquid solvent and may be cooled externally via a cooler (or a cooling pipe) <NUM>. The at least one extraction vessel <NUM> is wrapped in a jacket <NUM> which may be cooled by a cooler <NUM> and/or heated by a heater <NUM> externally.

The circulation pump <NUM> is a complex system of filers, pipes and valves allowing the solvent and miscella current to change and interconnect between the attached vessels. There is a gas and liquid piping distribution systems that are usually phase separated. A gas or a vapor pump <NUM> helps the gaseous phase to evacuate faster from the extraction module <NUM> and a liquid pump part of the circulation pump <NUM> assembly helps the liquid phase to recirculate in the extraction module <NUM> or feed to the filter or evaporation system. A filter is installed before the pump to filter particles and after the pump to filter particles in the miscella flow. In general, the circulation pump <NUM> comprises one or more pipes, one or more pumps and/or one or more valves connecting the first condenser <NUM>, the first evaporator <NUM>, the at least one extraction vessel <NUM>, and the discharge pump <NUM>.

The discharge pump <NUM> is a complex assembly of pipes, filters and pumps in order to provide the in and out flow of the liquid phase of solvent and miscella in the extraction module <NUM>. The filter is placed before the pump in order to filter particles in the miscella flow. The discharge pump <NUM> comprises one or more pipes, one or more pumps and/or one or more valves connecting the reservoir <NUM>, the at least one extraction vessel <NUM>, and the circulation pump <NUM>.

The vapor pump <NUM> is a complex system of filters, pipes and pumps that manages the vapor recovery process. The vapor pump <NUM> is connected to the vapor distribution system of the circulation pump <NUM> and produces the required pressure to increase the vapor condensation and liquefaction required for the vapors to condense in the condenser <NUM>. The vapor pump <NUM> comprises one or more pipes, one or more pumps and/or one or more valves connecting the first condenser <NUM>, the reservoir <NUM>, the at least one extraction vessel <NUM>, and the circulation pump <NUM>. The first evaporator <NUM> and the first condenser <NUM> are connected via a heat pump <NUM>. A collection vessel <NUM> is connected to the first evaporator <NUM>.

The plant material is loaded into the at least one extraction vessel <NUM> and soaked in the (liquid) solvent containing one or more C1 to C4 fluorinated hydrocarbon fed from the reservoir <NUM> via the discharge pump <NUM> and forced into the plant material using a pump until the solvent reaches the top of the at least one extraction vessel <NUM> and all the gas phase has been evacuated. The jacket <NUM> may be externally or internally heated or chilled to the point for achieving an appropriate pressure in the at least one extraction vessel <NUM> under a pre-determined temperature to extract desired active ingredients from the plant material.

The apparatus <NUM> may operate under at least three <NUM> modes: a soaking mode, a short loop circulation mode, and a long loop circulation mode.

In soaking mode, the at least one extraction vessel <NUM> stays loaded with the solvent and the plant material soaked in the solvent for as long as the processing time under the processing pressure. After such time the solvent and the constituent mixture called miscella are sent to the first evaporator <NUM> via the discharge pump <NUM> connected to the circulation pump <NUM> (starting the long loop circulation mode).

In long loop circulation mode, the circulation pump <NUM> allows the overflow solvent to pass to the first evaporator <NUM> where excess vapors are passed from the first evaporator <NUM> to the first condenser <NUM> via the circulation pump <NUM>. The vaporization may be additionally increased by the vapor pump <NUM>. At the same time, a fresh solvent is fed to the at least one extraction vessel <NUM> via the discharge pump <NUM> which can be either gravity fed or induced by a liquid pump.

In short loop circulation mode, the circulation pump <NUM> and the discharge pump <NUM> are fluidly connected to ensure that there is a steady recirculation without the presence of a gas phase for a pre-determined period of time. When the time is up, the discharge pump <NUM> via the help of a pump and via the circulation pump <NUM> drains the solvent mixture into the first evaporator <NUM>. At the same time, the first evaporator <NUM>, having a temperature higher than that of the at least one extraction vessel <NUM>, gasifies the solvent and sends the vapors via the circulation pump <NUM> to the first condenser <NUM> for liquefaction.

The short loop circulation mode is preferably performed at a flow rate of <NUM> to <NUM>/min (in and out of the at least one extraction vessel <NUM>). Further, the short loop circulation mode may be performed for about <NUM> minutes at about <NUM> or for about <NUM> minutes at about <NUM>.

After all vapors from the first evaporator <NUM> liquefied in the first condenser <NUM> are fed to the reservoir <NUM> where they are kept liquid at a temperature lower than ambient temperature. After all solvent is vaporized from the extract and the extract is completely separated from solvent in the first evaporator <NUM>, the extract is fed to the collection vessel <NUM>. The process of gasification of the solvent in the first evaporator <NUM> requires heat and the process for liquefaction in the first condenser <NUM> requires coldness, which are provided by both ends of the heat pump <NUM>, respectively.

After the liquid solvent is evacuated from the at least one extraction vessel <NUM>, the at least one extraction vessel <NUM> is heated and the solvent residue is forced into fast evaporation. The vapors from the at least one extraction vessel <NUM> are fed to the first condenser <NUM> via the vapor pump <NUM>. The vapor pump <NUM> comprises a set of gas pumps which speed up the process of evaporation by maintaining a low pressure in the at least one extraction vessel <NUM>. The vapors from the at least one extraction vessel <NUM> liquefied in the first condenser <NUM> are fed to the reservoir <NUM> where they are kept liquid at a temperature lower than ambient temperature. The reservoir <NUM> is externally cooled to maintain the solvent in liquid phase.

Referring to <FIG>, there is shown an apparatus <NUM> for extracting essential oils and oleoresins from a plant material. The apparatus <NUM> comprises a circulation pump <NUM>, a discharge pump <NUM>, an extraction module <NUM>, a reservoir <NUM>, a first evaporator <NUM>, first condenser <NUM>, vapor pump <NUM>, and a second condenser <NUM>.

The is discharge pump <NUM> fluidly connected to the circulation pump <NUM>. The extraction module <NUM> includes at least one extraction vessel <NUM> for receiving the plant material. The reservoir <NUM> is fluidly connected to the discharge pump <NUM>. The first evaporator <NUM> is fluidly connected to the circulation pump <NUM>. The first condenser <NUM> is fluidly connected to the circulation pump <NUM>, and to the reservoir <NUM>. The a vapor pump <NUM> is provided for facilitating vaporization of solvent, and the vapor pump <NUM> is fluidly connected to the top of the at least one extraction vessel <NUM>, to the circulation pump <NUM>, and to the first condenser <NUM>. The second condenser <NUM> is disposed between and fluidly connected to the vapor pump <NUM> and the reservoir <NUM>. The at least one extraction vessel <NUM> has a lower part and an upper part. The lower part is fluidly connected to the discharge pump <NUM>, and the upper part is fluidly connected to the circulation pump <NUM>. The lower and upper parts are configured with a lower filter <NUM> and an upper filter <NUM>, respectively. The reservoir <NUM> is configured to store a solvent containing one or more C1 to C4 fluorinated hydrocarbon. The first evaporator <NUM> and the first condenser <NUM> are connected via a heat pump <NUM>. Another heat pump <NUM> may be connected to the second condenser <NUM>. A collection vessel <NUM> is connected to the first evaporator <NUM>.

In this embodiment, the energy utilization may be further improved by connecting the heat pumps <NUM> and <NUM> which are mutually inverted by temperature in the current process. For example, the heat pump <NUM> is connected between the first evaporator <NUM> and the first condenser <NUM>. Alternatively, the heat pump <NUM> may be on one side connected to a jacket <NUM> and the other to the second condenser <NUM>. In this disclosure, heat pumps can be thermodynamic, or refrigeration coupled.

Referring to <FIG>, there is shown an apparatus <NUM> for extracting essential oils and oleoresins from a plant material. The apparatus <NUM> comprises a circulation pump <NUM>, a discharge pump <NUM>, an extraction module <NUM>, a reservoir <NUM>, a first evaporator <NUM>, a second evaporator <NUM>, a first condenser <NUM>, and a second condenser <NUM>. The discharge pump <NUM> is fluidly connected to the circulation pump <NUM>. The extraction module <NUM> includes at least one extraction vessel <NUM> for receiving the plant material. The reservoir <NUM> is fluidly connected to the discharge pump <NUM>. The first evaporator <NUM> is fluidly connected to the circulation pump <NUM>. The second evaporator <NUM> is fluidly connected to the first evaporator <NUM>. The first condenser <NUM> is fluidly connected to the circulation pump <NUM>, and to the reservoir <NUM>, a vapor pump <NUM> for facilitating vaporization of solvent, and the vapor pump <NUM> is fluidly connected to the top of the at least one extraction vessel <NUM>, to the circulation pump <NUM>, and to the first condenser <NUM>. The second condenser <NUM> is disposed between and fluidly connected to the vapor pump <NUM> and the reservoir <NUM>. The at least one extraction vessel <NUM> has a lower part and an upper part. The lower part is fluidly connected to the discharge pump <NUM>, and the upper part is fluidly connected to the circulation pump <NUM>. The lower and upper parts are configured with a lower filter <NUM> and an upper filter <NUM>, respectively. The reservoir <NUM> is configured to store a solvent containing one or more C1 to C4 fluorinated hydrocarbon. The first evaporator <NUM> and the first condenser <NUM> are connected via a heat pump <NUM>. A collection vessel <NUM> is connected to the second evaporator <NUM>.

The process has similar flows as shown in <FIG>, <FIG> and <FIG> with the difference that the vapors from the first evaporator <NUM> are sent to the first condenser <NUM> and the vapors from the at least one extraction vessel <NUM> to the second condenser <NUM> via the vapor pump <NUM>. There are also two evaporators where the first evaporator <NUM> is dropping the temperature and pressure of the solvent to speed up the separation in second evaporator <NUM>.

The heat pump <NUM> is dual pump, either executed as <NUM> pumps located one located between first evaporator <NUM> and first condenser <NUM> and second between second evaporator <NUM> and reservoir <NUM> or as one pump with dual heat exchangers disposed between the first evaporator <NUM>, the first condenser <NUM>, the second evaporator (separator) <NUM> and the reservoir <NUM>, to provide a fluid connection therebetween. External cooler <NUM> may be used to chill the second condenser <NUM>, the reservoir <NUM> and the jacket <NUM> to speed up the process.

Referring to <FIG>, there is shown an apparatus <NUM> for extracting essential oils and oleoresins from a plant material. The apparatus <NUM> comprises a circulation pump <NUM>, a discharge pump <NUM>, an extraction module <NUM>, a reservoir <NUM>, a first evaporator <NUM>, a second evaporator <NUM>, a first condenser <NUM>, vapor pump <NUM>, and a second condenser <NUM>. The discharge pump <NUM> is fluidly connected to the circulation pump <NUM>. The extraction module <NUM> includes a first extraction vessel 410a and a second extraction vessel 410b. The reservoir <NUM> is fluidly connected to the discharge pump <NUM>. The first evaporator <NUM> is fluidly connected to the circulation pump <NUM>. The second evaporator <NUM> is fluidly connected to the first evaporator <NUM>. The first condenser <NUM> is fluidly connected to the circulation pump <NUM>, and to the reservoir <NUM>. The vapor pump <NUM> is provided for facilitating vaporization of solvent. The second condenser <NUM> is disposed between and fluidly connected to the vapor pump <NUM> and the reservoir <NUM>.

The first extraction vessel 410a has a first lower part 413a and a first upper part 414a. The first lower part 413a is fluidly connected to the discharge pump <NUM>, and the first upper part 414a is fluidly connected to the circulation pump <NUM>. The first lower and upper parts 413a, 414a are configured with a first lower filter 411a and a first upper filter 412a, respectively. The second extraction vessel 410b has a second lower part 413b and a second upper part 414b. The second lower part 413b is fluidly connected to the discharge pump <NUM>, and the second upper part 414b is fluidly connected to the circulation pump <NUM>. The second lower and upper parts 413b, 414b are configured with a second lower filter 411b and a second upper filter 412b, respectively.

The vapor pump <NUM> is fluidly connected to the first upper part 414a of the first extraction vessel 410a, to the second upper part 414b of the second extraction vessel 410b, to the circulation pump <NUM>, to the first condenser <NUM>, and to the second condenser <NUM>. The reservoir <NUM> is configured to store a solvent containing one or more C1 to C4 fluorinated hydrocarbon. A non-limiting example of the C1 to C4 fluorinated hydrocarbon is <NUM>,<NUM>, <NUM>,<NUM>-tetrafluoroethane. A collection vessel <NUM> is connected to the second evaporator <NUM>.

A heat pump <NUM> is disposed between the first evaporator <NUM>, the first condenser <NUM>, the second evaporator <NUM> and the reservoir <NUM>, to provide a fluid connection therebetween.

The process has similar flow as the apparatus shown in <FIG> with the difference of an additional extraction vessel. In this embodiment the solvent miscella drained from the second extraction vessel 410b via the discharge pump <NUM> is evaporated first in the first evaporator <NUM> and then separated in the second evaporator <NUM> while the vapors from the second evaporator <NUM> are condensed via the first condenser <NUM> and liquefied in the reservoir <NUM> while the vapors from the plant material drying in the first extraction vessel 410a are sent to the second condenser <NUM> via the vapor pump <NUM>.

Referring to <FIG>, there is shown an apparatus <NUM> for extracting essential oils and oleoresins from a plant material. The comprises a circulation pump <NUM>, a discharge pump <NUM>, an extraction module <NUM>, a reservoir <NUM>, a first evaporator <NUM>, a second evaporator <NUM>, a first condenser <NUM>, a vapor pump <NUM>, a second condenser <NUM>, a third condenser <NUM>. The discharge pump <NUM> is fluidly connected to the circulation pump <NUM>. The extraction module <NUM> includes a first extraction vessel 510a and a second extraction vessel <NUM>10b. The reservoir <NUM> is fluidly connected to the discharge pump <NUM>. The first evaporator <NUM> is fluidly connected to the circulation pump <NUM>. The second evaporator <NUM> is fluidly connected to the first evaporator <NUM>. The first condenser <NUM> is fluidly connected to the circulation pump <NUM>. The vapor pump <NUM> for is provided for facilitating vaporization of solvent. The second condenser <NUM> is disposed between and fluidly connected to the vapor pump <NUM> and the reservoir <NUM>. The third condenser <NUM> is disposed between and fluidly connected to the first condenser <NUM> and the reservoir <NUM>.

The first extraction vessel 510a has a first lower part and a first upper part. The first lower part is fluidly connected to the discharge pump <NUM>, and the first upper part is fluidly connected to the circulation pump <NUM>. Similarly, the second extraction vessel 510b has a second lower part and a second upper part. The second lower part is fluidly connected to the discharge pump <NUM>, and the second upper part is fluidly connected to the circulation pump <NUM>.

The vapor pump <NUM> is fluidly connected to the first upper part (at a top) of the first extraction vessel <NUM>10a, to the second upper part (at a top) of the second extraction vessel 510b, to the circulation pump <NUM>, to the first condenser <NUM>, and to the second condenser <NUM>. The reservoir <NUM> is configured to store a solvent containing one or more C1 to C4 fluorinated hydrocarbon. A first collection vessel <NUM> is connected to the first evaporator <NUM>, and first collection vessel <NUM> is connected to the second evaporator <NUM>.

A heat pump <NUM> is disposed between the first evaporator <NUM>, the first condenser <NUM>, the second evaporator <NUM> and the third condenser <NUM>, to provide a fluid connection therebetween. Another heat pump <NUM> is connected on one side to the second condenser <NUM>, and to the jackets 515a, 515b on the other (during the solvent recovery process).

In this embodiment, multiple staged condensers with separate collection vessels are used. For example, the first evaporator <NUM> coupled with the first condenser <NUM> may remove/collect a fraction in the first collection vessel <NUM>, and then the second evaporator <NUM> coupled with the third condenser <NUM> may remove/collect another fraction in the second collection vessel <NUM>, and so on.

Further, as the time for extraction may be from <NUM> to <NUM> hours and the time for evaporation is usually <NUM> hour to <NUM> hours using multiple extraction modules <NUM> can optimize the workflow. As an example, to offset the <NUM> hour time for evaporation (solvent recovery) on <NUM> extraction <NUM> extraction modules <NUM> can be used. They will work on the revolver principal where every <NUM> material will be loaded, and the solvent recovery will be performing while the extraction is performed from the 1st to the 4th extraction. In general, the extraction modules <NUM> are multiple in the time of extraction to evaporation ratio the evaporators are multiple on the fractions need to be collected separate by temperature where the temperature increases from the first to the last while in the coupled condensers the temperature decreases with the same ratio, therefore they cross connect together.

For example, the extraction is at <NUM>, the first evaporator <NUM> operates at <NUM> and the second evaporator <NUM> operates at <NUM>, while the first condenser <NUM> operates at <NUM> and third condenser <NUM> operates at <NUM>, wherein the first evaporator <NUM> is fluidly connected via the heat pump <NUM> to the third condenser <NUM> and the second evaporator <NUM> is fluidly connected via the heat pump <NUM> to the first condenser <NUM>.

The evaporators may also work in parallel coupled with the extraction vessels. For example, the extraction is performed under <NUM>, while a first evaporator evaporates at <NUM> and a coupled condenser operates at <NUM>; and on the next cycle, the extraction is performed under <NUM>, while a second evaporator evaporates at <NUM> and a coupled condenser operates at <NUM>.

Referring to <FIG>, shown is an apparatus <NUM> for extracting essential oils and oleoresins from a plant material. The apparatus <NUM> comprises a circulation pump <NUM>, a discharge pump <NUM>, an extraction module <NUM>, a reservoir <NUM>, a first evaporator <NUM>, a second evaporator <NUM>, a first condenser <NUM>, a vapor pump <NUM>, a second condenser <NUM>, and a third condenser <NUM>. The discharge pump <NUM> is fluidly connected to the circulation pump <NUM>. The extraction module <NUM> includes a first extraction vessel 610a and a second extraction vessel 610b. The reservoir <NUM> is fluidly connected to the discharge pump <NUM>. The first evaporator <NUM> is fluidly connected to the circulation pump <NUM>. The second evaporator <NUM> is fluidly connected to the first evaporator <NUM> The first condenser <NUM> is fluidly connected to the circulation pump <NUM>. The vapor pump <NUM> is provided for facilitating vaporization of solvent. The second condenser <NUM> is disposed between and fluidly connected to the vapor pump <NUM> and the reservoir <NUM>. The third condenser <NUM> is disposed between and fluidly connected to the first condenser <NUM> and the reservoir <NUM>.

The first extraction vessel 610a has a first lower part and a first upper part. The first lower part is fluidly connected to the discharge pump <NUM>, and the first upper part is fluidly connected to the circulation pump <NUM>. Similarly, the second extraction vessel 610b has a second lower part and a second upper part. The second lower part is fluidly connected to the discharge pump <NUM>, and the second upper part fluidly connected to the circulation pump <NUM>.

The vapor pump <NUM> is fluidly connected to the first upper part (at a top) of the first extraction vessel 610a, to the second upper part (at a top) of the second extraction vessel 610b, to the circulation pump <NUM>, to the first condenser <NUM>, and to the second condenser <NUM>. The reservoir <NUM> is configured to store a solvent containing one or more C1 to C4 fluorinated hydrocarbon. A collection vessel <NUM> is connected to the second evaporator <NUM>.

A heat pump <NUM> is disposed between the first evaporator <NUM>, the first condenser <NUM>, the second evaporator <NUM> and the third condenser <NUM>, to provide a fluid connection therebetween. Another heat pump <NUM> is connected on one side to the second condenser <NUM>, and to the jackets of the first and second extraction vessels 610a, 610b on the other.

Further, a filter device <NUM> is disposed between and fluidly connected to the circulation pump <NUM> and the discharge pump <NUM>.

In the present embodiment, a separation is performed by the filter device <NUM>. Preferably, the filter device comprises a membrane filter to single out a desired constituent or fraction, for example, by its molecular weight. The filter device <NUM> may allow the main stream to go through into the first evaporator <NUM> for separation of one or more first ingredients, while single out a fraction with a larger molecular weight into the second evaporator <NUM> for separation of one or more second ingredients.

As an alternative, the filter device <NUM> may be an adsorbent filter. The adsorbent filter may be a cassette filled with specially selected media to absorb certain compounds. A non-limiting Example of adsorbent is earth compound mixed with silica and activated carbon in various proportions. The absorbed ingredient would stay with the adsorbent, and the adsorbent needs to be changed every time the plant material in the extraction vessel(s) is changed. This type of filter is also called a scrubbing filter.

In addition, the filter device <NUM> may be detachable and replaceable. Either a scrubbing or membrane filter can be chosen and installed, thereby configuring the roles of the first and second evaporators <NUM>, <NUM> with a bypass pipe <NUM> around the filter <NUM>. The reason for disposing the bypass pipe <NUM> is that in between the processes there is a pressure difference in the vessels anywhere between <NUM> to <NUM> bars and that pressure needs to be equalized between processes. The bypass pipe <NUM> will be able to equalize the pressure between vessels first and then connect the filter in the loop to avoid taring and extreme pressure deviations when pressure is equalized in between vessels, in a pressurized system such as one of the apparatus <NUM>.

A membrane filter requires one miscella (solvent and constituents) input and <NUM> outputs with different constituents where one is separating the lower and the second the higher molecule mass constituents. With that regards the <NUM> evaporators can be reconfigured instead in serial to a parallel architectural flow. For example, when a membrane filter is used, the first evaporator <NUM> may be used for the solvent with constituents and the second evaporator <NUM> may be used for higher molecule mass constituents usually dissolved in the main solvent or a co-solvent (e.g., acetone, ethanol, hexane etc.). The co-solvent may only be circulated in a secondary filter loop and not mixed with the main solvent loop <NUM>, <NUM>, <NUM> and <NUM> (<FIG>).

Referring now to <FIG>, shown is an apparatus <NUM> for extracting essential oils and oleoresins from a plant material. The apparatus <NUM> comprises a circulation pump <NUM>, a discharge pump <NUM>, an extraction module <NUM>, a first evaporator <NUM>, a first condenser <NUM>, a vapor pump <NUM>, a second condenser <NUM>, and a third condenser <NUM>. The discharge pump <NUM> is fluidly connected to the circulation pump <NUM>. The extraction module <NUM> includes a extraction vessel <NUM>. The reservoir <NUM> is fluidly connected to the discharge pump <NUM>. The first evaporator <NUM> is fluidly connected to the circulation pump <NUM>. The second evaporator <NUM> is fluidly connected to the first evaporator <NUM>. The first condenser <NUM> is fluidly connected to the circulation pump <NUM>. The vapor pump <NUM> is provided for facilitating vaporization of solvent. The second condenser <NUM> is disposed between and fluidly connected to the vapor pump <NUM> and the reservoir <NUM>. The third condenser <NUM> is disposed between and fluidly connected to the first condenser <NUM> and the reservoir <NUM>. A collection vessel <NUM> is connected to the second evaporator <NUM>.

A heat pump <NUM> is disposed between the first evaporator <NUM>, the first condenser <NUM>, the second evaporator <NUM> and the third condenser <NUM>, to provide a fluid connection therebetween. Another heat pump <NUM> is connected on one side to the second condenser <NUM>, and to a jacket of the extraction vessel <NUM> on the other.

Further, a filter device <NUM> is disposed between and fluidly connected to the circulation pump <NUM> and the discharge pump <NUM>. The filter device <NUM> preferably comprises a membrane filter.

In the present embodiment, the filter device is to be used with a co-solvent. Accordingly, an auxiliary loop is equipped to handle the co-solvent while a main loop still operates continuously during a short loop circulation as described above to isolate and collect constituents into the collection vessel <NUM> through the first evaporator <NUM> and the second evaporator (separator) <NUM>. The auxiliary loop may comprise an auxiliary reservoir <NUM>, an auxiliary circulation pump <NUM>, an auxiliary collection vessel <NUM>, an auxiliary evaporator <NUM>; and an auxiliary collection vessel <NUM>. The auxiliary circulation pump <NUM> includes, for example, one or more filters, one or more pumps, and one or more flowmeters (not shown). In this auxiliary loop, a solution comprising the co-solvent and one or more active components of the plant material dissolved therein co-solvent is circulated through the membrane filter of the filter device <NUM> and separated in the auxiliary evaporator <NUM>. The separated active components are collected in the auxiliary collection vessel <NUM>. Such filtration mode is also called self-cleaning filtering.

Referring to aforementioned drawings, this disclosure also provides a method for extracting essential oils and oleoresins from a plant material using an apparatus of this disclosure.

The method for extracting essential oils and oleoresins from a plant material using the above-described apparatus comprises extracting one or more active components from a plant material placed in the at least one extraction vessel through the short loop circulation to perform the short loop circulation mode, wherein the discharge pump pumps the solution from the bottom of the at least one extraction vessel to the circulation pump, and the solution is transmitted to the top of the at least one extraction vessel through the circulation pump; and extracting the plant material remained in the at least one extraction vessel through a long loop circulation, wherein the discharge pump pumps the solution from the bottom of the at least one extraction vessel to the circulation pump, the solution is transmitted to the first evaporator where the solvent is gasified, and the circulation pump pumps the gasified solvent to the first condenser.

The method for extracting essential oils and oleoresins from a plant material according to this disclosure may comprise the steps of extraction and evaporation.

The step of extraction may be performed through a short loop circulation followed by a long loop circulation.

Take <FIG>, <FIG> and <FIG> as an illustration, providing an apparatus <NUM> comprising a circulation pump <NUM>; a discharge pump <NUM> fluidly connected to the circulation pump <NUM>; an extraction module <NUM> including at least one extraction vessel <NUM> for receiving the plant material, the at least one extraction vessel <NUM> having a lower part <NUM> fluidly connected to the discharge pump <NUM> and an upper part <NUM> fluidly connected to the circulation pump <NUM>, wherein the lower and upper parts (<NUM>, <NUM>) are configured with a lower filter <NUM> and an upper filter <NUM>, respectively; a reservoir <NUM> fluidly connected to the discharge pump <NUM>, the reservoir <NUM> being storing a solvent containing a C1 to C4 fluorinated hydrocarbon; a first evaporator <NUM> fluidly connected to the circulation pump <NUM>; and a first condenser <NUM> fluidly connected to the circulation pump <NUM>, and to the reservoir <NUM>.

At first, the method is to extract one or more active components from a plant material placed in the at least one extraction vessel <NUM> through a short loop circulation wherein the discharge pump <NUM> pumps the solution from the bottom of the at least one extraction vessel <NUM> to the circulation pump <NUM>, and the solution is transmitted to the top of the at least one extraction vessel <NUM> through the circulation pump <NUM>. In the short loop circulation, the discharge pump <NUM> pumps a solution comprising the solvent and one or more active components of the plant material dissolved therein from the bottom of the at least one extraction vessel <NUM>, passing through the circulation pump <NUM>, and then back to the top of the at least one extraction vessel <NUM>.

And then, the method is to extract the plant material remained in the at least one extraction vessel <NUM> through a long loop circulation, wherein the discharge pump <NUM> pumps the solution from the bottom of the at least one extraction vessel <NUM> to the circulation pump <NUM>, the solution is transmitted to the first evaporator <NUM> where the solvent is gasified, and the circulation pump <NUM> pumps the gasified solvent to the first condenser <NUM>.

According to this disclosure, the short circulation loop will recirculate the solvent through the extraction module and will enrich the solvent every pass with constituents turning it into miscella stream. This process is also known as re-percolation. It is known state of art that solvent extracts constituents having similar dielectric constant. During the re-percolation the solvent will be changing its polarity and dielectric constant and will be widening the extraction selectivity while the miscella will be slowly changing its dielectric constant from as example <NUM> to around <NUM>-<NUM>. This will widen the ability of the solvent to achieve additionally benefits in extraction of constituents outside of its original solubility limits.

In a short loop circulation as described above, a plant material is mixed with a solvent containing a C1 to C4 fluorinated hydrocarbon under predetermined pressure and temperature conditions in order to extract one or more target active components, wherein a solution comprising the solvent and one or more active components of the plant material dissolved therein is circulating through the extraction vessel(s) continuously for a predetermined time, so that the miscella is homogenized and the active components is dissolved homogeneously along the entire volume of the extraction vessel(s). This short loop circulation is also called reperculation.

The time, temperature and the process are carefully adjusted toward the extraction of target active components and the saturation of the components in the solution. The flow rate or the time of extraction is calculated based on the volume of the vessel and the extracted compounds. For example, a reperculation at a flow rate of <NUM> to <NUM>/min for <NUM> minutes at <NUM> in <NUM> vessel will turn the solvent <NUM> times, and every time the dielectric constant will increase with around <NUM>% or with constant between <NUM> to <NUM>, it would extract almost all flavonoid and acid components, while a re-percolation at a flow rate of <NUM> to <NUM>/min for <NUM> minutes at <NUM> will change the dielectric constant from <NUM> to <NUM> and would extract almost all acid components (such as amino acids and organic acids).

The long loop circulation may work in <NUM> modes: draining (batch) (<FIG>) and washing (continues) (<FIG>). In the batch process, the solvent is introduced in the extraction module <NUM> from the reservoir <NUM> then drained and via the circulation pipes <NUM> and <NUM> fed to the evaporator <NUM> where extract separated in container <NUM> and solvent collected in the reservoir <NUM> through the second evaporator <NUM>.

The continues washing is shown at <FIG> where the fresh solvent is constantly fed to the extraction module <NUM> from the reservoir <NUM> via the circulation pipe <NUM> then the extract is separated from the miscella in the separator <NUM> and the solvent vapors are further condensed in the reservoir <NUM> via the condenser <NUM>. Additional re-percolation can be applied according <FIG> to the continued and batch extraction and this may be repeated until the plant material is fully depleted.

The step of evaporation is to separate the active components from the material or solution by vaporizing the solvent to its gaseous phase. There are <NUM> types of evaporation: drying and recovery. During drying the solvent is evaporated from the material located in the extraction module <NUM> and liquefied in the reservoir via the first and second condenser with the help of the circulation pipe <NUM> and recovery pump <NUM>. And the recovery is a recovery of the solvent from the oil that happens in the first evaporator <NUM> where the recovered solvent is liquefied in the reservoir <NUM> via the condenser <NUM> and the extract collected in the collection vessel <NUM>.

According to this disclosure, the method may further comprise the steps of drying and recovery. In the step of drying, the solvent is separated from the plant material by vaporizing the solvent to its gaseous phase, and in the step of recovery, the solvent in its gaseous phase is liquefied to its liquid phase for recycling.

Claim 1:
An apparatus (<NUM>) for extracting essential oils and oleoresins from a plant material, comprising:
a circulation pump (<NUM>);
a discharge pump (<NUM>) fluidly connected to the circulation pump (<NUM>);
an extraction module (<NUM>) including at least one extraction vessel (<NUM>) for receiving the plant material, the at least one extraction vessel (<NUM>) having a lower part fluidly connected to the discharge pump (<NUM>) and an upper part fluidly connected to the circulation pump (<NUM>),
wherein the lower part and the upper part are configured with a lower filter (<NUM>) and an upper filter (<NUM>), respectively;
a reservoir (<NUM>) fluidly connected to the discharge pump (<NUM>), wherein the reservoir (<NUM>) is configured to store a solvent containing a C1 to C4 fluorinated hydrocarbon;
a first evaporator (<NUM>) fluidly connected to the circulation pump (<NUM>); and
a first condenser (<NUM>) fluidly connected to the circulation pump (<NUM>), and to the reservoir (<NUM>);
wherein a short loop circulation (S) comprises the discharge pump (<NUM>), the extraction module (<NUM>) and the circulation pump (<NUM>) without the first evaporator (<NUM>), the reservoir (<NUM>) and the first condenser (<NUM>),
wherein a long loop circulation (L) comprises the discharge pump (<NUM>), the extraction module (<NUM>), the circulation pump (<NUM>), the first evaporator (<NUM>), the reservoir (<NUM>) and the first condenser (<NUM>),
wherein the apparatus (<NUM>) is configured to operate in a short loop circulation mode, and in the short loop circulation mode the discharge pump (<NUM>) pumps a solution comprising the solvent and one or more active components of the plant material dissolved in the solution from the bottom of the at least one extraction vessel (<NUM>), passing through the circulation pump (<NUM>), and then back to the top of the at least one extraction vessel (<NUM>).