WO2021133410A1 - Procédé de post-traitement pour huile de cannabis - Google Patents

Procédé de post-traitement pour huile de cannabis Download PDF

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Publication number
WO2021133410A1
WO2021133410A1 PCT/US2019/068720 US2019068720W WO2021133410A1 WO 2021133410 A1 WO2021133410 A1 WO 2021133410A1 US 2019068720 W US2019068720 W US 2019068720W WO 2021133410 A1 WO2021133410 A1 WO 2021133410A1
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Prior art keywords
range
mixture
fraction
predetermined
heating
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PCT/US2019/068720
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English (en)
Inventor
David Ellis
Tamer Mohamed
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Cresco Labs Llc
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Priority to PCT/US2019/068720 priority Critical patent/WO2021133410A1/fr
Publication of WO2021133410A1 publication Critical patent/WO2021133410A1/fr

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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
    • C11B3/00—Refining fats or fatty oils
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2250/00—Food ingredients
    • A23V2250/30—Other Organic compounds
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2300/00—Processes
    • A23V2300/50—Concentrating, enriching or enhancing in functional factors

Definitions

  • the present invention relates to a method for post processing oil extracted from cannabis plants. More specifically, the present invention relates to a method for post processing that provides a full spectrum profile of cannabinoids and a high retention of terpenes.
  • Post processing techniques can be applied to oil extracted from cannabis plants to produce products having desirable formulations for intended uses. For example, if can be desirable for the post processed oil to have a high retention of terpenes, which are the aromatic oils produced by plants including cannabis.
  • the terpenes not only provide the characteristic smells that people normally associate with the plants, but can also provide other beneficial health effects depending on use.
  • the post processed oil can also be desirable for the post processed oil to have a full spectrum of cannabinoids, for example without limitation, tetrahydrocannabinol (THC), tetrahydrocannabinolic acid (THCA), cannabidiol (CBD), cannabinol (CBN), cannabichromene (CBC), and cannabigerol (CBG).
  • THC tetrahydrocannabinol
  • THCA tetrahydrocannabinolic acid
  • CBD cannabidiol
  • CBN cannabinol
  • CBC cannabichromene
  • CBG cannabigerol
  • Butane hash oil extraction which uses Butane to produce a product oil commonly known as Butane hash oil (BHO).
  • BHO Butane hash oil
  • Typical non-post processed extracted oil for example, BHO, does not provide a high level of terpenes or a full spectrum of cannabinoids.
  • the raw non-post processed oil can be improved by applying post processing techniques to the raw oil to achieve desired formulations for intended uses. Therefore, there is a need for post processing techniques that produce cannabis oil having a high level of terpenes and/or a full spectrum of cannabinoids.
  • a method for post processing oil extracted from cannabis comprises the steps of placing the oil into a container at a first predetermined temperature for a first predetermined time during which the oil will separate into two parts comprising a high terpene (HT) liquid fraction and a high cannabinoid (HC) crystal fraction, heating the HT and HC fractions under a first predetermined level of vacuum at a second predetermined temperature for a second predetermined time, and heating the HC fraction to a third predetermined temperature for a third predetermined time.
  • HT terpene
  • HC cannabinoid
  • a method for post processing oil extracted from cannabis comprises the steps of placing the oil into a container at a first predetermined temperature in a range of between about 35°C to about 50°C for a first predetermined time in a range of between about 2 days to about 30 days, during which time the oil will separate into two parts comprising a high terpene (HT) liquid fraction and a high cannabinoid (HC) crystal fraction.
  • HT high terpene
  • HC cannabinoid
  • the method further comprises the steps of heating the HT and HC fractions under a first predetermined level of vacuum in a range between about -25 inches of Hg to about -30 inches of Hg at a second predetermined temperature in a range between about 25°C to about 50°C for a second predetermined time in a range between about 48 hours to about 96 hours.
  • the method still further comprises the step of heating the HC fraction to a third predetermined temperature in a range between about 80°C to about 100°C for a third predetermined time in a range between about 10 hours to about 14 hours.
  • the method further comprises the steps of formulating a finished mixture by adding a first predetermined quantity of the HT fraction in a range of between about 10% to about 14% of the finished mixture by weight of the HT fraction back into the HC fraction to create a first mixture, adding a second predetermined quantity of benign terpenes in a range between about 5% to about 9% of the finished mixture by weight into the first mixture to create a second mixture, and mixing the second mixture while heating at a temperature range of between about 60°C to about 90°C for a time range of between about 15 minutes and about 30 minutes to create the finished mixture.
  • a method for post processing oil extracted from cannabis comprises the steps of placing the oil into a container at about 35°C for a first predetermined time in a range of between about 3 days to about 10 days, during which time the oil will separate into two parts comprising a high terpene (HT) liquid fraction and a high cannabinoid (HC) crystal fraction, heating the HT and HC fractions under a vacuum level of about -28 inches of Hg at about 35°C for about 72 hours, and heating the HC fraction about 95°C for about 12 hours.
  • HT terpene
  • HC cannabinoid
  • the method further comprises the steps of adding about 12% of the finished mixture by weight of the HT fraction back into the HC fraction to create a first mixture, adding about 7% of the finished mixture by weight of benign terpenes into the first mixture to create a second mixture, and mixing the second mixture while heating at a temperature of about 75°C for a minimum of about 20 minutes to create the finished mixture.
  • Figure 1 is a process flowchart for a cannabis oil extraction process
  • Figure 2 is a process flowchart for a first example of a method for post processing a quantity of raw cannabis oil extract
  • FIG. 3 is an embodiment of a pressure rated vessel (PRV) of the sort suitable for use in the present invention.
  • PRV pressure rated vessel
  • Figure 4 is a process flowchart for a second example of a method for post processing a quantity of raw cannabis oil extract.
  • the first step for producing cannabis oil having high terpene retention and a full spectrum of cannabinoids is to provide raw cannabis oil extracted by any means as may be known in the art, for example, by a hydrocarbon cannabis oil extraction process.
  • a process starting with fresh frozen cannabis plants in contrast to plants that have been dried or heated produces a product known as live resin, which typically has a higher retention of terpenes than would result from plants that have been dried or heated.
  • One exemplary hydrocarbon cannabis oil extraction process suitable for use with the post processing techniques described hereinbelow utilizes liquid Butane as the hydrocarbon.
  • the exemplary process is executed with the aid of a chiller for the solvent tank that is set, for example, to a temperature range between about 0°C and about -20°C.
  • the chiller is set to a temperature range between about -2°C and about -15°C.
  • the chiller is set to a temperature between about -5°C and about -9°C, preferably at about -7°C.
  • a vacuum sealed bag of the fresh frozen cannabis is placed into a cryogenic unit, for example, at a temperature of about -80°C for about 5 to 6 hours at step 12.
  • a material column for example, a tube lined with a filtering cloth or a screen across a bottom end is also placed into the cryogenic unit and allowed to cool for at least an hour at step 14.
  • the bag of fresh frozen cannabis is removed from the cryogenic unit and the frozen cannabis is ground up, for example, by pounding with a mallet at step 16.
  • the ground cannabis is poured into a portion of the material column and packed down firmly. More ground cannabis is repeatedly poured into the material column and packed down firmly until the material column is considered to be fully packed, which occurs when about 1-2 inches are left unfilled at a top of the material column.
  • the fully packed material column can be placed back into the cryogenic unit to cool for at least three more hours.
  • the fully packed material column is removed from the cryogenic unit, a top of the material column is sealed, and the material column is placed on top of a collection vessel that is connected to an extraction system under vacuum.
  • a separate vacuum system is used to pull vacuum on the extraction system and therefore on an outlet of the material column.
  • a vacuum for example, of between about -25 and about -30 inches of Hg, and preferably of about -28 inches of Hg is established in the material column by the vacuum system.
  • a liquid Butane supply is disposed in fluid communication with an inlet at the top of the material column so that a predetermined amount of the liquid Butane, for example, between about 1 pound and about 5 pounds of liquid Butane per pound of frozen cannabis biomass, preferably between about 2 pounds and about 4 pounds of liquid Butane per pound of frozen cannabis biomass, and more preferably about 3 pounds of liquid Butane per pound of frozen cannabis biomass, flows into the material column assisted by a pneumatic pump connected on the extraction system.
  • the inlet to and the outlet from the material column are closed, and the liquid Butane and the raw cannabis oil extract are pumped out of the collection vessel for post processing.
  • Both of the post processing methods provide a cannabis oil formulation that has a high retention of terpenes and a full spectrum cannabinoid profile.
  • both of the post processing methods inhibits further crystallization of THCA once the process is complete. Inhibiting further crystallization of THCA is imperative for vaporizer cartridges as it stops clogging of the device due to THCA crystalline being absent.
  • a first step in a first exemplary method for post processing a quantity of raw cannabis oil extract acquired from the extraction process described hereinabove or by any other suitable process as known in the art is a crystalizing step.
  • the raw cannabis oil extract is placed into one or more containers, for example, one or more wide mouth mason jars, and left to stand at a first predetermined temperature, for example, in an oven, for a first predetermined time to begin a crystallization process.
  • the first predetermined temperature is in a range of between about 30°C to about 50°C. In another embodiment the first predetermined temperature is about 35°C. Both the first predetermined temperature and the first predetermined time may be dependent upon the particular strain of cannabis being processed. In one embodiment the first predetermined time is anywhere between about 2 days to about 30 days. In another embodiment the first predetermined time is in a range of between about 3 days to about 10 days. In a further embodiment the first predetermined time is in a range between about 4 days to about 7 days.
  • the crystalizing step in this embodiment is executed at atmospheric pressure. However, in other embodiments the crystalizing step may be executed at a pressure greater than or less than atmospheric pressure. After the predetermined time the cannabis oil extract will have separated into two parts comprising a high terpene (HT) liquid fraction on top and a high cannabinoid (HC) crystal fraction on bottom.
  • HT high terpene
  • HC cannabinoid
  • the HT and HC fractions are decanted into separate containers, for example, by filtering the oil extract through a screen.
  • the screen has apertures that are, for example, about 300 microns wide; however in other embodiments the filtering screen may have apertures that are larger or smaller then about 300 microns wide.
  • the size of the apertures in the filtering screen may be dependent upon the strain of cannabis being processed.
  • the HT liquid fraction passes through the screen and is collected in a container, for example, a beaker.
  • the HC crystal fraction collects on the screen and is placed into a separate container.
  • the decanted HT and HC fractions are vacuum oven purged.
  • the decanted HT and HC fractions are placed into a vacuum oven under a first predetermined level of vacuum and at a second predetermined temperature for a second predetermined time to purge any hydrocarbons, for example Butane, remaining in the fractions.
  • the first predetermined level of vacuum is in a range of between about -25 inches of Hg to about -30 inches of Hg.
  • the first predetermined level of vacuum is about -28 inches of Hg.
  • the second predetermined temperature is in a range of between about 25°C to about 50°C.
  • the second predetermined temperature is about 35°C.
  • the second predetermined time is in a range between about 48 hours and about 96 hours. In another embodiment the second predetermined time is about 72 hours.
  • the container comprising the HC fraction is heated to a third predetermined temperature for a third predetermined time to activate the HC fraction.
  • the third predetermined temperature is in a range of between about 80°C to about 100°C. In another embodiment the third predetermined temperature is about 95°C. In one embodiment the third predetermined time is in a range between about 10 hours and about 14 hours. In another embodiment the third predetermined time is about 12 hours.
  • step 36 may further include a brief ramp up time for reaching the third predetermined temperature.
  • the HC fraction may first be heated to a lower temperature that is less than the third predetermined temperature and held there for a brief period of time, for example without limitation, about 15 minutes to about 30 minutes, to allow the glassware to heat up.
  • Including the brief ramp up time of the alternative embodiment may be desirable because heating the glassware directly to the third predetermined temperature may risk cracking the glassware, which would be undesirably messy and expensive.
  • the HC fraction is heated to the third predetermined temperature and held there until the time since being first heated to the lower temperature reaches the third predetermined time.
  • the activation step is meant to specifically decarboxylate cannabinoids such as CBDA and THCA that are comprised with a carboxyl group. Removal of the carboxyl group enables binding to CB1 and CB2 receptors.
  • the CBDA is converted into CBD and the THCA is converted into “activated” THC. This activation is performed by the activating step outlined above.
  • the activating step is executed correctly, activation of the HC fraction is evident from melting of the HC crystals as well as the off gassing of CO 2 . As the activating step progresses the HC fraction will start to become a homogenous oil mixture. The activating step is complete when there is no longer any CO 2 off gassing from the HC fraction, meaning that the HC fraction should be fully activated. In a further embodiment, the activating step is preferably executed using a stir bar to stir the HC fraction while heating to ensure complete activation thereof.
  • a formulation step completes the first exemplary post processing method.
  • the formulation step comprises first and second adding steps and a final mixing step.
  • a first of two adding steps comprises adding a first predetermined quantity of the purged HT fraction into the now activated HC fraction. The amount of purged HT fraction added is determined based on the desired percentage of HT fraction by weight (%w) in the final mixture.
  • a second of two adding steps comprises adding a second predetermined quantity of benign, flavorless, and inert terpenes (BT fraction) into a mixture of the activated HC fraction and the purged HT fraction. The amount of BT fraction added is determined based on the desired percentage of BT fraction by weight (%w) in the final mixture.
  • the formula for deducing how much of the HT fraction and how much of the BT fraction are needed for adding in the two adding steps is simple to derive. For example, weighing the quantities of components in grams, one can derive a final formulated batch weight (FFBW) based on the desired percentages of the FFBW for the HT and BT fractions through the following progression of equations:
  • FFBW grams HC grams + HT grams + BT grams (1)
  • the first predetermined quantity of the HT fraction is in a range between about 10% by weight (%w) to about 14% by weight (%w) of the completed mixture. In another embodiment the first predetermined quantity of the HT fraction is about 12% by weight (%w) of the completed mixture. In one embodiment the second predetermined quantity of the BT fraction is in a range between about 5% by weight (%w) to about 9% by weight (%w) of the completed mixture. In another embodiment the second predetermined quantity of the BT fraction is about 7% by weight (%w) of the completed mixture.
  • the amounts of the HT and BT fractions needed to achieve the desired first and second quantities thereof are computed by using equation 5 to first compute the FFBW based on the amount of the HC fraction. For example, assuming an amount of HC fraction of about 313.3 grams, and plugging in the desired percentages of the HT and BT fractions noted above, equation 5 becomes:
  • the weights of the HT and BT fractions needed to produce the desired final percentages of each by weight in the completed mixture are easily computed by multiplying the FFBW by each desired percentage.
  • the second of the two adding steps comprises adding the second predetermined quantity of benign, flavorless, and inert terpenes (BT fraction) into the mixture of the activated HC and the first predetermined quantity of HT fraction resulting from the first adding step.
  • BT fraction benign, flavorless, and inert terpenes
  • a homogenizing step at step 42 comprises mixing the activated HC fraction, the first predetermined quantity of the HT fraction, and the second predetermined quantity of the BT fraction.
  • the homogenizing step comprises mixing using a stirrer on a hotplate.
  • homogenization of the final formulated solution should be performed at a temperature range of between about 60°C to about 90°C and should be stirred on the hot plate for a time range of between about 15 minutes and about 30 minutes.
  • homogenization of the final formulated solution should be performed at a temperature of about 75°C and should be stirred on the hot plate for a minimum of about 20 minutes.
  • the resultant cannabis oil formulation resulting from the first method described hereinabove for example 1 comprises both a high level of terpene concentration and a full spectrum cannabinoid profile.
  • the first method of example 1 results in detectable levels of as many as four different cannabinoids in addition to a high terpene concentration of at least 4.7% wt (by weight).
  • a second exemplary method for post processing a quantity of raw cannabis oil extract acquired from the extraction process described hereinabove or by any other suitable process as known in the art is described hereinbelow. While the first exemplary method described hereinabove works very well for the post-processing of extracted cannabis oil, as will be seen the second exemplary method has some advantages over the first exemplary method.
  • a first step in the second exemplary method for post processing is an activation step.
  • One advantage of the second exemplary method over the first exemplary method is that the activation step in the second exemplary method is executed within a single pressure rated vessel (PRV) without separation of the HC and HT fractions, and without the need for one or more containers, for example, one or more wide mouth mason jars.
  • Another advantage of the second exemplary method is that the processing time for activation and purging of the oil is reduced from a typical range of between about 9 days to 12 days for the first exemplary method to a typical range of about 5 days for the second exemplary method.
  • the second exemplary method does not include steps for formulation that are included in the first exemplary method. Elimination of the formulation step further reduces the total processing time, and elimination of the separation of the HC and HT fractions eliminates waste of HT fraction that goes unused in the final formulation.
  • the typical yield of oil post processed by the second exemplary method is increased from the typical yield of oil post processed by the first exemplary method (for example, the yield was 3.3% by weight for the second exemplary method vs 2.6% by weight for the first exemplary method, representing a 27% increase in yield).
  • the average level of Terpenes in the oil post processed by the second exemplary method is increased to about 4.1% from an average level of Terpenes of about 3.3% yielded by the first exemplary method, while the average %THC in the post processed oil from both methods remains about the same (decreasing slightly from to 77.4% for the second exemplary method from about 79.5% for the first exemplary method).
  • the second exemplary method requires less actual process steps and far fewer container transfers than the first exemplary method (as will be seen hereinbelow). Fewer process steps and fewer container transfers can mean less losses due to process, losses due to transfer, or even losses due to breakage of the one or more containers utilized in the first exemplary method. Less losses translates to less lost revenues. Further, whereas scaling the first exemplary method up to larger production quantities of oil would require using more and more containers and would be practically far more difficult, the second exemplary method is more easily scalable for processing larger production quantities of oil simply by using a larger pressure rated vessel (PRV).
  • PRV pressure rated vessel
  • the raw cannabis oil is placed into a pressure rated vessel (PRV) that can hold fluids, for example, hydrocarbons under pressure.
  • PRV 100 can be an unjacketed vessel as illustrated in Figure 3 meaning that the primary pressure retaining structure of the PRV has no secondary jacket around it.
  • the PRV can be a jacketed vessel meaning that the primary pressure retaining structure of the PRV is at least partially enclosed within an outer jacket forming a secondary volume within the outer jacket.
  • the secondary volume may comprise a vacuum.
  • the outer jacket may be configured to hold elevated pressures like the primary pressure retaining structure of the PRV.
  • the secondary volume has one or more inlet ports and/or valves and one or more outlet ports and/or valves, thereby allowing the circulation of a secondary fluid through the jacket.
  • the secondary fluid could be used, for example, to provide heating and/or cooling to the PRV.
  • circulation of superheated steam or other heated fluid through the outer volume can heat the contents of the contents of the primary pressure retaining structure of the PRV without placing the PRV into an oven.
  • the raw cannabis oil extract is placed inside the PRV 100 with a third predetermined quantity of liquid Butane. If an insufficient amount of liquid Butane is used, the oil extract/Butane mixture can stick to the inside of the PRV 100 and burn, which is highly undesirable. Therefore, the objective is to use copious amounts of liquid Butane, so as to objectively suspend the raw cannabis oil extract in a liquid Butane solution.
  • the third predetermined quantity of liquid Butane has between about 3 times and about 10 times the volume of the raw cannabis oil extract. In another embodiment the third predetermined quantity of liquid Butane has at least about 5 times the volume of the raw cannabis oil extract.
  • the vessel is sealed shut and heated to a fifth predetermined temperature for a fifth predetermined time to activate the cannabinoids THC or CBD.
  • the activation step is meant to specifically decarboxylate cannabinoids such as CBDA and THCA that are comprised with a carboxyl group.
  • the CBDA is converted into CBD and the THCA is converted into “activated” THC.
  • the PRV 100 is heated in an oven at the fifth predetermined temperature in a range of between about 60°C to about 235°C.
  • the fifth predetermined temperature is in a range of between about 60°C to about 100°C.
  • the fifth predetermined temperature is in a range of between about 60°C to about 75°C, and preferably at about of 68°C.
  • the PRV 100 is heated in an oven at the fifth predetermined temperature for a fifth predetermined time in a range of between about 24 to about 60 hours.
  • the fifth predetermined time is in a range of between about 30 to about 54 hours, and in yet another embodiment the fifth predetermined time is a minimum of about 48 hours.
  • Step 52 includes controlling the level of the internal pressure in the PRV 100 to be at about a predetermined pressure or at least to be maintained within a predetermined range of pressures.
  • the level of the internal pressure in the PRV 100 is controlled by controlling the amount of heat applied to the PRV 100 in combination with controlling the total volume of the raw cannabis oil extract and the liquid Butane disposed inside the PRV 100.
  • the PRV 100 is only partially filled with the raw cannabis oil extract and the liquid Butane.
  • the PRV 100 is filled to about 50% volume capacity with the raw cannabis oil extract and the liquid Butane.
  • the PRV 100 is filled to less than 50% volume capacity, for example to about 40%, about 30%, about 20% volume capacity, or less with the raw cannabis oil extract and the liquid Butane.
  • the PRV 100 is filled to about 60%, about 70%, or about 80% volume capacity with the raw cannabis oil extract and the liquid Butane. As a safety precaution and to allow for operable control of the internal pressure of the PRV 100, the PRV 100 is not filled past about 80% volume capacity with the raw cannabis oil extract and the liquid Butane.
  • step 52 Execution of step 52 with controlled application of heat to a controlled total volume of the raw cannabis oil extract and the liquid Butane as described hereinabove, results, in one embodiment, in a controlled increase in internal pressure of the PRV 100 to a pressure between about 20 psi and about 450 psi above atmospheric pressure.
  • the internal pressure of the PRV 100 is controllably increased to a pressure between about 150 psi and about 350 psi above atmospheric pressure.
  • the internal pressure of the PRV 100 is controllably increased to a pressure between about 150 psi and about 250 psi above atmospheric pressure, and preferably to a pressure of about 200 psi above atmospheric pressure.
  • the controlled application of heat to the PRV 100 to control the temperature and the internal pressure of the PRV 100 may be through application of heat to an unjacketed PRV from an external heat source, or through application of heat to a jacketed PRV using the circulation of a heated secondary fluid through the jacket as described above, or through a combination of heat applied to a jacketed PRV from an external heat source and using the circulation of a heated secondary fluid through the jacket.
  • the PRV 100 is cooled at step 54.
  • the PRV 100 is cooled by placing the PRV 100 on a cold surface, for example, on ice for a brief time, for example about 10 min, and subsequently allowing it to rest at room temperature, for example, for about an additional 15 minutes.
  • the PRV 100 has an internal pressure that can still be above atmospheric pressure.
  • the internal pressure typical of the cooling step described above can be about 110 psi above atmospheric pressure.
  • the PRV 100 is released of its internal pressure at step 56, for example, by opening the valve 110.
  • the PRV 100 is cooled via other sequences of times and temperatures to the point where the PRV 100 is cool enough for safe release of its internal pressure by opening of the valve 110.
  • the contents of the PRV 100, now comprising activated cannabis oil are transferred into another container at step 58 and vacuum oven purged under a third predetermined level of vacuum held steady at a sixth predetermined temperature for a sixth predetermined time.
  • the third predetermined level of vacuum is in a range of between about -25 inches of Hg and about -30 inches of Hg.
  • the third predetermined level of vacuum is about -28 inches of Hg.
  • the sixth predetermined temperature is in a range of between about 35°C and about 50°C.
  • the sixth predetermined temperature is about 48°C.
  • the sixth predetermined time is in a range of between about 48 hours to about 120 hours. In another embodiment the sixth predetermined time is about 72 hours.
  • the resultant cannabis oil formulation resulting from the second method described hereinabove for example 2 comprises both a high level of terpene concentration and a full spectrum cannabinoid profile.
  • the second method of example 2 results in detectable levels of at least 5 different cannabinoids in addition to a high terpene concentration of at least 4.88% wt (by weight).
  • the second method results in an unprecedented amount of terpenes in the cannabis oil when compared to the known conventional methods.
  • the method for post processing cannabis oil can be used by or in industry to produce cannabis oil having a high level of terpenes and/or a full spectrum of cannabinoids.
  • the method comprises placing the oil into a container at a first predetermined temperature for a first predetermined time during which the oil will separate into two parts comprising a high terpene (HT) liquid fraction and a high cannabinoid (HC) crystal fraction.
  • the HT and HC fractions are heated under a first predetermined level of vacuum at a second predetermined temperature for a second predetermined time, and heated to a third predetermined temperature for a third predetermined time.
  • a first predetermined quantity of the HT fraction is added back into the HC fraction to create a first mixture
  • a second predetermined quantity of benign terpenes is added into the first mixture to create a second mixture, which is further mixed to create a finished mixture.

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Abstract

Un procédé de post-traitement d'huile extraite du cannabis comprend les étapes consistant à placer l'huile dans un récipient à une première température prédéterminée pendant un premier temps prédéterminé durant lequel l'huile est séparée en deux parties dont une fraction liquide à teneur en terpène élevée (HT) et une fraction cristalline à teneur en cannabinoïde élevée (HC), à chauffer les fractions HT et HC à un premier niveau prédéterminé de vide à une seconde température prédéterminée pendant un second temps prédéterminé, et à chauffer la fraction HC à une troisième température prédéterminée pendant un troisième temps prédéterminé. Les étapes comprennent en outre l'ajout d'une première quantité prédéterminée de la fraction HT de nouveau dans la fraction HC pour créer un premier mélange, l'ajout d'une seconde quantité prédéterminée de terpènes bénins dans le premier mélange pour créer un second mélange, et le mélange du second mélange pour créer un mélange fini.
PCT/US2019/068720 2019-12-27 2019-12-27 Procédé de post-traitement pour huile de cannabis WO2021133410A1 (fr)

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