Patent Publication Number: US-2021187413-A1

Title: System, method and apparatus for processing organic material

Description:
This application claims priority to and the benefit of U.S. Provisional Patent Application No. 62/953,322, filed Dec. 24, 2019 (having attorney docket number 66370-100), which is incorporated herein by reference in its entirety. 
    
    
     BACKGROUND 
     The disclosed systems, methods and devices generally relate to processing organic material and using fluid extraction techniques to do so. 
     SUMMARY 
     Embodiments of a system, method and apparatus for processing organic material are disclosed. For example, an extraction apparatus can include an extraction vessel configured to receive a process fluid, permit the process fluid to come into contact with a source material within the extraction vessel, permit an extracted material to be removed from the source material, and permit the extracted material and the process fluid to form a mixture. The extraction vessel can include an extraction vessel filter adapted to retain portions of the source material while also allowing the mixture to pass. 
     The extraction apparatus can include a separation chamber. The extraction apparatus also can include a process fluid circulation conduit configured to selectively restrict, allow, and reversibly direct flow of the process fluid into and out of the extraction vessel. In addition, it can permit the mixture to flow from the extraction vessel to the separation chamber. The process fluid circulation conduit can include a separation portion configured to receive the mixture and permit a portion of the extracted material to separate from the mixture within the separation chamber. 
     The extraction apparatus can include a temperature regulator. The temperature regulator can include a temperature regulation fluid and a temperature regulation fluid circulation line. The temperature regulator can be configured to permit re-circulation of the temperature regulation fluid and regulate the temperature of the process fluid. 
     The extraction apparatus can include a back pressure regulator configured to maintain pressure within the separation chamber and vent the process fluid. 
     In some examples, the extraction apparatus can include a heating source configured to heat the process fluid prior to ingress of the process fluid into the extraction vessel. The fluid can be carbon dioxide or other solvents, such as similar solvents. 
     In some examples, the extraction apparatus can include a heat exchanger configured to regulate temperature of the process fluid prior to ingress of the process fluid into the extraction vessel. 
     In some examples, the extraction apparatus can include an extraction vessel temperature regulator. In some examples, the extraction apparatus can include a separation chamber temperature regulator. 
     In some examples, of the extraction apparatus, the process fluid used can be carbon dioxide. In some examples, of the extraction apparatus, the process fluid can be supercritical carbon dioxide. In some examples, of the extraction apparatus, the source material can be a botanical substance. In some examples, of the extraction apparatus, the extracted material can include at least one of a botanical oil and a wax, fats, lipids, chlorophyll, etc., as part of the extracted material. 
     In some examples, of the extraction apparatus, the process fluid circulation conduit can include valves configured to selectively restrict, allow, and reversibly direct flow of the process fluid through the process fluid circulation conduit. In addition to extraction apparatus, embodiments can include filter and separation apparatus such as a loop with valves for the filter and separation apparatus. 
     In some examples, of the extraction apparatus, the extraction vessel can include a first extraction vessel filter and a second extraction vessel filter. In some examples, the extraction apparatus can be configured to permit reversal of a direction of flow of the process fluid through the first extraction vessel filter and the second extraction vessel filter. 
     In some examples, of the extraction apparatus, the separation portion can include an orifice. In some examples, of the extraction apparatus, the separation portion can be orientated to direct the process fluid along an inner wall of the separation chamber in a generally rotational manner. In some examples, of the extraction apparatus, the orifice can be sized to match a flow rate of the process fluid. In some examples a membrane filter can be applied to an additional separator to be used to separate fats, waxes, lipids from desired products. 
     A re-circulating extraction apparatus can include an extraction vessel configured to receive a process fluid, permit the process fluid to come into contact with a source material within the extraction vessel, permit an extracted material to be removed from the source material, and permit the extracted material and the process fluid to form a mixture. The extraction vessel can include a filter adapted to retain portions of the source material while also allowing the mixture to pass. In some examples a separator can be used to separate the process fluid from the desired oil. Some process fluid(s) can be separated via a membrane filter and others can be separated via phase transformation. 
     The re-circulating extraction apparatus can include a separation chamber. The re-circulating extraction apparatus can include an overflow chamber. 
     The re-circulating extraction apparatus can include a process fluid circulation conduit configured to selectively restrict, allow, and reversibly direct flow of the process fluid into and out of the extraction vessel, permit the mixture to flow from the extraction vessel to the separation chamber, permit the process fluid to flow from the separation vessel to the overflow chamber, and permit re-circulation of the process fluid. The process fluid circulation conduit can include a separation portion configured to receive the mixture and permit a portion of the extracted material to separate from the mixture within the separation chamber. 
     The re-circulating extraction apparatus can include a temperature regulator. The temperature regulator can include a temperature regulation fluid and a temperature regulation fluid circulation line. The temperature regulator can be configured to permit re-circulation of the temperature regulation fluid and regulate the temperature of the process fluid. 
     The re-circulating extraction apparatus can include a pump configured to increase or maintain the pressure and/or the flowrate of the process fluid. The filter apparatus can include a pump to deliver crude oil to and from membrane. 
     In some examples, the re-circulating extraction apparatus can include a heating source configured to heat the process fluid prior to ingress of the process fluid into the extraction vessel. 
     In some examples, the re-circulating extraction apparatus can include a heat exchanger configured to regulate temperature of the process fluid prior to ingress of the process fluid into the extraction vessel. 
     In some examples, the re-circulating extraction apparatus can include a regenerative heat exchanger. 
     In some examples, the re-circulating extraction apparatus can include an extraction vessel temperature regulator. In some examples, the re-circulating extraction apparatus can include a separation chamber temperature regulator. In some examples, the re-circulating extraction apparatus can include an overflow chamber temperature regulator. 
     In some examples, of the re-circulating extraction apparatus, the process fluid can include carbon dioxide. In some examples, of the re-circulating extraction apparatus, the process fluid can include supercritical carbon dioxide. In some examples, of the re-circulating extraction apparatus, the source material can include a botanical substance. In some examples, of the re-circulating extraction apparatus, the extracted material can include at least one of a botanical oil and a wax, other solvents, fats, lipids, chlorophyll, etc. 
     In some examples, of the re-circulating extraction apparatus, the process fluid circulation conduit can include valves configured to selectively restrict, allow, and reversibly direct flow of the process fluid through the process fluid circulation conduit. The filter apparatus also can have valves. 
     In some examples, of the re-circulating extraction apparatus, the extraction vessel can include a first extraction vessel filter and a second extraction vessel filter. In some examples, the re-circulating extraction apparatus can be configured to permit reversal of a direction of flow of the process fluid through the first extraction vessel filter and the second extraction vessel filter. 
     In some examples, of the re-circulating extraction apparatus, the separation portion can include an orifice. In some examples, of the re-circulating extraction apparatus, the separation portion can be orientated to direct the process fluid along an inner wall of the separation chamber in a generally rotational manner. In some examples, of the re-circulating extraction apparatus, the orifice can be sized to match a flow rate of the process fluid. In some examples a filter apparatus can be applied. 
     The foregoing and other objects and advantages of these embodiments will be apparent to those of ordinary skill in the art in view of the following detailed description, taken in conjunction with the appended claims and the accompanying drawings. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
       So that the manner in which the features and advantages of the embodiments are attained and can be understood in more detail, a more particular description can be had by reference to the embodiments thereof that are illustrated in the appended drawings. However, the drawings illustrate only some embodiments and therefore are not to be considered limiting in scope as there can be other equally effective embodiments. 
         FIG. 1  is a schematic diagram of an embodiment of an extraction system. 
         FIG. 2  is a perspective view of an embodiment of an extraction system. 
         FIG. 3  is a schematic diagram of another embodiment of an extraction system. 
         FIGS. 4A-4C  are sectional side, top and bottom views, respectively, of an embodiment of an extraction vessel. 
         FIGS. 5A-5C  are sectional side, top and bottom views, respectively, of another embodiment of an extraction vessel. 
         FIGS. 6A-6C  are sectional side, top and bottom views, respectively, of an embodiment of a separation chamber. 
         FIGS. 7A-7C  are sectional side, top and bottom views, respectively, of an embodiment of an overflow chamber. 
         FIG. 8  is a perspective view of still another embodiment of an extraction system. 
         FIG. 9  is a schematic diagram of an embodiment of a membrane filtration system. 
         FIG. 10  is a CO 2  phase diagram that depicts membrane filtration pressures and operating temperatures, for some embodiments. 
         FIG. 11  includes schematic diagrams of embodiments of a processing system. 
         FIG. 12  includes schematic diagrams of embodiments of membrane filtration processing. 
     
    
    
     DETAILED DESCRIPTION 
       FIGS. 1-12  depict various embodiments of a system, method and apparatus for processing organic material. Several examples, of systems configured to perform extraction are disclosed. In each example, the systems can be configured to permit a process fluid to be in contact with a source material, whereby an extracted material is removed from the source material, forming a mixture with the process fluid. 
     In some examples, the process fluid can be carbon dioxide. In some examples, the process fluid can be supercritical carbon dioxide. The process fluid can any other fluid suitable for forming a mixture when placed in contact with the source material. Optionally, certain additives can be included in the process fluid, for example, ethanol. 
     In some examples, the source material can be a botanical substance. In some examples, the extracted material can include at least one of a botanical oil and a wax. In other examples, the source material can be any material in which extraction is desired. For example, the source material could be any physical article such as an instrument, tool, medical device, or implant. By operation of the disclosed systems, manufacturing fluids or other forms of residue can be removed from the surface of the physical article. 
     As shown in  FIG. 1 , an extraction apparatus  100  can include an extraction vessel  110  configured to receive a process fluid, permit the process fluid to come into contact with a source material within the extraction vessel  110 , permit an extracted material to be removed from the source material, and permit the extracted material and the process fluid to form a mixture. 
     In some examples, the extraction vessel  110  can comprise a volume of about one liter, and it can be rated at a maximum pressure of about 1500 pounds per square inch (psi) at about 200 degrees F. Other pressure and temperature ratings can be used. For example, the pressure and temperature ratings can be anything that causes CO 2  to be in subcritical or supercritical fluid phase. Moreover, the extraction vessel  110  can comprise any volume. 
     In some examples, the extraction vessel  110  can have an opening for receiving the process fluid. In some examples, the extraction vessel can have multiple openings for receiving the process fluid. In the example shown in  FIG. 1 , the extraction vessel  110  includes a first extraction vessel opening  111  and a second extraction vessel opening  112 . In some examples, the openings of the extraction vessel can be sealed using an elastomeric O-ring. One example of a suitable elastomeric O-ring is a Buna-90 O-ring. 
     The extraction vessel  110  can include an extraction vessel filter adapted to retain portions of the source material while also allowing the mixture to pass. In some examples, the extraction vessel  110  can have one or more filters. As shown in  FIG. 1 , the extraction vessel  110  can include a first extraction vessel filter  181  located near the first extraction vessel opening  111  and a second extraction vessel filter  182  located near the second extraction vessel opening  112 . 
     The extraction apparatus  100  can include a separation chamber  120 . In some examples, the separation chamber  120  can be rated for about 500 psi at 200° F. In some examples, the filter chamber can be rated for subcritical and/or supercritical CO 2 . Versions of the separation chamber  120  can be designed for any rating that allows for a gaseous phase. 
     The extraction apparatus  100  can include a process fluid circulation conduit  130  configured to selectively restrict, allow, and reversibly direct flow of the process fluid into and out of the extraction vessel  110  and permit the mixture to flow from the extraction vessel  110  to the separation chamber  120 . The process fluid circulation conduit  130  can be stainless steel in some examples. In other examples, the process fluid circulation conduit  130  can be made from one of a family of austenitic nickel-chromium based alloys, such as those supplied commercially under the brand name Inconel by Special Metals Corporation. In other examples, the process fluid circulation conduit  130  can be made from other suitable material for high corrosion resistance. In other examples, the process fluid circulation conduit  130  can be steel or another suitable material for applications with low sanitary requirements. In some examples, the process fluid circulation conduit  130  can be sized about 304 stainless steel (SS) with about ⅜ inches diameter, and a wall thickness of about 0.035 inches. The process fluid circulation conduit  130  can include flexible portions  131 . 
     The process fluid circulation conduit  130  can include one or more valves configured to selectively restrict, allow, and reverse a direction of flow of the process fluid through the process fluid circulation conduit  130  and other portions of the extraction apparatus  100 . In some examples, the valves can be temperature rated from about 22 F to about 356 F. 
     In some examples, the process fluid circulation conduit  130  can be configured with a system of valves to selectively direct an amount of the process fluid to remain within the extraction vessel  110  for a desired time. For example, this can allow the extraction process to be completed to a desired extent. In some versions, the extraction apparatus  100  can be configured with a system of valves to permit reversal of a direction of flow of the process fluid through the extraction vessel  110 . In some examples, the reversal of the direction of flow of the process fluid through the extraction vessel  110  can facilitate cleaning or clearing of the first and second extraction vessel filters  181  and  182  without interrupting ongoing extraction processing. Flushing and/or cleaning membranes can be included. Valves can be used to direct fluid to flush/clean the membranes. Embodiments of the membranes are enabled for back flushing to clean the membrane surfaces. 
     In some examples, the system of valves can include one or more pairs of opposing valves for directing the flow of process fluid. In the example of  FIG. 1 , the first, second, third, fourth, and fifth valves, labeled  132 . 1 ,  132 . 2 ,  132 . 3 ,  132 . 4 , and  132 . 5  respectively, can be positioned along the process fluid circulation conduit  130  as shown. To direct process fluid into the extraction vessel  110  at a first extraction vessel opening  111 , the first valve  132 . 1  can be opened while the second valve  132 . 2  can be closed. To direct the process fluid out of the extraction vessel  110  and further downstream in the system, the second valve  132 . 2  can be opened while the first vale  131 . 1  can be closed. The third valve,  132 . 3 , can be used to decompress the system and vent process fluid out of the system. 
     In the example of  FIG. 1 , the fourth and fifth valves,  132 . 4  and  132 . 5 , can be configured to direct the process fluid into or out of a second extraction vessel opening  113 . Optionally, the valves could be used to direct the process fluid into or out of multiple openings of the extraction vessel  110 . For example, by opening the first valve  132 . 1  and fifth valve  132 . 5  while closing the downstream second valve  132 . 2  and fourth valve  132 . 4 , the process fluid can be directed into the first extraction vessel opening  111  and out of the second extraction vessel opening  112 . By closing the first valve  132 . 1  and fifth valve  132 . 5  while opening the second valve  132 . 2  and fourth valve  132 . 4 , the process fluid can be directed into the second extraction vessel opening  112  and out of the first extraction vessel opening  111 . 
     In the example apparatus depicted in  FIG. 1 , the process fluid can be directed in a first direction of flow such that the process fluid enters the extraction vessel  110  through extraction vessel opening  111 , passing through the extraction vessel filter  181 . According to this direction of flow, the process fluid can pass through an interior portion of the extraction vessel  110  where it can come into contact with the source material, extract the extracted material, and form the mixture. The mixture can then be directed to pass through filter  182  and exit the extraction vessel  110  at opening  112 . Optionally, the valves can be re-configured such that the direction of flow of the process fluid and/or mixture can be reversed, allowing the process fluid and/or mixture to enter the extraction vessel  110  at extraction vessel opening  112 , pass through the extraction vessel filter  182 , pass through filter  181 , and exit at extraction vessel opening  111 . 
     The process fluid circulation conduit  130  can include a separation portion  134  configured to receive the mixture and permit a portion of the extracted material to separate from the mixture within the separation chamber  120 . In some examples, the separation portion  134  can allow the process fluid to decompress in the separation chamber  120  and separate the extracted material from the process fluid without the use of a valve or regulator for separation. 
     In some examples, the separation portion  134  can include an orifice. The orifice can be sized to match a flow rate of the process fluid. In some examples, the orifice can be about 0.010 inches in diameter. In some examples, the orifice can restrict the flow of process fluid, allowing a significant pressure drop in the mixture after passing through the orifice and allowing the process fluid to change from a subcritical or supercritical state to a gaseous state, thereby allowing the extracted material to fall out, or separate, from the process fluid. 
     In some examples, the separation portion  134  can be positioned near an inner wall of the separation chamber  120 . In some examples, the separation portion  134  can be orientated to direct the process fluid along the inner wall of the separation chamber  120  in a generally rotational manner. In some examples, a portion of process fluid circulation conduit  130  leading to the separation portion  134  can be angled at an appropriate angle, which can be about 45 degrees. In some examples, the inner wall of the separation chamber  120  can be relatively warmer than an interior portion of the separation chamber  120 . In some examples, directing the process fluid along the inner wall of the separation chamber  120  in a generally rotational manner can help to keep the process fluid in a gaseous state after the process fluid is depressurized in the separation chamber  120 . In such examples, the relatively warmer inner wall can help to counteract the Joule-Thompson cooling effect that can occur when the process fluid decompresses. 
     In some examples, a separation process can be executed via a membrane filter. 
     In some examples, the extraction apparatus  100  can be configured to receive the process fluid from a process fluid storage container  105 , which can be a cylinder or any other storage device capable of holding the process fluid. 
     An initial state of the process fluid in the process fluid storage container  105  can be solid, liquid, gaseous, or supercritical. Where the process fluid is in an initial liquid state, a siphon can be optionally used to remove the process fluid from a top opening of the process fluid storage container while maintaining consistent pressure. Alternatively, the liquid process fluid can be removed by inverting the process fluid storage container  105  such that the opening is on the bottom. 
     In some examples, the extraction apparatus  110  can include a heating source  107  configured to heat the process fluid prior to ingress of the process fluid into the extraction vessel  110 . In some examples, heating source  107  can heat the process fluid within the process fluid storage container  105 . The heating source  107  can be a heating blanket, electric band heater, induction heater, coiled tubing with heating fluid in intimate contact, or an open flame. 
     In some examples, as the process fluid is heated by the heating source  107 , a temperature and the internal pressure of the process fluid rises. In this way, a desired pressure for the process fluid in the system can be achieved without the need for a pump. If necessary, the heating source  107  can deliver continuous or recurring heat to the process fluid so as to maintain the pressure within the system. 
     Optionally, the temperature and internal pressure of the process fluid can be increased to the point of allowing a phase transformation of the process fluid. Optionally, this phase transformation can occur within the process fluid storage container  105 . When the initial state of the process fluid is liquid or gas, increasing the temperature and pressure above the fluid&#39;s critical point can allow a phase change to a supercritical state. For example, heating carbon dioxide above about 87 F at a pressure above about 1083 psi will result in a phase change to a supercritical state. 
     The extraction apparatus  100  can include a temperature regulator. The temperature regulator can include a temperature regulation fluid and a temperature regulation fluid circulation line  142 . In the example shown in  FIG. 1 , the temperature regulator can include a chiller/heater  144  with temperature regulation fluid circulation line  142  running through the extraction apparatus  100  to regulate temperature of the process fluid. 
     The temperature regulator can be configured to permit re-circulation of the temperature regulation fluid. The temperature regulation fluid circulation line  142  can run in close proximity to the process fluid circulation conduit  142 . In some examples, the circulation line can form a coil around the temperature regulation fluid circulation line  142 . 
     In some examples, the temperature regulation fluid can be liquid water, steam or another heating/cooling fluid. In some examples, the temperature regulation fluid can include distilled water. In some examples, the temperature regulation fluid can be a mixture, for example, a mixture of about 50% water and about 50% glycol. 
     The temperature regulator can be configured to raise, lower, or maintain the temperature of the process fluid prior to introduction into the extraction vessel  110  to achieve a desired temperature. In some examples, the temperature regulator can be configured to optionally cause a phase change in the process fluid prior to entering the extraction vessel  110 . 
     In some examples, temperature regulator can include a heat exchanger  146  configured to regulate temperature of the process fluid prior to ingress of the process fluid into the extraction vessel  110 . In some examples, the heat exchanger  146  can be a tube-in-tube configuration, allowing the process fluid to be in close physical proximity to the temperature regulation fluid, thereby allowing for the exchange of heat between the two fluids while maintaining their separation from one another. Alternative configurations of the heat exchanger  146  could include a shell and tube design, a coil design, or any other method of heat exchange. 
     In some examples, the temperature regulator can be configured to regulate the temperature of the process fluid within the extraction vessel  110 . In some versions, the temperature regulator can be configured to regulate the temperature of the process fluid within the separation chamber  120 . As shown in the example of  FIG. 1 , the extraction apparatus  100  can include an extraction vessel temperature regulator  116  and a separation chamber temperature regulator  126 . As shown in this example, the temperature regulation fluid circulation line  142  can extend to the extraction vessel temperature regulator  116  and the separation chamber temperature regulator  126 . In the example shown in  FIG. 1 , the system can be configured to permit the temperature regulation fluid to flow through the temperature regulation fluid circulation line  142 , through the extraction vessel temperature regulator  116 , through the temperature regulation fluid circulation line  142 , through the separation chamber temperature regulator  126 , and through the temperature regulation fluid circulation line  142 . In some examples, the extraction vessel temperature regulator  116  can be a heating/cooling jacket surrounding an exterior portion of extraction vessel  110 . In some examples, the separation chamber temperature regulator  126  can be a heating/cooling jacket surrounding an exterior portion of separation chamber  120 . In some embodiments, the filtration vessel  310  can have a temperature regulator that can be a heating/cooling jacket surrounding an exterior portion of the filtration vessel  310 . 
     In some examples, the temperature regulator can regulate the temperature of the process fluid in other portions of the process fluid circulation conduit  130 . In one example, a portion of the process fluid circulation conduit  130  connecting the extraction vessel  110  with the separation chamber  120  could run in close proximity to the temperature regulation fluid circulation line  142 . Alternative configurations could include a shell and tube design, a coil design, or any other method of heat exchange. Any other portion of the process fluid circulation conduit  130  could be regulated in the same ways. 
     In some examples, the extraction apparatus  100  can include a back pressure regulator  135  configured to maintain pressure within the separation chamber  120  and vent the process fluid. In some examples, the backpressure regulator  135  can be located at a discharge opening of the separation chamber  120 . 
     In some examples, a collection cup  122  can be used to capture the extracted material after separation from the process fluid in the separation chamber  120 . 
     In other examples, a valve, such as the sixth valve  132 . 6  shown in  FIG. 1 , can be used to direct the extracted material out of the separation chamber  120  after separation from the process fluid. Optionally, the extracted material can be directed out of the separation chamber  120  while the separation chamber  120  remains under pressure. 
     As shown in  FIG. 1 , the extraction apparatus  100  can include one or more pressure gauges  171 . As shown in  FIG. 1 , the extraction apparatus  100  can include one or more relief valves  133 . As shown in  FIG. 1 , the extraction apparatus  100  can include one or more relief valves  133 . 
     In the example shown in  FIG. 2 , some of the described aspects of the extraction apparatus  100  are shown mounted on a frame  160  in an exemplary arrangement. 
     As shown in  FIG. 3 , a re-circulating extraction apparatus  200  can include an extraction vessel  210  configured to receive a process fluid, permit the process fluid to come into contact with a source material within the extraction vessel  210 , permit an extracted material to be removed from the source material, and permit the extracted material and the process fluid to form a mixture. 
     In some examples, the extraction vessel  210  can have an opening for receiving the process fluid. In some examples, the extraction vessel can have multiple openings for receiving the process fluid. In the example shown in  FIG. 3 , the extraction vessel  210  includes a first extraction vessel opening  211  and a second extraction vessel opening  212 . In some examples, the openings of the extraction vessel can be sealed using an appropriate O-ring, such as an elastomeric O-ring. One example of a suitable elastomeric O-ring can be a Buna-90 O-ring. 
     The extraction vessel  210  can include an extraction vessel filter adapted to retain portions of the source material while also allowing the mixture to pass. In some examples, the extraction vessel  210  can have a multiple filters. As shown in  FIG. 3 , the extraction vessel  210  can include a first extraction vessel filter  281  located near the first extraction vessel opening  211  and a second extraction vessel filter  282  located near the second extraction vessel opening  212 . 
     In the example shown in  FIGS. 4A, 4B, and 4C , the extraction vessel  210  can include an interior portion sounded by an extraction vessel temperature regulator  216 , with a first flange  213  and a second flange  214 . As also shown in  FIG. 4A , O-rings  218  can be used to seal the first and second flanges  213  and  214  of the extraction vessel  210 . As also shown in  FIG. 4A , the first and second extraction vessel filters  281  and  282  can be located near the first and second extraction vessel openings  211  and  212  respectively. 
     As shown in  FIG. 4B , the first flange  213  can have one or more openings, which may include the first extraction vessel opening  211 . As shown in  FIG. 4C , the second flange  214  can have one or more openings, which may include the second extraction vessel opening  212 . In some examples, the top and bottom flanges can be secured with bolts  217 . In some examples, the volume of the extraction vessel  210  can be about 20 liters, and it can be rated to a maximum pressure of about 1500 psi at about 200° F. In other examples, the extraction vessel  210  can have a volume of about 5 liters, and it can be rated to a maximum pressure of about 1500 psi at about 200° F.  FIGS. 5A, 5B, and 5C  show another example configuration of extraction vessel  210 , top flange  213 , and bottom flange  214 . In some embodiments, the vessel openings can be any design that can meet the required temperature and pressure parameters to induce a subcritical or supercritical phase. 
     The re-circulating extraction apparatus  200  can include a separation chamber  220 . As shown in  FIG. 6A , the separation chamber  220  can have an interior portion, surrounded by a separation chamber temperature regulator  226 . As shown in  FIGS. 6B and 6C , the separation chamber  220  can have a first cap  223  and a second cap  224 . In some examples, the separation chamber  220  can be rated for about 500 psi at about 200 F. In some examples, the pressure and temperature can be in super and/or subcritical ranges. 
     The re-circulating extraction apparatus  200  can include an overflow chamber  250 . As shown in  FIG. 7A , the overflow chamber  250  can have an interior portion, surrounded by an overflow temperature regulator  256 . As shown in  FIGS. 7B and 7C , the overflow chamber  250  can have a first cap  253  and a second cap  254 . In some examples, the overflow chamber  250  can be rated for about 500 psi at 200 F. 
     The re-circulating extraction apparatus  200  can include a process fluid circulation conduit  230  configured to selectively restrict, allow, and reversibly direct flow of the process fluid into and out of the extraction vessel  210 . The process fluid circulation conduit  230  can also be configured to permit the mixture to flow from the extraction vessel  210  to the separation chamber  220 . The process fluid circulation conduit  230  can also be configured to permit the process fluid to be re-circulated through the extraction vessel  210 , separation chamber  220 , and overflow chamber  250 . 
     The process fluid circulation conduit  230  can be stainless steel in some examples. In other examples, the process fluid circulation conduit  230  can be made from one of a family of austenitic nickel-chromium based alloys, such as those supplied commercially under the brand name Inconel by Special Metals Corporation. In other examples, the process fluid circulation conduit  230  can be made from and other suitable material for high corrosion resistance. In other examples, the process fluid circulation conduit  230  can be steel or another suitable material for applications with low sanitary requirements. In some examples, the process fluid circulation conduit  230  can be sized about 304 stainless steel (SS) with about ⅜ inches diameter, and a wall thickness of about 0.035 inches. The process fluid circulation conduit  230  can include flexible portions  231 . 
     In some examples, a pump  290  can be configured to create a desired pressure and to help circulate the process fluid through the system and to recover the process fluid for re-circulation. Any type of pump suitable for use with the chosen process fluid could be used, including pumps of varying configurations and which can use particular liquids or gases and be air driven or electrically driven. In some examples, the pump  290  can be an air driven gas booster. In some examples, the pump  290  may operate with a pump fluid, which may be air or any other suitable fluid. 
     In some examples, the pump  290  may circulate the pump fluid through a pump fluid circulation line  292 . As shown in the example of  FIG. 3 , the pump fluid circulation line  292  can be configured with one or more valves, such as solenoid valves  235 . 1 ,  235 . 2 ,  235 . 3 , and safety valve  238 . As also shown in  FIG. 3 , the pump fluid circulation line  292  can be configured with one or more filters, such as pump fluid intake filter  283 . 
     The process fluid circulation conduit  230  can include one or more valves configured to selectively restrict, allow, and reverse a direction of flow of the process fluid through the process fluid circulation conduit  230  and other portions of the re-circulating extraction apparatus  200 . In one example arrangement shown in  FIG. 3 , the system of valves can include thirteen valves, labeled  232 . 1 ,  232 . 2 ,  232 . 3 ,  232 . 4 ,  232 . 5 ,  232 . 6 ,  232 . 7 ,  232 . 8 ,  232 . 9 ,  232 . 10 ,  232 . 11 ,  232 . 12 ,  232 . 13 , configured to selectively restrict, allow, and reverse a direction of flow of the process fluid through the process fluid circulation conduit  230  and other portions of the re-circulating extraction apparatus  200 . In some examples, the valves can be rated from about −22 degrees F. to about 356 degrees F. 
     In some examples, the process fluid circulation conduit  230  can be configured with a system of valves to selectively direct the process fluid to flow within the extraction vessel  210  for a desired time, for example, to allow the extraction process to be completed to a desired extent. In some examples, the re-circulating extraction apparatus  200  can be configured with a system of valves to permit reversal of a direction of flow of the process fluid through the extraction vessel  210 . In some examples, the reversal of the direction of flow of the process fluid through the extraction vessel  210  can facilitate cleaning or clearing of first and second extraction vessel filters  281  and  282  without interrupting ongoing extraction processing. In some examples, the system of valves can include one or more pairs of opposing valves for directing the flow of process fluid. 
     In the example apparatus depicted in  FIG. 3 , the process fluid can be directed in a first direction of flow such that the process fluid enters the extraction vessel  210  through extraction vessel opening  211 , passing through extraction vessel filter  212 . According to this direct direction of flow, the process fluid can pass through an interior portion of the extraction vessel  210  where it can come into contact with the source material, extract the extracted material, and form the mixture. The mixture can then be directed to exit the extraction vessel  210  at opening  213  and passing through filter  214 . Optionally, the valves can be re-configured such that the direction of flow of the process fluid and/or mixture to be reversed, causing the process fluid and/or mixture to enter the extraction vessel  210  at extraction vessel opening  213 , pass through extraction vessel filter  214 , exit opening  211  and pass through filter  212 . 
     As shown in  FIG. 3 , the re-circulating extraction apparatus  200  can include one or more relief valves  237  to selectively allow the depressurization of fluid at one or more locations within the re-circulating extraction apparatus  200 . As shown in  FIG. 3 , the re-circulating extraction apparatus  200  can include one or more regulating valves  236 . As shown in  FIG. 3 , the re-circulating extraction apparatus  200  can include one or more solenoid valves  235 . The apparatus can be configured to redirect flow to flush membrane. 
     The process fluid circulation conduit  230  can include a separation portion  234  configured to receive the mixture and permit a portion of the extracted material to separate from the mixture within the separation chamber  220 . In some examples, the separation portion  234  can allow the process fluid to decompress in the separation chamber  220  and separate the extracted material from the process fluid without the use of a valve or regulator for separation. 
     In some examples, the separation portion  234  can include an orifice. The orifice can be sized to match a flow rate of the process fluid. In some examples, the orifice can be about 0.010 inches in diameter. In some examples, the orifice can restrict the flow of process fluid, allowing a significant pressure drop in the mixture after passing through the orifice and allowing the process fluid to change from a subcritical or supercritical state to a gaseous state, thereby allowing the extracted material to fall out, or separate, from the process fluid. 
     In some examples, the separation portion  234  can be positioned near an inner wall of the separation chamber  220 . In some examples, the separation portion  234  can be orientated to direct the process fluid along the inner wall of the separation chamber  220  in a generally rotational manner. In some examples, a portion of process fluid circulation conduit  230  leading to the separation portion  234  can be angled at an appropriate angle, which can be about 45 degrees. In some examples, the inner wall of the separation chamber  220  can be relatively warmer than an interior portion of the separation chamber  220 . In some examples, directing the process fluid along the inner wall of the separation chamber  220  in a generally rotational manner can help to keep the process fluid in a gaseous state after the process fluid is depressurized in the separation chamber  220 . In such examples, the relatively warmer inner wall can help to counteract the Joule-Thompson cooling effect that can occur when the process fluid decompresses. Membrane filtration can be used for separation. 
     In some examples, the re-circulating extraction apparatus  200  can be configured to receive the process fluid from a process fluid storage container  205 , which can be a cylinder or any other storage device capable of holding the process fluid. 
     In some examples, the extraction apparatus  210  can include a heating source  207  configured to heat the process fluid prior to ingress of the process fluid into the extraction vessel  210 . In some examples, heating source  207  can heat the process fluid within a process fluid storage container  205 . The heating source can be a heating blanket, electric band heater, induction heater, coiled tubing with heating fluid in intimate contact, or an open flame. 
     In some examples, as the process fluid can be heated by the heating source  207 , a temperature and the internal pressure of the process fluid rises. If necessary, the heating source  207  can deliver continuous or recurring heat to the process fluid so as to help maintain the pressure within the system. 
     Optionally, the temperature and internal pressure of the process fluid can be increased to the point of causing a phase transformation of the process fluid. Optionally, this phase transformation can occur within the process fluid storage container  205 . When the initial state of the process fluid is liquid or gas, increasing the temperature and pressure above the fluid&#39;s critical point will cause a phase change to a supercritical state. For example, heating carbon dioxide above about 87° F. at a pressure above about 1083 psi can result in a phase change to a supercritical state. 
     The initial state of the process fluid in the process fluid storage container  205  can be solid, liquid, gaseous, or supercritical. Where the process fluid is in an initial liquid state, a siphon can be optionally used to remove the process fluid from a top opening of the process fluid storage container while maintaining consistent pressure. Alternatively, the liquid process fluid can be removed by inverting the process fluid storage container  205  such that the opening is on the bottom. 
     The re-circulating extraction apparatus  200  can include a temperature regulator. The temperature regulator can include a temperature regulation fluid and a temperature regulation fluid circulation line  242 . In the example shown in  FIG. 3 , the temperature regulator can include a chiller/heater  244  with temperature regulation fluid circulation line  242  running through the re-circulating extraction apparatus  200  to regulate temperature of the process fluid in various locations of the re-circulating extraction apparatus  200 . 
     The temperature regulator can be configured to permit re-circulation of the temperature regulation fluid. In some examples, the temperature regulation fluid can be liquid water, steam or another other heating/cooling fluids. The temperature regulation fluid circulation line  242  can run in close proximity to the process fluid circulation conduit  242 . In some examples, the circulation line can form a coil around the temperature regulation fluid circulation line  242 . 
     The temperature regulator can be configured to raise, lower, or maintain the temperature of the process fluid prior to introduction into the extraction vessel  210  to achieve a desired temperature. In some examples, the temperature regulator can be configured to optionally cause a phase change in the process fluid prior to entering the extraction vessel  210 . 
     As shown in the example of  FIG. 3 , the temperature regulator can include a heat exchanger  246  configured to regulate temperature of the process fluid prior to ingress of the process fluid into the extraction vessel  210 . In some examples, the heat exchanger  246  can be a tube-in-tube configuration, allowing the process fluid to be in close physical proximity to the temperature regulation fluid, thereby allowing for the exchange of heat between the two fluids while maintaining their separation from one another. Alternative configurations of the heat exchanger  246  could include a shell and tube design, a coil design, or any other method of heat exchange. 
     In some examples, a regenerative heat exchanger can be configured to help regulate the temperature of process fluid at the beginning and the end of the closed-loop re-circulating system. In some examples, the regenerative heat exchanger can use heat generated from the compression of process fluid by the pump at the beginning of the cycle to offset Joule-Thompson cooling that can occur when the process fluid decompresses in the separation chamber. 
     In the example shown in  FIG. 3 , a regenerative heat exchanger  248  comprises two portions of the process fluid circulation conduit  230  running in close proximity to one another to transfer heat from a relatively warm portion of the process fluid circulation conduit  230  to a relatively cool portion of the process fluid circulation conduit  230 . In some examples, the regenerative heat exchanger  248  can be a tube-in-tube configuration, allowing a relatively warm portion of the process fluid to be in close physical proximity to a relatively cool portion of the process fluid, thereby allowing for the exchange of heat between the two portions while maintaining their separation from one another. Alternative configurations of the heat exchanger  248  could include a shell and tube design, a coil design, or any other method of heat exchange. 
     In some examples, the temperature regulator can be configured to regulate the temperature of the process fluid within the extraction vessel  210 . In some examples, temperature regulator can be configured to regulate the temperature of the process fluid within the separation chamber  220 . As shown in the example of  FIG. 3 , the re-circulating extraction apparatus  200  can include an extraction vessel temperature regulator  216 , a separation chamber temperature regulator  226 , and an overflow chamber temperature regulator  256 . As shown in this example, the temperature regulation fluid circulation line  242  can extend to the extraction vessel temperature regulator  216 , the separation chamber temperature regulator  226 , and the overflow chamber temperature regulator  256  and allow the temperature regulation fluid to flow through each of these components. In some examples, the temperature regulators  216 ,  226 , and  256  can be a heating/cooling jacket. Alternative configurations could include a shell and tube design, a coil design, or any other method of heat exchange. 
     In some examples, the temperature regulator can regulate the temperature of the process fluid in other portions of the process fluid circulation conduit  230 . In one example, a portion of the process fluid circulation conduit  230  connecting the extraction vessel  210  with the separation chamber  220  could run in close proximity to the temperature regulation fluid circulation line  242 . Alternative configurations could include a shell and tube design, a coil design, or any other method of heat exchange. Any other portion of the process fluid circulation conduit  230  could be regulated in the same ways. 
     In some examples, a collection cup  222  can be used to capture the extracted material after separation from the process fluid in the separation chamber  220 . 
     In other examples, a valve, such valve  232 . 9  shown in  FIG. 3 , can be used to direct the extracted material out of the separation chamber  220  after separation from the process fluid while the separation chamber  220  remains under pressure. In some examples valves and a pump can be used to direct the extracted material into a separation chamber utilizing a membrane filter. 
     As shown in  FIG. 3 , the re-circulating extraction apparatus  200  can include one or more pressure gauges  271  to indicate a pressure of fluid at one or more locations within the re-circulating extraction apparatus  200 . As shown in  FIG. 3 , the re-circulating extraction apparatus  200  can include one or pressure transducers  272  to sense a pressure of fluid at one or more locations within the re-circulating extraction apparatus  200 . As shown in  FIG. 3 , the re-circulating extraction apparatus  200  can include one or more thermocouples  273  to sense a temperature of fluid at one or more locations within the re-circulating extraction apparatus  200 . 
     In the example shown in  FIG. 8 , some of the described aspects of the re-circulating extraction apparatus  200  are shown mounted on a frame  260  in an exemplary arrangement. In some examples, a system scale  262  can be incorporated into the apparatus  200  below the frame  260 . 
     In some examples, the extraction apparatus  100  and re-circulating extraction apparatus  200  can display system parameters such as temperature, pressure, and time. In some examples, the extraction apparatus  100  and re-circulating extraction apparatus  200  can receive data on system parameters from one more sensors. For example, in the apparatus shown in  FIG. 1 , pressure can be displayed on pressure gauges  171 . Optionally, pressure and other system parameters can be displayed on an electronic control panel or other suitable display mechanism. In the example shown in  FIG. 3 , a control panel could display pressure data received from sensor such as pressure gauges  271  and pressure transducers  272 . The control panel could also display temperature data received from sensor such as thermocouples  173 . 
     In some examples, the filtration apparatus  300  can display system parameters such as temperature, pressure, and time. In some examples, the filtration apparatus  300  can receive data on system parameters from one or more sensors. For example, the apparatus shown in  FIG. 9 , pressure can be displayed on pressure gauges  371 . Optionally, pressure and other system parameters can be displayed on an electronic control panel or other suitable display mechanism. In the example shown in  FIG. 3 , a control panel could display pressure data received from sensor such as pressure gauges  271  and pressure transducers  272 . The control panel could also display temperature data received from sensor such as thermocouple  173  and  373 . 
     In some examples, various aspects of the operation of the extraction apparatus  100  and re-circulating extraction apparatus  200  can be automated with a control system. The control system can include electronic components and mechanical components. In some examples, the control system can be configured to automate the operation of the system based upon data supplied by sensors or based upon the lapse of time. For example, in the device shown in  FIG. 3 , the control system could be configured to turn on or off the chiller/heater  244  or the pump  290 , in response to data supplied by the sensors or the lapse of time. The system could also be configured to implement certain other logical operations helpful in system operation. For example, the control system can be configured to run certain operations for a certain elapsed period of time or based upon certain data received from sensors and thereafter perform a desired function or set of functions, such as open or close certain valves. In the example of  FIG. 3 , the control system could be configured to open or close any of valves  232 . 1  through  232 . 13 , any of the relief valves  233 , any of the solenoid valves  135 , any of the regulating valves  136 , and any of the safety valves  138 . For example, in the device shown in  FIG. 9 , the control system could be configured to control feed, retentate, and permeate pressures. Control of these pressures lead to the control of the transmembrane pressure of the membrane filter. In the example of  FIG. 9 , the control system could be configured to open or close any of valves  332 . 2  through  332 . 6 . 
     In the example shown in  FIG. 8 , the apparatus  200  can have a control box  295  that can include either or both of the control panel and control system. The control box could be electrically connected to the various sensors and system components of the apparatus  200 . 
     Examples, of methods of operating the system disclosed in  FIG. 3  will now be disclosed. As an initial state, the system can be confirmed to be clean. 
     The extraction vessel  210  can be opened with the following steps. Close valves  232 . 1  and  232 . 2 . Open valves  232 . 3  and  232 . 4 . Remove bolts on the top of the extraction vessel  210 , for example using a 1.5″ impact socket and impact wrench. Lift the flange and allow it to rest in the open position on the stops. 
     The extraction vessel  210  can be loaded with source material, optionally with a funnel to avoid spillage. The source material can be prepared in a desired fashion. For example, the source material could be ground, gently compressed, or otherwise prepared. The system scale  262  can be used to weigh the amount of source material loaded. 
     Once the desired amount of source material is loaded, the extraction vessel can be closed and sealed. In some examples, the sealing surfaces can be checked to be clean and generally free of debris. In some examples, O-rings can be inspected for any visible damage or defects and replaced as necessary. In some examples, the O-rings do not require lubrication. In some examples, an extraction vessel flanges  213  and  214  can be closed and closure bolts  217  installed. 
     The filtration vessel  310  can be opened before, during, or after a run. To open the filtration vessel during a run, open valve  332 . 1  and close valve  332 . 2  through  332 . 4 . Open valve  332 . 6 . Remove bolts on the ends of the filtration vessel  310 . Remove the clamping mechanism and remove the vessel cap. To open the filtration vessel before or after a run, remove bolts on the ends of the filtration vessel  310 . Remove the clamping mechanism and remove the vessel cap. 
     The filtration vessel  310  can be loaded or unloaded with one or more membrane filters. In some examples ceramic membranes can installed or removed. In some examples polymer membranes can be installed or removed. Membranes are installed or removed from either end of the filtration vessel  310 . Membrane filters can be sealed within the filtration vessel  310  on one end or both ends depending on the membrane design. If the membrane filter has a seal on one end, the seal should be orientated to allow for permeate and retentate to flow to the fluid permeate line  350  and the fluid retentate line  340  respectively. 
     Once the desired membrane is installed, the filtration vessel can be closed and sealed. In some examples, the sealing surfaces can be checked to be clean and generally free of debris. In some examples, O-rings can be inspected for any visible damage or defects and replaced as necessary. In some examples, the O-rings do not require lubrication. In some examples, a filtration vessel flange can be closed and closure bolts installed. 
     The re-circulating extraction apparatus  200  can be evaluated for moisture or other fluids. The following valves can be opened:  232 . 1 ,  232 . 2 ,  232 . 3 ,  232 . 5 ,  232 . 10 ,  232 . 11 ,  232 . 12 , and  232 . 13 . A pump can be connected to valve  232 . 10  and the system pumped down to a desired pressure, for example 20-25 in Hg. This pressure can be held for several minutes to ensure no gross leaks and to remove moisture. All valves can be closed and the pump disconnected from valve  232 . 10 . 
     Process fluid can be filled according to the following steps. Tare the scale by pushing a “tare/reset” key. Open a valve on the process fluid storage container  205 . Open valves  232 . 1 ,  232 . 3 ,  232 . 5 , and  232 . 7 . Pressurize and fill extraction vessel  210  by slowly opening valve  232 . 13 . Extraction vessel  210  can be pressurized from both top and bottom. Allow extraction vessel  210  pressure to equalize with the pressure in the process fluid storage container  205 . Shut valves  232 . 5  and  232 . 13 . Pressurize the separation chamber  220  and overflow chamber  250  to 300 psi by opening valve  232 . 12  and throttling valve  232 . 11 . Close valve  232 . 11  when pressure in the separation chamber  220  and overflow chamber  250  is approximately 300 psi. Increase extraction vessel  210  pressure by turning the switch to “START” on control panel. Once extraction vessel  210  pressure has reached desired pressure, open valve  232 . 6 . Shut valve  232 . 12 . Open valve  232 . 11 . Allow system to stabilize for approximately 5 minutes. 
     At this stage in the example method, the system can be now circulating process fluid  210  and extracting. It may be necessary to adjust the amount of process fluid  210  in the system to maintain a desired extraction pressure. To increase pressure in the extraction vessel  201 , the following steps can be performed. Shut valve  232 . 11 . Open valve  232 . 12  until extraction vessel  210  reaches the desired pressure or the separation chamber  220  or overflow chamber  250  reach 450 psi. Shut valve  232 . 12 . Open valve  232 . 11 . Allow the system to stabilize, and repeat as necessary. To decrease pressure in the extraction vessel  210 , the following steps can be performed. Shut one of valves  232 . 1  and  232 . 5  (only one of them will be open). Throttle valve  232 . 13  and allow the extraction vessel pressure to decrease to a desired level. Shut valve  232 . 13 . Open one of valves  232 . 1  or  232 . 5  (whichever was previously opened). 
     In the example shown in  FIG. 3 , the process fluid  210  can flow through the process fluid circulation conduit  230  according to the following path: (1) out of the left side of the pump  290 , (2) down to the regenerative heat exchanger  248 , (3) up and over to the heat exchanger  246 , (4) through the extraction chamber  210 , (5) through the safety valve  238 , (6) through the separation portion  234  within in the separator chamber  220 , (7) to the regenerative heat exchanger  248 , (8) through the overflow chamber  250 , (9) through filters  284  and  285 , and (10) back up to the pump  290 . 
     In the example shown in  FIG. 3 , the temperature regulation fluid can flow through the temperature regulation fluid circulation line according to the following path: (1) out of the chiller/heater  244 , (2) through the temperature heat exchanger  246 , (3) through the extraction vessel temperature regulator  216 , (4) through the separation chamber temperature regulator  226 , (5) through the overflow chamber temperature regulator  226 , and (6) back up to the chiller/heater  244 . 
     Multiple separate temperature regulation fluid circulation lines (e.g., chillers/heaters) can be implemented. One line can take the following path: (1) out of the chiller/heater  244 , (2) through the temperature heat exchanger  246 , (3) through the extraction vessel temperature regulator  216 , and either (4) through the filtration vessel temperature regulator and then to (4) back to the chiller/heater  244  or directly (4) back to the chiller/heater. A second line can take the following path: (1) out of an additional chiller/heater  244 , (2) through the regenerative heat exchanger  248 , (3) through the separation chamber temperature regulator  226 , (4) through the overflow chamber temperature regulator  226 , and (6) back up to the chiller/heater  244 . 
     In some examples, a control system can be equipped with a timer that will automatically shut down the system after a set amount of time has elapsed. The timer can be adjusted at any time during the extraction. Actual time elapsed can be displayed. 
     In some examples, a flow of the process fluid within in the extraction vessel  210  can be reversed during operation. For example, to back flush a clogged filter, to prevent channeling through the source material, or both. In some examples, one or more of the extraction vessel filters  281  or  282  can be back-flushed when a differential pressure greater than 300 psi exists between the extraction vessel  210  pressure and either the pressure at either of the extraction vessel openings  211  or  212 . 
     According to some examples, a first direction of flow through the extraction vessel  210  can be reversed according to the following steps. Open valve  232 . 5 . Open valve  232 . 2 . Shut valve  232 . 1 . Shut valve  232 . 6 . 
     According to some examples, following a first reversal of direction of the process fluid, a second direction of flow through the extraction vessel  210  can be reversed according to the following steps. Open valve  232 . 1 . Open valve  232 . 6 . Shut valve  232 . 5 . Shut valve  232 . 2 . 
     According to some examples, the separation portion  234  may include an orifice and an orifice filter. The orifice and orifice filter can be unclogged according to the following steps. Shut valve  232 . 2  and valve  232 . 6  (only one of them will be open). Allow the pump  290  to draw the process fluid out of the separation chamber  220  and overflow chamber  250  and transfer the process fluid to the extraction vessel  210 . Optionally, a portion of the process fluid can be transferred back to the process fluid storage container  205  by shutting valves  232 . 1  and  232 . 5 , throttling valve  232 . 14  to direct pump output to the process fluid storage container, then shutting valve  232 . 13  and re-opening valve  1  or  5 . 
     Continuing with the example method for unclogging an orifice and orifice filter, when the separation chamber  220  and overflow chamber  250  reach approximately 70 psi, the pump can be configured to automatically turn off. Shut valve  232 . 11 . Open valve  232 . 10  to relieve any residual pressure in the separation chamber  220  and overflow chamber  250 . Remove the separation chamber top flange  213 . Remove the orifice and orifice filter. Clean the orifice and the orifice filter by soaking them in acetone or methanol and blowing them out with compressed air. Verify the orifice is clear by looking through it. 
     Continuing with the example method for unclogging the orifice and orifice filter, after cleaning the orifice and orifice filter, reassemble the orifice and filter using the provided Teflon tape. Use caution to prevent excess Teflon tape from getting into the orifice. Tighten the orifice assembly such that the orifice points toward the separation vessel inner wall. Replace the separation vessel top flange  213  and tighten the clamp bolts  217  to about 20 ft-lbs. Close valve  232 . 10 . Open valve  232 . 12 . Pressurize separation vessel  220  and overflow chamber  250  to about 300 psi by opening valve  12  and throttling valve  232 . 11 . Close valve  232 . 11  when separator pressure is approximately 300 psi. In some examples, the pump can be configured to automatically re-start when separator vessel pressure is above about 70 psi. Open valve  232 . 2  or valve  232 . 6  (whichever valve was previously opened) to restart the extraction. Shut valve  12 . Open valve  232 . 11 . Increase or decrease extractor vessel pressure as described above. Valves can be used to flush/clean the membranes. 
     If the membrane filter is recommended by the manufacturer to backflush, then the following steps can be taken to backflush the membrane filter. Ensure that valves  332 . 1  and  332 . 2  are open, open valve  332 . 5  to open Line  360  from the compressor, close valves  332 . 3  and  332 . 4  and ensure valve  332 . 6  is closed, and close off valves going into the extraction apparatus. Back pressure regulator  335  is used to set the pressure of the filtration vessel. Allow the membrane to backflush for the manufacturer&#39;s recommended time. 
     Once the extraction is complete to a desired extent, the process fluid can be recovered according to the following method. Increase the temperature of the chiller/heater  244  to at least about 110 F. Open valve  232 . 6  and shut valve  232 . 2  (they may already be in this position). Shut valve  1  and valve  5  (only one of them will be open). Open valve  232 . 13  slowly to allow flow into the process fluid storage container  205 . When separation vessel  220  pressure is less than about 200 psi, shut valve  232 . 6  and open valves  232 . 2  and  232 . 8 . In some examples, the pump  290  can be configured to shut down automatically when separation chamber pressure reaches about 70 psi. Close process fluid storage container valve. Vent remaining process fluid out of the system by opening valves  232 . 10 ,  232 . 1  and  232 . 4  and allow residual pressure in the system to vent. The system can now be powered down, or new source material can be loaded and the extraction process started again. 
     In some examples, the orifice can be sized such that a flow rate of the process fluid into the separation chamber  220  matches a flow rate of the process fluid from the pump  290 . In examples, in which the process fluid is supercritical carbon dioxide, the following system parameters and orifice sizes can be used. Chiller/heater temperature: about 110° F. to about 120° F. Extraction vessel pressure: about 1200 psi to about 1400 psi. Orifice size: Size #15 orifice for about 30 cubic feet per minute (CFM) air flow (about 7.5 horse power (HP) air compressor); Size #15 orifice for about 60 CFM air flow (about 15 HP air compressor); Size #25 orifice for about 100 CFM air flow (about 25 HP air compressor). Weight of CO2 in system: approximately 12 pounds for about 5 L extraction vessel systems and about 30 pounds for about 20 L extraction vessel systems. Separation chamber and overflow chamber pressure: about 350 psi to about 400 psi. Separation chamber and overflow chamber temperature: about 70° F. to about 80° F. 
     In examples, in which the process fluid is subcritical carbon dioxide, the following system parameters and orifice sizes can be used. Chiller/heater temperature: about 60° F. to about 70° F. Extraction pressure: about 1100 psi to about 1400 psi. Orifice size: size #10 orifice for about 30 CFM air flow (about 7.5 HP air compressor); size #15 orifice for about 60 CFM air flow (about 15 HP air compressor); size #20 orifice for about 100 CFM air flow (about 25 HP air compressor). Weight of CO2 in system: approximately 17 pounds for the about 5 L extraction vessel systems and about 45 pounds for the about 20 L extraction vessel systems. Separation chamber and overflow chamber pressure: about 250 psi to about 300 psi. Separation chamber and overflow chamber temperature: about 20° F. to about 30° F. 
     In subcritical CO2 operation, the extraction vessel  210  can be full of liquid CO2. In such examples, CO2 can be added to the system after extraction has begun in order to maintain a desired extraction pressure. 
       FIGS. 9-12  disclose other embodiments of systems that can be employed. For example,  FIG. 9  schematically depicts a filtration apparatus or system  300  having a filtration vessel  310  and a fluid bypass line  330 . One or more valves  332 . 1 ,  332 . 2 ,  332 . 3 ,  332 . 4 ,  332 . 5 ,  332 . 6  (e.g., six valves shown) can be included, as well as relief valves  333 . 1  and  333 . 2 . Embodiments can include a back pressure regulator  335 , fluid retentate line  340 , fluid permeate line  250 , filtration vessel permeate pressure buildup line  360 , and filtration vessel permeate vent line  370 . System  300  also can include a pressure gauge  371 , temperature reading device  373 , and pump  395 . 
     During pressurization, valve  332 . 2  and  332 . 5  are open to evenly pressurize both sides of the membrane. When desired pressure is achieved, close valve  332 . 5  and continue with operation. 
     During venting, valve  332 . 6  is open and vent valve in extraction apparatus is also open to allow for even pressure drop across the membrane. Valve  332 . 1  can be opened in addition to or as a replacement to the extraction apparatus vent valve to vent the membrane feed side through the separator apparatus. 
       FIG. 10  is a CO 2  phase diagram that depicts some of the useful ranges for the embodiments disclosed herein.  FIG. 10  represents the performance of merely one example of a membrane from many optional membranes. This CO 2  phase diagram depicts membrane filtration pressures and operating temperatures for that membrane. Another optional membrane has been tested to an operating temperature of 194° F., as an example. 
       FIG. 11  includes a schematic diagram of an embodiment of a system and method. For example, crude oil may be extracted from the plant material via supercritical and/or subcritical CO2. Next, extracted hemp/ cannabis  oil is sent through a membrane filter. The removed retentate can include larger undesirables, and the passed through permeate can include smaller desirables. Next, liquid and/or supercritical CO2, cannabinoids, and terpenes can be collected and depressurized. As the solution pressure decreases, the CO2 converts to a gas and naturally separates from the cannabinoids and terpenes. A reduced usage of heat, or even no application of heat is needed for collection of cannabinoids and terpenes. The system can protect heat-sensitive desirables as well as reduce the costs, energy use and time required for the application of heat. 
       FIG. 12  includes schematic diagrams of embodiments of membrane filtration examples. Membrane filtration can be a pressure-driven separation process based on particulate sizing, such as those shown in the upper, horizontal portion of  FIG. 12 . In the middle horizontal portion of  FIG. 12 , solution travels through a selected membrane and smaller particles (permeate) are pushed through the membrane, while larger particles (retentate) are not. The lower horizontal portion of  FIG. 12  depicts the interest of the  cannabis  and hemp industry in the nanofiltration range. Nanofiltration can be suitable for molecular weights of about 100 Da to about 1000 Da. It is suitable for applications such as fine chemistry, pharmaceuticals, oil and petroleum chemistry, natural essential oils and medicine. 
     The term “supercritical CO2” can be defined as above 88° F. and above 1070 psi. The term “subcritical CO2” can be defined as a minimum of about 910 psi at 75° F., or a minimum of about 800 psi at 65° F. The term “cryogenic CO2” can be defined as about −200° F. to about −300° F. at ambient pressure. The term “ambient room temperature” can be defined as about 65° F. to about 75° F., or about 55° F. to about 85° F. Other definitions also can be used. 
     The organic material can comprise plant material, such as botanicals, which can be processed by non-thermal processing. In one version, the system does not comprise a cooling system. In another version, the process temperature range can include supercritical CO2, which could include a cooling system. Some versions of the system do not include any vessel/building requirements that are normally required for flammable/explosive solvents. Additional programming/sensors can be include for enhanced automation. 
     In some embodiments, the filter membranes can be conventional. In other embodiments, new membrane designs can be deployed, such as to work more effectively with CO2. In one example, conventional processing equipment can be included to recycle the CO2 back to the storage tanks as the CO2 is depressurized. 
     In general, the membranes can work at the same operating conditions as the extractors. Operating conditions can go up to higher pressures (e.g., about 5000 psi) and the system can still function. The membranes can work with any subcritical or supercritical parameters. Valving can be used to control the transmembrane pressure and flowrate to allow for proper usage of the membranes. 
     Without the requirement of heat from evaporation techniques used for conventional solvent removal, the following advantages can be provided by the embodiments disclosed herein:
         heat-sensitive products like terpenes are unaffected   acidic forms of cannabinoids stay intact since there is no addition of heat   evaporation techniques can be partially or completely removed to reduce cost, energy, and time requirements to obtain final product (e.g., rotary evaporator, distillation, etc.)   CO2 can be used to clean oils and residues from any material or decontamination of materials; CO2 can be used to remove oils and other materials or compounds that are soluble in CO2.       

     Other examples can include one or more of the following items. 
     1. A system for processing organic material, the system comprising: 
     an extraction system for extracting soluble compounds from organic material using a compressed solvent to form diluted soluble compounds; 
     a filter system for filtering the diluted soluble compounds through a membrane filter that can:
         remove a retentate comprising undesirable components; and   permit passage of a permeate comprising desirable components and the compressed solvent, wherein the undesirable components comprise a larger molecular weight than the desirable components; and the system further comprises:       

     a depressurization system for depressurizing the permeate and the compressed solvent, and separating the desirable components from the permeate and the compressed solvent. 
     2. The system wherein the extraction system and filter system can process the compressed solvent at a pressure in a range of about 570 psi to not greater than about 5000 psi. 
     3. The system wherein the extraction system and the filter system can process the compressed solvent at a temperature in a range of about 40′F to about 120° F. 
     4. The system wherein the filter system comprises a pump and at least one of microfiltration, ultrafiltration, nanofiltration or reverse osmosis filtration. 
     5. The system wherein the retentate comprises at least one of fats, waxes, lipids or chlorophyll. 
     6. The system wherein the permeate comprises at least one of cannabinoids or terpenes. 
     7. The system wherein the depressurization system can operate without additional heat such that separation of the desirable components from the permeate and the compressed solvent can occur at ambient room temperature. 
     8. The system wherein, other than the depressurization system, the system does not comprise an evaporation system, rotary evaporator or distillation system to separate the desirable components from the compressed solvent. 
     9. The system wherein the extraction system, filter system and depressurization system comprise a continuous, integrated system. 
     10. The system wherein the extraction system, filter system and depressurization system comprise a batch processing system. 
     11. The system of claim  1 , wherein the filter system can receive the diluted soluble compounds directly from the extraction system, and the depressurization system can receive the permeate directly from the filter system. 
     12. The system wherein the filter system and the depressurization system can operate at ambient room temperature. 
     13. The system wherein an entirety of the system can operate at ambient room temperature. 
     14. The system wherein the system can operate at a ratio of the compressed solvent to the soluble compounds, and the ratio is in a range of about 4:1 to about 20:1. 
     15. The system wherein the compressed solvent comprises liquid CO2. 
     16. The system wherein the membrane filter comprises at least one of polymer or ceramic material. 
     17. The system wherein the filter system comprises a filtration vessel having one or more filters. 
     18. The system wherein the filter system comprises a plurality of filtration vessels that are coupled in at least one of in parallel or in series. 
     19. The system wherein the system further comprises an additional extraction system that can process the retentate for batch recirculation without an additional pump. 
     20. The system further comprising a temperature regulator that can regulate a temperature within the filter system. 
     21. The system wherein the system can operate at any temperature and pressure that enables CO2 to be in a subcritical or supercritical fluid phase. 
     22. The system wherein the depressurization system can depressurize the compressed solvent to convert from a liquid to a gas. 
     23. Devices for processing organic material, the devices comprising: 
     an extraction system configured to extract soluble compounds from organic material using a compressed solvent to form diluted soluble compounds; 
     a filter system configured to be coupled to the extraction system to filter the diluted soluble compounds through a membrane filter that is configured to:
         remove a retentate comprising undesirable components; and   permit passage of a permeate comprising desirable components and the compressed solvent, wherein the undesirable components comprise a larger molecular weight than the desirable components; and the devices further comprise:       

     a depressurization system configured to be coupled to the filter system to depressurize the permeate and the compressed solvent, and separate the desirable components from the compressed solvent. 
     24. A method of processing organic materials, the method comprising: 
     extracting soluble compounds from organic material using a compressed solvent to form diluted soluble compounds; 
     filtering the diluted soluble compounds through a membrane filter, removing a retentate comprising undesirable components and permitting passage of a permeate comprising desirable components and the compressed solvent, such that the undesirable components comprise a larger molecular weight than the desirable components; 
     depressurizing the permeate and the compressed solvent; and 
     separating the desirable components from the permeate and the compressed solvent. 
     This written description uses examples to disclose the embodiments, including the best mode, and also to enable those of ordinary skill in the art to make and use the invention. The patentable scope is defined by the claims, and can include other examples that occur to those skilled in the art. Such other examples are intended to be within the scope of the claims if they have structural elements that do not differ from the literal language of the claims, or if they include equivalent structural elements with insubstantial differences from the literal languages of the claims. 
     Note that not all of the activities described above in the general description or the examples are required, that a portion of a specific activity may not be required, and that one or more further activities can be performed in addition to those described. Still further, the order in which activities are listed are not necessarily the order in which they are performed. 
     In the foregoing specification, the concepts have been described with reference to specific embodiments. However, one of ordinary skill in the art appreciates that various modifications and changes can be made without departing from the scope of the invention as set forth in the claims below. Accordingly, the specification and figures are to be regarded in an illustrative rather than a restrictive sense, and all such modifications are intended to be included within the scope of invention. 
     It can be advantageous to set forth definitions of certain words and phrases used throughout this patent document. The term “communicate,” as well as derivatives thereof, encompasses both direct and indirect communication. The terms “include” and “comprise,” as well as derivatives thereof, mean inclusion without limitation. The term “or” is inclusive, meaning and/or. The phrase “associated with,” as well as derivatives thereof, can mean to include, be included within, interconnect with, contain, be contained within, connect to or with, couple to or with, be communicable with, cooperate with, interleave, juxtapose, be proximate to, be bound to or with, have, have a property of, have a relationship to or with, or the like. The phrase “at least one of,” when used with a list of items, means that different combinations of one or more of the listed items can be used, and only one item in the list can be needed. For example, “at least one of: A, B, and C” includes any of the following combinations: A, B, C, A and B, A and C, B and C, and A and B and C. 
     Also, the use of “a” or “an” are employed to describe elements and components described herein. This is done merely for convenience and to give a general sense of the scope of the invention. This description should be read to include one or at least one and the singular also includes the plural unless it is obvious that it is meant otherwise. 
     The description in the present application should not be read as implying that any particular element, step, or function is an essential or critical element that must be included in the claim scope. The scope of patented subject matter is defined only by the allowed claims. Moreover, none of the claims invokes 35 U.S.C. § 112(f) with respect to any of the appended claims or claim elements unless the exact words “means for” or “step for” are explicitly used in the particular claim, followed by a participle phrase identifying a function. 
     As used herein, the term “about” or “approximately” applies to all numeric values, whether or not explicitly indicated. These terms generally refer to a range of numbers that one of skill in the art would consider equivalent to the recited values (i.e., having the same function or result). In many instances these terms may include numbers that are rounded to the nearest significant figure. As used herein, the terms “substantial” and “substantially” means, when comparing various parts to one another, that the parts being compared are equal to or are so close enough in dimension that one skill in the art would consider the same. Substantial and substantially, as used herein, are not limited to a single dimension and specifically include a range of values for those parts being compared. The range of values, both above and below (e.g., “+/−” or greater/lesser or larger/smaller), includes a variance that one of skill in the art would know to be a reasonable tolerance for the parts mentioned. 
     Benefits, other advantages, and solutions to problems have been described above with regard to specific embodiments. However, the benefits, advantages, solutions to problems, and any feature(s) that can cause any benefit, advantage, or solution to occur or become more pronounced are not to be construed as a critical, required, sacrosanct or essential feature of any or all the claims. 
     After reading the specification, skilled artisans will appreciate that certain features which, for clarity, are described herein in the context of separate embodiments, can also be provided in combination in a single embodiment. Conversely, various features that are, for brevity, described in the context of a single embodiment, can also be provided separately or in any subcombination. Further, references to values stated in ranges include each and every possible value within that range.