Abstract:
Methods and apparatus for producing bio-diesel from triglycerides and lower alcohols, desirably in the presence of liquid or supercritical CO 2 , are provided. The apparatus are designed to enhance the miscibility of the triglycerides with lower alcohols.

Description:
CROSS-REFERENCES TO RELATED APPLICATIONS 
       [0001]    This application is a continuation of U.S. application Ser. No. 11/490,861, filed Jul. 21, 2006, incorporated herein by reference in its entirety, which claims priority to U.S. Provisional Application No. 60/783,963, filed Mar. 20, 2006; U.S. Provisional Application No. 60/786,959, filed Mar. 29, 2006; and U.S. Provisional Application No. 60/799,515, filed May 11, 2006, the entire disclosures of which are incorporated herein by reference. 
     
    
     FIELD OF THE INVENTION 
       [0002]    The present invention relates to the improved and efficient manufacture of renewable fuels and in particular, the production of normally liquid, fluid, renewable fuels and more specifically bio-diesel, from animal and plant fats or triglycerides by the method of trans-esterification. The production methods disclosed may use high pressure in miniaturized or micro and nano (when channels are below about 100 μm diameter) chemical processing apparatus. The purpose of the apparatus is to reduce the floor space needed to install the complete production system, when compared with the typical bio-diesel processing plant used previously and/or to create conditions under which triglycerides and lower alcohols mix efficiently. 
       BACKGROUND OF THE INVENTION 
       [0003]    Hitherto, bio-diesel has been produced in ambient conditions by providing a catalyst, such as sodium hydroxide or potassium hydroxide, blended with an excessive quantity of methanol and a quantity of refined animal or plant fat; most preferably the fat or triglycerides are heated to about 120° F. then the combined liquids and catalyst are transferred to a storage vessel or reactor and agitated for up to approximately 7 hours or more, until the animal fat (triglycerides) has reacted with as much methanol as the triglycerides have chemical bonds to allow and the reaction phase of bio-diesel production is complete. Bio-diesel produced in this way requires copious quantities of clean water to wash any detergents, such as sodium stearate (otherwise known as soap) from the fluid bio-diesel that will likely be present in small quantities. The excess methanol and catalyst is then allowed to stratify after transfer to a suitably, elongated, tall vessel, or separation column, where the bio-diesel (e.g., specific gravity=approximately 890 Kg/M 3 ) can stratify into layers according to the specific gravity of each fluid present; therefore, the lowest stratified layer would be glycerol (specific gravity=1126 kg/M 3 ) with water (specific gravity=approximately 1000 Kg/M 3 ) directly above the glycerol, bio-diesel fatty esters (approximately 890 Kg/M 3 ) above the water and the surplus methanol (specific gravity=approximately 791.3 Kg/M 3 ) floating above the bio-diesel. The stratified and separated fluids can then be de-cantered for subsequent use as intended, with recycling of surplus methanol and the bio-diesel for use as the intended liquid fuel. 
       SUMMARY OF THE INVENTION 
       [0004]    One aspect of the present invention is directed to a process for the production of bio-diesel that uses liquid or fluid, dense phase CO 2  as an alternative or additional catalyst. The use of liquid or fluid, dense phase CO 2  (L-CO 2 ) significant reaction time reduction and also facilitates a more complete reaction of triglycerides with a lower alcohol, such as methanol or ethanol, followed by an improved separation of firstly, clean bio-diesel and secondly, glycerol from the remaining fluid comprising excess methanol and/or ethanol, catalyst, L-CO 2  and impurities. More specifically, the improved separation process comprises an enclosed, pressurized, vertically disposed centrifuge using liquid CO 2  as a liquid medium for separation of crystallized bio-diesel and glycerol. The use of a pressurized centrifuge is described in patent applications by the present inventor, for example, as in U.S. Patent Application Publication No. 2005/0042346 and in International Patent Application No. PCT/US2005/043507, filed Dec. 2, 2005, which was published on Jun. 8, 2006, under Publication No. WO 2006/060596. The above patents and the disclosures of all patent applications in the name of the present inventor are herein expressly incorporated by reference in their entirety. 
         [0005]    The invention relates to the use of micro or nano technology in the production of renewable fuels and, in particular, of bio-diesel and all corresponding by-products. In one embodiment of the invention, a stream of low cost, readily available, excess beef fat feedstock (a bio-diesel feedstock) is transferred by any suitable pumping means under controlled pressure into manifolds (or ports), which feed micro-size conduits (or reaction tubes). This process reduces reaction time since the close proximity of the reagents in the conduits enables reactions to occur more rapidly and also produces controlled quantities of materials of higher value, such as bio-diesel, more rapidly than systems that use, for example, sodium hydroxide blended with triglycerides in a large tank or vat system. Furthermore solid catalysts such as silica can be fixed to the inner surface of the reaction conduits and vessels. This invention includes preferred conditions to rapidly mix reagents by way of static structures assembled from a series of plates (or discs) wherein each plate has depressions (or recesses) with profiles that align with depressions having corresponding mirrored profiles in each adjacent plate. Typically, the plates are manufactured from, most preferably as a first instance, stainless steel and secondly, plates formed under high pressure such as by way of compression and/or injection molding of suitable polymers. A series of conduits are machined or molded such that when several plates are stacked together, a series of uniform cross-section conduits traversing all plates, enable the transfer of micro quantities of chemical feed stock through the enclosed spaces in which controlled reactions take place. After the reactions are complete, the newly formed materials are then transferred via a series of conduits connected to manifolds that traverse the stacked plates in a similar fashion to those provided for the feed stock materials. A purpose of this equipment is to enable the manufacture of small quantities of chemicals that may otherwise require very costly apparatus and processes. 
         [0006]    An additional benefit of the process disclosed herein includes the reduction in the quantity of water ordinarily required for preparing bio-diesel manufactured with sodium hydroxide or potassium hydroxide as catalysts. Very large quantities of water are required to “wash” bio-diesel prior to consumption in, for example, an internal combustion engine. Sodium hydroxide and/or potassium hydroxide are potentially damaging to, for example, injection and all exposed metal surfaces within an internal combustion engine. Corrosion can occur and the life of the subject internal combustion engine will be reduced. The disclosure below provides details of a process incorporating sub and/or super-critical CO 2  as the catalyst. L-CO 2  blended with the other components, which may include a quantity of water, required to produce bio-diesel after the reaction has occurred, can provide a low pH value such as 5, 4, 3 and even as low as about 2.9. Elevated pressure on the order of 500 psi at about 34° F. to 36° F. may be required to create the conditions under which such low pH will occur; conversely, when pressure is released under controlled reduction to ambient pressure, any CO 2  that remains with the bio-diesel will quickly boil off, leaving no more than the bio-diesel and glycerol present. 
         [0007]    A second aspect of the invention is directed to an improved separation process that uses an apparatus that comprises a single or series of interconnected hydro-cyclones or more specifically, enclosed and sealed cyclones using liquid/fluid carbon dioxide instead of water, wherein the cyclones are suitably enclosed, sealed and pressurized, save the input and output ports. The input and output ports are connected to conduits which are enclosed by suitable valves, to maintain the carbon dioxide at a selected pressure such that the specific gravity of the liquid carbon dioxide is maintained at a selected level, such as 58 lbs. closed cubic foot. The cyclones are connected to, most preferably, centrifugal pumps, wherein a single centrifugal pump is connected via a conduit to the upper inlet of a cyclone. The fluid carbon dioxide containing triglyceride-containing solids, such as ground beef, in suspension is transferred via a pressurized conduit which is connected to the cyclone. The ratio of solids in suspension to the carbon dioxide fluid can be on the order of one part liquid carbon dioxide to 4 or 5 parts solids in suspension. In the case of ground beef, the particles of ground fat can be separated from the lean beef particles. The fat, or more specifically the fatty adipose tissue including some inseparable lean beef (muscle striations), is then processed by applying heat, then centrifuging and separating the beef oil from the other solids. The solids are then chilled and blended with other lean food products and the beef oil is used in the production of bio-diesel as disclosed herein. The cyclones incorporated in the process of beef oil extraction are described in greater detail below. 
         [0008]    The foregoing aspects and many of the attendant advantages of this invention will become more readily appreciated by reference to the following detailed description when taken in conjunction with the accompanying drawings. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0009]      FIG. 1  shows a full set of laminae in an exploded view, according to the present invention; 
           [0010]      FIG. 2  shows a three dimensional view of a collection of four plates arranged to provide a series of connected conduits within which controlled chemical reaction can take place, according to the present invention; 
           [0011]      FIG. 3  shows the outline of conduits created when the apparatus of  FIG. 2  is assembled. Inlet conduits connected via manifolds and enclosed spaces to outlet conduits arranged adjacent to one another, according to the present invention; 
           [0012]      FIG. 4  shows cross sectional illustrations of the conduits and spaces enclosed within four corresponding plates that are stacked and clamped together, according to the present invention; 
           [0013]      FIG. 5  shows the behavior of three fluid streams combined into a single stream shown immediately after combining and then after transfer into the enclosed space of a reaction chamber, according to the present invention; 
           [0014]      FIG. 6  shows a diagrammatic representation, generally in plan view, of an application where the present invention is applied, according to the present invention; 
           [0015]      FIG. 7  shows a preferred embodiment of an apparatus, wherein a centrifugal reaction process is illustrated, according to the present invention: 
           [0016]      FIG. 8  shows the chemical reaction of triglycerides and methanol to produce fatty esters and glycerol, according to the present invention; 
           [0017]      FIG. 9  shows a 3D view of an apparatus designed for the production of bio-diesel, according to the present invention; 
           [0018]      FIG. 10  shows a preferred embodiment of an apparatus, wherein a rotating reaction member provides mixing means according to the present invention. 
           [0019]      FIG. 11  is diagram showing steps in a production configuration that can be arranged to produce bio-diesel and other components of a chemical reaction plant matter. 
           [0020]      FIG. 12  a plan view of a diagram showing a preferred method of bio-diesel and glycerol production. 
           [0021]      FIG. 13  is a table showing a range of temperatures and pressures that can be maintained to achieve maximum efficiency of a particular reaction. 
           [0022]      FIG. 14  shows a hydrocyclone that may be used to separate lean beef from beef fat in accordance with the present invention. 
           [0023]      FIG. 15  shows a cross-sectional view of the hydrocyclone of  FIG. 14 . 
       
    
    
     DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS 
       [0024]    The apparatus and processes described herein are most preferably used for the production of bio-diesel. The apparatus shown herein comprises a series of three dimensional views of a micro reactor with details showing the manifolds and conduits providing a general understanding of the operation and approximate size of the apparatus.  4000  and  4008  in  FIG. 1  represent length by width, respectively, of the plan view of a stacked and assembled grouping of laminae wherein the diameter of  4000  equals approximately one inch and the diameter of  4008  is ¾ of an inch. The thickness of a typical laminae is represented by  5042  and is on the order of 1/16 of an inch. The diameter of manifold  4020  is approximately ⅛ of an inch. Hence, the equipment described herein is generally referred to as “micro technology”. 
         [0025]    The reaction residence time during which the blended materials required for the reaction are retained in the reactor (vessel) of a typical macro bio-diesel production system is on the order of 7 hours, whereas the reaction time for the micro-technology described herein can be on the order of 20 seconds. It can therefore be seen that relatively substantial quantities of bio-diesel can be produced by the micro equipment when compared with macro equipment production rates. An integrated micro structure is provided by stacking several flat sections (or plates) of selected material, wherein each flat section is machined or molded to provide channels, vessels, ports and conduits that may communicate directly with adjacent flat sections. The inlet and outlet ports of each flat section are located in common positions such that when stacked together the outlet port of a first flat section can communicate directly with the inlet port of a second adjacent flat section, which are connected together such that their inlet and outlet ports are connected by a series of channels and enclosed chambers in which the chemical reaction required to produce renewable fuels can take place. In this way, flat sections are connected together via outlet and inlet ports and the inlet and outlet ports of each flat section are connected by a series of channels and enclosed chambers specifically designed to facilitate the chemical reaction required to produce renewable fuels or bio-diesel. The stacked laminae formed from the flat section (with slots, perforations, grooves, recesses, channels and vessels), are carefully arranged to provide a series of reticulating conduits within which, when stacked and held firmly together, immiscible and/or miscible fluids alike, can be blended together thoroughly in the micro channels, vessels and miniature reactors to ensure contact between, in particular, immiscible fluids such as fluid beef tallow and methanol or ethanol. Such thorough mixing can occur with dissimilar materials that ordinarily may repel each other. The reaction to produce bio-diesel and glycerol is shown in  FIG. 8 . 
         [0026]    Additionally, it is a purpose of the new technology disclosed herein to facilitate enhanced quality of food and, in particular, the quality of beef harvested, typically, from either steer or heifer sources wherein these animals are slaughtered at the age of about 30 months or less or more, enhancing beef flavor, tenderness, mouth-feel and aroma while facilitating the low cost production of low cost bio-diesel from animal fat harvested from the slaughtered animals. Animal fat sources most preferably from cattle and having been lot fed to attain a body weight greater than 1,200 lbs will be more abundant than if the animals are smaller. Typically, steer and heifers can be transferred to lot feeding facilities at the age of, for example, 1 year to 2 years and then the animals may be retained in the lot feeding facility for a period of several months, but generally, significantly less than 12 months. The period of time that the cattle are held is determined by the weight gain of individual animals. The animals will generally be released for slaughter when they reach an approximate weight of 1,200 lbs. Some cattle attain this weight by or before the age of 15 months, whereas others may take significantly longer and in some cases never reach this target weight. So, it is a purpose of this invention to provide an incentive to cattle “feeders” to retain cattle at the lot feeding facility for a period of time determined by the attained body weight of each animal. Furthermore, it is intended to encourage feed lot operators to allow cattle to be finished and released for slaughter only when a significant quantity of beef fat has become available for harvesting from the carcasses after slaughter. More particularly, it should be noted that cattle around the age of 15 to 24 months have a capacity to consume vast quantities of feed. Little exercise is required for the animal located in a feed lot since feed is available within a short distance, even from the furthermost point in each pen of the feeding lot. Therefore, little exercise is possible, although sufficient to satisfy the natural requirements of cattle, which are quite different from other animals housed in intensive breeding and rearing facilities. Briefly, intensive breeding and animal rearing procedures comprise enclosure of, for example, sows in breeding pens that restrict them from even turning around. Such an example is typical and the pigs have been bred by selecting those animals with the most suitable characteristics for enclosing within the intensive rearing facility. Conversely, cattle cannot be intensively farmed, particularly during the first few months of the animal&#39;s life, at least not with the currently predominant cattle breeds and they must be enclosed within pens having at least one hill that they can climb and also the provision of feed and water close by. The typical heifer and steer body weight of 1,200 lbs enables harvesting of more than 200 lbs of fat (white adipose fatty tissue) from which proteins, collagen and connective tissue must be separated from the fatty tissue prior to the production of bio-diesel from said fat. Approximately 8 lbs of oil (tallow; in particular, beef tallow having no solids or other contaminants) with a proportioned quantity of methanol (see below for specific quantities) can produce about one gallon of bio-diesel. 
         [0027]    It is a purpose of this present invention to provide encouragement to cattle feed lot operators to retain animals for a longer period and in the feed lot facilities so that the quantity of fat yielded from each animal is increased. It is anticipated that such increase would be equal to at least a 50% more than is currently available. The benefit of this prospect far exceeds the associated costs. A 1,200 lb steer or heifer consumes vast quantities of feed; however, the conversion rate can exceed 25% at this stage of their life cycle. Therefore, adopting this method of producing fat for production of bio-diesel is substantially less costly than, for example, sourcing similar fat from plant matter such as seeds or beans (such as soy beans). Costs inevitably incurred in the production of oil derived from plant matter include the crushing plant costs, which is on the order of $60 million. Therefore, to extract a quantity of oil from virtually any plant source requires the cultivating of the appropriate plant (e.g., soy beans) to be harvested. The separation of seeds or beans from the supporting plants then crushing the beans or seeds, results in a relatively small quantity of extracted oil when compared with the value or cost of entire living plant, most of which is lost. In fact, greater than 75% of the energy stored in a plant having been derived via photosynthesis from the solar source, is lost. When compared with fat derived from an animal source, it can be seen the plant matter wasted in producing oil by way of plant cultivation is 75% which is comparable to the feed loss with a 25% conversion rate. However, the conversion rate of feed in cattle of 20 months old is greater than 25% and the animal fat source does not require new fat extraction crushing plant and equipment. 
         [0028]    Desirably, bio-diesel shall be produced according to the processes disclosed herein by the trans-esterification of triglycerides harvested from cattle (or plant matter of suitable type or genus). In one embodiment, CO 2  is used as a catalyst in suitable proportion to the beef fat or oil at appropriate temperature and pressure as required to maintain the CO 2  phase most suitable for the maximized bio-diesel production. These processes may use micro and/or nano technologies such as those recently developed at ONAMI Pacific North West Laboratories or Oregon Nano Science and Micro Technology Institute. ONAMI have developed a micro scale production plant for the manufacture of bio-diesel from plant materials. In addition, SafeFresh Technologies, LLC have developed processes incorporating CO 2  as the catalyst, medium, refrigerant, antimicrobial and propellant, all employed in a process that has now reached commercial operation. By combining these two separate technologies, the investor has developed an efficient process for bio-diesel production. The processes may utilize micro technology such as the ONAMI bio-diesel micro technology, as disclosed in association with  FIGS. 1-5 . Notably, unlike the technologies developed by ONAMI wherein catalysts such as silicon, sodium hydroxide, potassium hydroxide and other solid structures form a component of the micro equipment developed by ONAMI, the present methods may displace other more conventional catalysts with L-CO 2 . The reactions (between the triglyceride fat molecules and methanol and/or ethanol) can be enabled when liquid CO 2  or, alternatively, dense phase critical CO 2  which is thoroughly miscible with said triglyceride animal fats is combined with a proportionate quantity of methanol and/or ethanol. 
         [0029]    In some embodiments, the reaction between methanol and/or ethanol and triglycerides with a suitable catalyst yields approximately 20 grams of glycerol with every 100 grams of bio-diesel. Furthermore, it is preferable that excessive methanol and/or ethanol be provided and therefore, the residual methanol and/or ethanol will comprise a component of the resultant mixture. Said mixture contains bio-diesel, glycerol, methanol and/or ethanol and CO 2 . In any event, the resultant mixture of liquids is desirably separated prior to using the bio-diesel as a liquid fuel. 
         [0030]    In particular, the apparatus disclosed in association with a series of figures describing an enclosed pressurized vertically disposed (or horizontally disposed) decanter-style centrifuge arranged to separate liquids and solids from liquids and solids into separated, isolated streams. In one preferred embodiment, the separation of glycerol and bio-diesel can be achieved by “spray-freezing” the resultant fluid as disclosed herein. The separated streams of methanol, ethanol, water and CO 2  can then be recycled with bio-diesel transferred into suitable storage vessels. A hydrocyclone separation apparatus is shown in  FIGS. 14 and 15 . 
         [0031]    Referring now to  FIG. 1 , a three dimensional view of an apparatus comprising a series of plates or lamina such as  4040  and  4044  are arranged in symmetrical groups of 4× lamina each, between an upper end plate  4014  and a lower end plate  4092 . The view in  FIG. 1  is “exploded” and 5 groups of 4× lamina, or flat sections, are shown in an expanded view and spread apart. The apparatus when in closed position, such that all laminae are held in tight contact with adjacent lamina, held together by said end lamina  4014  and  4092  in such a manner that suitable clamps exert such pressure so as to close end plate  4014  toward opposing end plate  4092  with a closing pressure sufficient to inhibit leaking of any pressurized fluids that may be transferred through ports, conduits and vessels provided within the assembled flat sections, generally provides a fully enclosed system, other than inlet and outlet ports which are also sealed tight in connections to corresponding supply and removal conduits, preventing escape of any fluid to atmosphere, having conduits communicating and connected in a manner that is described as follows: 
         [0032]    Port  4002  connects directly with a series of ports having a center line parallel with arrow  5046  and extending through all flat sections, plates or lamina with an end plate  4014  through plate  4080  and enclosed at a lower end by plate  4092 , thereby creating a conduit into which fluid can be transferred, wherein said fluid can transfer via conduits parallel with manifolds  5044  and  5045 , and all manifolds of similar length to  5044  and  5045 , wherein said manifolds connect each group of conduits together such that the fluids transferred therein can be extracted by connecting to extraction conduits (such conduits not shown). Ports  4020  and  4022  connect directly with ports  4038  and  5016  respectively, then plates  4082  and  4084  respectively and so on to provide two parallel conduits in direct communication with a series of perpendicular conduits such as those defined by recesses  5031  and  5039 . Recess  5031  communicates with a series of connection tubes  5026 ,  5038 ,  5036 ,  5034  and  5032  with similar and corresponding connection tubes communicating with recess  5039 . It can therefore be understood that fluid transferred into port  4022  in the direction shown by arrow  5048  can enter recess  5031  and from recess  5031  into connection port  5026 , etc. Similarly, fluid transferred in the direction shown by arrow  4010  into port  4020  can flow into conduit segment  4038  and then into recess  5039  and so on. The conduits or recesses arranged between laminae such as  4014  and  4040  are arranged to communicate in such a manner that bio-diesel and a proportionate quantity of glycerol can be manufactured in the apparatus. When fluids comprising beef fat are blended with a proportionate quantity of liquid CO 2  then transferred into port  4002 , a quantity equal to about 20% by volume, for example, of fluid transferred into port  4002  is transferred via ports  4020  and  4022 . The conduits provided are arranged to combine a suitable quantity of methanol and/or ethanol with a corresponding quantity of blended liquid CO 2  and beef tallow such that contact between molecules of beef fat and molecules of methanol and/or ethanol occurs, resulting in a reaction between the methanol and/or ethanol and the triglyceride molecules of the beef tallow, resulting in production of bio-diesel which then transfers into reaction chambers, the detail of which shall be provided below. 
         [0033]    Five assembly groups of lamina are shown in  FIG. 1  in exploded view between end plates  4014  and  4092  including a first assembled group of plates  4040 ,  4044  and  4046 . Each group of lamina are similar and are profiled with slots, recesses and ports that correspond with the profiles of adjacent lamina to provide a series of conduits and reaction tubes connected directly with input ports  4002 ,  4004  and  4020  which can communicate there through with extraction ports such as  4026 ,  4028  through  4036  and also a corresponding series of ports including port  5022 .  FIG. 2  shows the outline of a similar grouping of laminae such as  4040 ,  4044 ,  4046  and  4047  (of  FIG. 1 ) with the outline of extraction ports  4026 ,  4028 ,  4030 ,  4032 ,  4034  and  4036  (of  FIG. 1 ) and input connection ports  4038 ,  5016  and  5017  which together correspond with ports  28 ,  32  and  30  (of  FIG. 2 ), which connect to distribution conduits (or manifolds) such as  5031  and  5039  ( FIG. 1 ), transfer tubes such as  5034 ,  5036  and  5026 , which connect with reaction tubes such as  245  or  288  in  FIG. 3  which in turn connect with reactor vessels or reaction chambers such as  274  or  254  in  FIG. 3  which collectively communicate directly between said input ports and output ports of an output manifolds of  FIG. 1 . Said series of 5 laminate groupings shown in exploded view and spaced apart in-line between end plates  4014  and  4092  (of  FIG. 1 ) are each constructed and arranged in like fashion as the outline of members  40 ,  44 ,  76  and  46  as shown in  FIG. 2 , all generally arranged such that when assembled and held compressed, by any suitable set of tie-rods (not shown) for example, between said end plates  4014  and  4092 , bio-diesel can be manufactured within such an enclosed series of micro channels and conduits with an input stream provided via feeding tubes connected directly to manifolds such as  4012  and  5040  of  FIG. 1 . 
         [0034]    Referring again to  FIG. 1  and, in particular, inlet ports  4002 ,  4020  and  4022 , it should be noted that fluids transferred therein will follow the micro conduits such as  5031  and  5039  and then through ports such as  5036  and  5034  and after reticulating through the micro channels and reaction chambers, bio-diesel and glycerol will transfer through extraction ports such as  5008  in the direction shown by arrows  5006  and  5010  to connect with manifold  5000  or manifold  4088  and then through outlet ports such as  4087  in the direction shown by arrow  4093  provided in manifold  4088  or, alternatively, through outlet port  5001  of manifold  5000  in the direction shown by arrow  5003 . 
         [0035]    Referring now to  FIG. 2 , ports  28  and  32  are arranged to provide communication with reactor vessels such as  22  and  38 . First, fluid comprising a blend of refined beef tallow and any suitable fluid catalysts such as L-CO 2 , sodium hydroxide or potassium hydroxide blended together can be transferred through port  30 . Port  30  communicates with conduit  35 , enabling transfer of said first fluid to be transferred via conduit  35  and then into connection tube  23  and into reaction conduit  24 , followed by reaction vessel  22 . The reaction vessels  22 ,  38  and  50 , for example, which are connected to reaction conduits  24  and  36 , are typical examples of preferred profiles for most efficiently producing bio-diesel from the fluids provided therein. Conduits  35 ,  26  and  66  are examples of conduits provided to transfer fluid prior to reaction together. In particular, fluids transferred via port  30  combine with fluids transferred via ports  28  and  32  within reactor conduits such as  24  and  36  which, in turn, communicate with reaction vessels  22  and  38  respectively and similar to, for example, reactor conduit  74  or reactor vessel  64 . Fluids transferred via port  30  are ultimately sandwiched above and below, in intimate contact with fluid transferred via ports  28  and  32  as described below in association with  FIGS. 3 ,  4  and  5 , and in particular, as shown in  FIG. 5 , section “B-B”. 
         [0036]    Referring now to  FIG. 3 , the outer profile of a complex manifold-like image is shown with solid lines, projected in a three dimensional view. Again, the outline shown in  FIG. 3  corresponds to the groupings of plates shown in three dimensional view in  FIG. 2  which also corresponds with the assembly of 5 groupings of 4 laminae each (such as  4040 ,  4044 ,  4046  and  4047 ) shown in  FIG. 1 . 
         [0037]    The three dimensional image shown in  FIG. 3  comprises a series of input ports  228 ,  234  and  240  (also referred to as manifolds) which correspond with inlet ports  30 ,  28  and  32  as shown in  FIG. 2 . Fluid transferred into port  234  in the direction shown by arrow  232  ultimately becomes sandwiched between fluid transferred via port  228  in the direction shown by arrow  230  and port  240  in the direction shown by arrow  236 . Fluid transferred via port  234  is ultimately sandwiched between fluid transferred via port  228  and fluid transferred via port  240  in such a way that contact between molecules of the fluids enables the rapid production of bio-diesel according to the reaction shown in  FIG. 8 . 
         [0038]    In one preferred embodiment, a blended fluid comprising a catalyst such as L-CO 2  combined with ethanol and/or methanol collectively maintained at a suitable pressure such as 1,100 PSIG or greater and temperature such as 90° F. or greater (to ensure fluid L-CO 2  is maintained in a suitable, super critical phase) is transferred at a controlled and adjustable rate into ports  28  and  32  of  FIG. 2  which connect with lateral conduits  34  and  66  and also  26  and  69 . Corresponding lateral conduits are arranged in pairs with, for example, lateral conduit  26  located above reaction conduits  24  and  74  with vertically disposed connection tubes such as  70 . A supply of fluid comprising beef fat having been separated from substantially all other source material solids (e.g. proteins and connective tissue) is transferred under controlled pressure (e.g., about 500 psi) through port  30  which, in turn, connects with a lateral conduit such as  68  and then with connection tubes such as  23  and  65  before direct transfer at a perpendicular disposition to a reaction conduit such as  24 . The reaction conduit  24  connects directly to reactor vessel  22  which has a profile flattened to ensure a broad exposure between fluids transferred there through. 
         [0039]    Referring to  FIG. 2 , it can be seen that a controlled supply of liquid beef fat transferred via port  30  and into lateral conduit  68  can be pumped under selected pressure into reaction conduits such as  74 ,  24  and  36 . Said reaction conduits connect directly to enclosed flattened reaction vessels such as  38 ,  50 ,  64  and  22 . In this instance, the enclosed reaction vessels are arranged to ensure the contact between the catalyst super-critical CO 2  with methanol and/or ethanol and beef fat transferred into said reaction vessels. The lateral connection tubes such as  26  and  69  are arranged to transfer L-CO 2  and methanol and/or ethanol simultaneously into the upper zone of reaction conduits via lateral conduit  26  and into lower zone of reaction conduits by lateral conduit  69 . In this way, beef fat is transferred at a suitable temperature via distribution port  30 , lateral conduit  68  and vertical transfer connection such as  23 , directly into an end of conduit such as  24  such that the single stream of beef fat is transferred along a reaction conduit such as  24  which is then sandwiched between upper and lower streams of fluid transferred via lateral conduits  26  and  69 , for example. A fundamental purpose of the arrangement of conduits and reaction cavities shown in  FIG. 2  is to ensure that contact is made between beef fat and said CO 2  catalyst with methanol (or ethanol). The apparatus shown in  FIG. 2  comprises a series of flat parallel sided, adjacent lamina or plate assemblies arranged together (as shown in  FIG. 1  in exploded view between conduit terminating end plates  4008  and  4092 ). Extraction tubes can be directly connected to each manifold  4088  and  5000  to extract the resultant fluid after the reaction is complete; the resultant fluid comprising bio-diesel, glycerol, methanol and/or ethanol and any other catalysts that may have been used, may then be separated into the components of bio-diesel, glycerol, methanol and other matter such as impurities. 
         [0040]    Referring again to  FIG. 2 , a three dimensional view outlines the conduits formed into 4× plates or laminae when they are stacked together as shown in  FIG. 1 . The rectangular plates or flat sections are arranged wherein an upper plate  40  and a lower plate  46  sandwiches plates  44  and  76  there between. An outline of cavities such as conduit  36  and enclosed vessels such as  38  and  64  which connect a series of conduits to extraction ports  10 ,  12 ,  14 ,  16 ,  18 , and  20  and also  62 ,  60 ,  58 ,  56 ,  54  and  52  respectively, created by assembly of the four plates, can also be seen. 
         [0041]    Referring now to  FIG. 3 , the outline of all inner conduits and transfer tubes in a section comprising 3× plates with feeding ports, lateral micro conduits with perpendicular reaction tubes and enclosed reaction vessels connected to extraction manifolds is shown with arrows such as  278 ,  302 ,  316 ,  224 ,  327 ,  221 ,  212 ,  270 ,  266 ,  218  and  253  showing the flow and direction of each stream of fluid through each conduit segment. It should be noted that a series of solid lines shown in  FIG. 3  correspond with broken lines shown in  FIG. 2  wherein inlet ports  28  and  32  correspond with  228  and  240  of  FIG. 3 . Fat distribution manifold  234  corresponds with conduit  30  of  FIG. 2 ; lateral conduit  26  corresponds with  226  of  FIG. 3  and so on, with reaction conduit  222 , for example, corresponding with reaction conduit  24  which is shown in  FIG. 2 . 
         [0042]    Referring again to  FIG. 3 , lateral conduits  226  and  292  connect with fluid supply port  228  such that said fluid transferred under controlled pressure and temperature in the direction shown by arrow  230  through said port  228  is pressurized such that quantities substantially controlled by the cross sectional diameter of lateral conduits  226  and  292  provide an enclosed pathway for the material supplied in the direction shown by arrow  230  to flow in the direction shown by arrows such as  224  and  320  and then in the direction shown by arrows such as  293  and  317 . Fluid transferred via conduit  226  in the direction shown by arrow  224  is subsequently divided equally so as to flow via perpendicular conduits such as  294  in direction shown by arrow  317 . In like fashion, fluid transferred in the direction shown by arrow  236  through port  240  is divided proportionately by transfer through lateral conduits such as  238  and  244  flowing in the direction shown by arrows  235  and  242  respectively. Perpendicular transfer tubes such as  286  and  246  provide sealed pathways for fluid transfer in the direction shown by arrows  283  and  325 , respectively. Blended fluid streams transferred via connection conduits such as said  286  and  289  is transferred into an upper region of reaction conduit  288  volumetrically and substantially equally. The combined mass flow of the streams transferred through perpendicular connection tubes such as  286  in the direction shown by arrow  283  is equal to the mass flow of fluid transferred via port  234  ( FIG. 3 ). 
         [0043]    It can therefore be readily understood that in this way, fluids and/or suspensions transferred via ports  228  and  240  in the direction shown by arrows  230  and  236  respectively, can be distributed into reaction conduits such as  245 ,  323 ,  338 ,  300 ,  314  and  322 . A stream of fluid represented by arrow  232  is pumped under pressure (480 psi to about 600 psi) along port  234  and is subsequently divided into equal but separate streams of fluid traveling in the direction shown by arrow  297  which is then divided into 12 streams comprising six (6×) pairs of streams including the stream represented by arrow  298  in conduit (or reaction tube)  300  above and the stream shown by arrow  287  in conduit (or reaction tube)  288 . The fluid beef fat is therefore sandwiched between a pair of layers transferred into said reaction tube such as  300  via perpendicular conduit  294  on a first side and via conduit  296  on the upper or opposite side. 
         [0044]    The mass flow of combined fluid transferred into ports  228  and  240  may be arranged such that it corresponds to the mass flow of fluid transferred via port  234  in the direction shown by arrow  232  such that the mass flow of the upper and lower streams, for example, transferred into conduit  338  via conduit  286  in the direction shown by arrow  283  when combined with a stream transferred into the lower zone of conduit  288  via conduit  289  will flow in the direction shown by arrow  287  at a rate substantially equal to the velocity of the fat stream transferred into reaction port  338 . Most preferably the velocity of upper and lower streams transferred into reaction conduits such as  245  is substantially the same as the velocity of fluid fat material transferred from port  234  and lateral tube  297 . It can be seen in  FIG. 3  that the profile of each reaction conduit such as  245  changes as it approaches the extraction manifold such as  258 . In fact, the width at region  254  of conduit  245  is substantially increased while the depth is substantially reduced. This causes the three streams transferred into reaction conduit  245  to become flat, parallel sheet-like streams moving in direction shown by arrows such as  251 ,  253  and  257 . In this way, the stream of beef fat material is exposed to relatively large upper and lower surface areas, thereby encouraging rapid reactions. 
         [0045]    Referring now to  FIG. 4 , a series of cross sections through a selected section of 4× laminae or plates  3004 ,  3008 ,  3012  and  3014  are assembled together to provide an exemplary side view of the multiple laminae of the apparatus shown in  FIG. 1 . Ridges (e.g.,  3002 ) in plate  3008  are located around the perimeter of both the upper and lower sides and with similar plate  3014  also having ridges, thereby providing a registration for the alternately stacked plates of  3004  and  3012  to accurately locate relative to adjacent plates  3008  and  3014 . In this way, recesses such as  3070  and  3068  in adjacent plates  3054  and  3058  (which correspond to plates  3012  and  3014 , respectively), provided in the surface of each plate and which are intended to be aligned correspondingly, can be aligned by locating plate  3054  against the ridges of plate  3058  and plate  3096  (which corresponds to plate  3008 ), respectively. In this way the conduits passing through the entire stack of plates such as  3050  and  3020  are easily aligned and lateral conduits such as  3082  and  3070  formed from depressions provided in adjacent plates are readily aligned when the plates are assembled together. Cross section “A-A” passes through lateral and vertical conduits as shown in section “A-A”. 
         [0046]    The purpose of the arrangement shown in connection with  FIGS. 1 through 5  is to enable the exposure of triglyceride molecules to methanol or ethanol with the appropriate catalyst such as L-CO 2  in the most rapid way possible. It is a purpose of this arrangement to sandwich a layer of triglycerides blended with L-CO 2  between two layers on opposite sides comprising methanol and/or ethanol and any other suitable catalyst such as sodium hydroxide if necessary. A blend of L-CO 2  and triglycerides is transferred from conduit  3034  to conduit  3082  and  3073  via vertically disposed connection tube  3032 . The blend enters conduit  3082  at  3077  and similarly fluid enters conduit  3068  at  3073 . Arrows show the direction of flow and the sandwiching fluid comprising a blend of methanol and/or ethanol can be transferred into conduit  3068  via vertical conduit  3042  from one side and via conduit  3071  on the alternate side. The combined three layers then transfer through a blended section at  3048  and  3066  at which point the profile of the circular cross section of a fluid in conduit  3068  changes as it travels through the areas shown as  3048  and  3066  where the fluid is fanned out as it conforms to the change in conduit profile at  3064  and  3062 . The reactive fluid is then transferred into conduit  3050 . In a similar fashion, fluids are transferred into conduit  3026  in the direction shown by arrows  3028  and  3024  and from there through profile changing segment  3023  and into the widened and flattened segment  3022 . Referring now to sections “B-B” and “C-C” as shown in  FIG. 5  firstly, it can be seen in section “C-C” that the triglyceride fluid  3202  is penetrated by oval beads  3214  and  3204 . Referring now to section “B-B” the profile of the triglycerides  3102  and ethanol and/or methanol materials has been divided to provide maximum exposure such that layer  3102  is sandwiched and in close proximity to the fluids shown as  3100  and  3104 . Section “B-B” of  FIG. 5  shows an enlarged view of the reaction enclosure as described in connection with the earlier figures. In this way, maximum exposure between the triglycerides and ethanol and/or methanol is provided thereby rapidly producing bio-diesel and glycerol by ensuring a more complete reaction. 
         [0047]    With appropriate quality control measures in place, the assured consistency of materials produced via the micro equipment and methods herein described provide tightened and more accurate tolerances to the respective reactions and subsequently more consistent production rates where reaction time is measured in seconds as opposed to hours for the current macro bio-diesel production technology commonly used. 
         [0048]    Referring again to  FIG. 3 , in a preferred embodiment, warmed, liquid, filtered beef fat, can also be blended directly with methanol and/or ethanol and then transferred via conduit  234  in the direction shown by arrow  232  and into the ends of reaction transfer conduit such as  288 . Therefore, controlled quantities of feed stock materials useful for production of bio-diesel by way of chemical reaction enhanced by suitable catalysts are directed by transfer through micro conduits directly into reaction tubes, within which solid catalysts can be fixed to the walls, designed to create close and thorough contact of the materials and the alteration of reaction tubes profiled wherein the diameter is reduced in the vertical plane and increased in the horizontal plane in blended gradual profile change wherein at the entry end of reaction conduit such as  3047  in section “A-A” is a circular profile ( FIG. 4 ), as can be seen in section “C-C” ( FIG. 5 ). 
         [0049]    Referring again to  FIG. 4 , a fluid transferred through conduit  3032  is divided between two opposing connection tubes  3075  and  3077 . Opposing recesses  3034  and  3036  in plates  3096  and  3094  create an enclosed conduit when the adjacent plates are in contact. Alternate plates are arranged to mate with each adjacent plate. Ridges such as  3052 ,  3002  and  3056  follow a path around the perimeter of the female plates. As can be seen, male plates such as  3051  (which corresponds to plate  3004 ) and  3094  penetrate the female plates when in contact such that conduits such as  3050  and  3020  are created. Male plate  3054  with adjacent female plates  3096  and  3092  provide a reaction tube  3047  connected at a first end to connection tube  3075  and at a second end to vessel sections  3062  and  3064 . The circular cross sectioned reaction tube  3047  connects via a tapered region  3048  and  3066  to low profile vessel sections  3064  and  3062  in such a way that fluid transferred in the direction shown by arrow  3042  through conduit  3044  contacts fluid transferred through connection tube  3075  intimately. Correspondingly, fluid transferred through conduit  3071  into reaction tube  3047  also contacts fluid transferred via connection tube  3075  on the alternate side of fluid flowing in direction shown by arrow  3074  and collectively three separate streams of fluid combine within reaction tube  3047  and are transferred in the direction shown by arrows  3038  and  3074  through upper and lower tube segments  3070  and  3068  comprising reaction tube  3047  through tapering zones  3048  and  3066  and into low profile vessels  3064  and  3062 . 
         [0050]    Section “A-A” shows a lateral cross section of four assembled and engaging plates  3018 ,  3096 ,  3094  and  3092  and the pathway created by the assembly of said plates. In this assembly, a first fluid is transferred via tube  3032  into reaction tubes  3026  and  3047 , where a second stream of fluid transferred via conduit  3030  and a third fluid transferred via conduit  3076  in the direction shown by arrow  3078  sandwiches said first fluid stream transferred via conduit  3030 . Said first, second and third fluids subsequently combine in a single stream which is transferred collectively in the direction shown by arrows  3028  and  3024  via tapering section  3023  and into low profile sections  3022  and  3086 . Section “A-A” also shows a second reaction tube  3047  wherein a first fluid transferred via conduit  3032  in the direction shown by arrow  3073  is subsequently sandwiched between a fourth fluid stream transferred via conduit  3044  in the direction shown by arrow  3042  and a fifth fluid stream transferred via connection conduit  3071 . The combined stream of first, fourth and fifth fluids is transferred in the direction shown by arrows  3038  and  3074  through tapering sections  3048  and  3066  and into low profile sections  3064  and  3062 . 
         [0051]    Section “C-C” in  FIG. 5  shows a cross section of reaction tube  3206  containing a combined stream of said first fluid  3202  sandwiched between said second fluid  3204  and said third fluid  3214 . Section “C-C” has been illustrated for the purpose of showing the intimate contact of male plate  3208  and female plate  3212  in direct compressed and close contact along interface  3200  wherein reaction tube  3206  is thereby facilitated which enables said first fluid  3202  to be in close and intimate contact with said second fluid  3204  and said third fluid  3214 . The elliptical profile of said second fluid  3204  and said third fluid  3214  are both transformed, after transfer via tapering section  3023  as shown in section “A-A” in  FIG. 4 , into sheet profiled layers  3114  and  3110  shown in section “B-B” in  FIG. 5  sandwiching said first stream  3112 . 
         [0052]    Referring again to section “B-B” in  FIG. 5 , a pair of plates  3098  and  3108  are shown in intimate contact along interface  3102 . This figure shows the profile of vessel  3022  in section “A-A” in  FIG. 4  with said first stream  3112  sandwiched between said second stream  3114  and said third stream  3110 . Section “B-B” indicates how said first, second and third fluid streams  3112 ,  3114  and  3110 , respectively, are in close contact such that the reaction time between said first, second and third streams can be reduced. 
         [0053]    It can be seen, therefore, that first, second and third fluid streams transferred via conduits  3036 ,  3030  and  3076  in section “A-A” are combined in such a way to enable reduced reaction time by altering the combined stream profile of said first, second and third fluids as shown in section “B-B” as layers  3112 ,  3114  and  3110 , respectively. The close proximity of said three streams is facilitated by combining said first, second and third streams into a circular section conduit  3206 , as shown in section “C-C”, which is then transformed into a low profile section as shown in section “B-B”, facilitating the combining of fluids which may repel each other due to a physical property, but which nevertheless, can be encouraged to react by altering the combined stream profile  3104  as shown in section “B-B”. 
         [0054]    Referring now to  FIG. 6 , a view of the entire process is shown by way of diagrammatic representation line drawings. Cattle at  6000  enter the slaughterhouse  6004  along path  6002  and data downloaded from RFID tags which have previously been either embedded in the animals&#39; neck muscles or any other method known in the art. Immediately following slaughter and evisceration, the carcasses are graded in factory represented by square line drawing  6004 . After removal or harvesting from animal carcasses low value fat is transferred via  6008  to processing plant  6010  where either electric power or liquid fuels can be efficiently converted from this by-product. After slaughtering and chilling the animal carcasses, they are transferred via  6006  to processing plant  6012  where the animals are graded and stored. After quartering the animal and downloading information about the animal to RFID tags, special apparatus such as transponders can be arranged to check outgoing beef quarters which are transferred to the adjacent building  6034  where animals are de-boned and sliced to produce retail package cuts of beef and the remaining trim or boneless beef for ground beef production. Some packages are shipped out of  6034  in the opposite direction of arrow  6018 , but the majority of packages are transferred in the direction of arrow  6032 . Approximately 40% of the weight of boneless beef received in  6012  is transferred into an adjacent room  6036  for the purpose of grinding boneless beef. Liquid and gaseous CO 2  is transferred via  6028  from pressure vessel and storage tank  6026 . The boneless beef is treated with a CO 2  snow and can be packaged in barrier chubs and stored in area  6038  after transfer from the factory area  6036  along  6030 . While ground beef can be packaged in chubs, at this point most likely the boneless beef transferred into area  6036  will be graded and grouped into approximately one ton palletized quantities which are typically treated with CO 2  snow. Any chub production would be from the high lean grades such as 85% lean through 94% lean. Boneless beef streams comprise typically grade groupings of 75% VL (75% lean beef) or 65% VL and 50% VL. Lower grade described as 30&#39;s, comprise the remaining fat stream with any quantities up to 30% lean and perhaps 40%. These remaining palletized streams are transferred into separation enclosures via  6042 . In this area, all boneless beef is ground and automatically separated into streams of any quantity ordered by customers such as 85% lean ground beef, all of which may be packaged in barrier chubs or, alternatively, case ready retail packages. The process of separation employs quantities of CO 2  which can be sourced from tank  6026  via conduit  6023  and returned after use for recycling via conduits  6044  and  6024 . Packages shown as  6058  have been packaged in regions  6050  and  6054 . The fat stream removed in area  6040  is then transferred to area  6066 . The stream of white fatty adipose tissue is centrifuged and all proteins removed are returned to area  6040  in the direction shown by arrow  6045  and is then included in ground beef production, all of which is transferred in the direction shown by arrow  6048 . After removal of solids from the fat stream at  6066 , the beef fat which is now in a warm fluid condition is filtered prior to transfer in the direction shown by arrow  6068  to  6070 , where it is combined with a suitable mixture and controlled quantity of liquid CO 2  under appropriate pressure which is then transferred in the direction shown by arrow  6074  to  6086 .  6086  is representative of apparatus shown in  FIGS. 1 through 5 ,  7  and  9  through  10 . Bio-diesel and glycerol are produced in this way and glycerol is transferred in the direction shown by arrow  6076  to storage area  6080  where the viscous liquid glycerol is refined and transferred to customers at  6084  in the direction shown by arrow  6082 . Bio-diesel transferred in the direction shown by arrow  6088  and stored at  6092  can be filtered and further refined using the method described below. Refined bio-diesel is transferred via  6094  to processing area  6096  where fossil fuel diesel transferred from  6100  in the direction shown by arrow  6098  is blended with said bio-diesel to produce a range of bio-diesel and fossil fuel diesel blends such as B 2  and B 20 . B 2  represents a blend of diesel wherein 2% bio-diesel has been added. B 20  represents diesel fuel containing 20% bio-diesel and 80% fossil fuel diesel. These finished fuels are transferred in the direction shown by arrow  6102  for use as fuel in automobiles, or any engine such as trains, electric generators, and the like. 
         [0055]    Referring now to  FIG. 7 , yet another preferred embodiment is shown by way of a diagrammatic representation of a pair of spinning discs traveling in opposite directions. Housing  7010  encloses a pair of machined matched discs  7030  and  7028 . The purpose of this apparatus is for production of bio-diesel and glycerol from, most preferably, animal fats derived from unwanted beef fat. In order to produce bio-diesel and glycerol, the reactive ingredients are desirably blended together at a suitable temperature such as 70° F. or between about 65° F. and about 130° F. 
         [0056]    A disc  7030  manufactured from a suitable material such as 316 stainless steel which has been machined and surface treated, is shown. Disc  7030  is fixed rigidly to centrally located perpendicular first drive shaft  7004  via boss and bearing housing  7006 . A second disc  7028  is shown adjacent to and parallel with disc  7030 . Disc  7028  is mounted to a boss  7020  with suitable bearing means and to a second drive shaft  7022 . Drive shaft  7004  desirably comprises a heavy wall tube manufactured from a suitable material such as stainless steel and is provided with conduit  7002  thereby allowing fluid to be transferred there through, for example, in the direction shown by arrow  7000 . Conduit  7002  can be provided with drive means such as a variable speed electric drive that can rotate shaft  7004  in the direction shown by arrow  7001 . A series of apertures such as  7034  extending along a path parallel with machined disc  7030  and around the circumference of boss  7006  communicate directly with conduit  7002 . Shaft  7022  can be provided with a driving motor capable of driving in either direction and at any selected speed. Conduit  7024  communicates with a series of apertures such as  7029  wherein said apertures follow a path parallel and adjacent to said first series of apertures  7034 . A diffusing disc  7027  extends around the perimeter of apertures  7034  and also apertures  7029 . It should be noted that a diffusion disc such as  7027  could be manufactured with a barrier splitting said disc  7027  along a plane parallel with rotating discs  7030  and  7028 . The assembled apparatus shown in  FIG. 7  is also provided with an enclosing cover  7010  which encloses a space around and close to parallel discs  7030  and  7028 . Enclosure  7010  is provided with a conduit  7012  which can transfer fluids there through in the direction shown by arrow  7014 . The purpose of the apparatus shown in  FIG. 7  is to provide a reliable and efficient means of manufacturing bio-diesel. A fat stream at a suitable pressure such as between 400 and 600 psi (pounds per square inch) can be transferred in the direction shown by arrow  7000  into conduit  7002 . The catalysts (e.g., sodium hydroxide and/or L-CO 2 , with water as required) and methanol and/or ethanol can be transferred under pressure corresponding with the pressure of triglyceride fats transferred through conduit  7002  and in the range of 400 to 600 psi. Parallel discs  7030  and  7028  are arranged in close proximity and with space of between 100 and 200 microns, and an example of providing the space is shown in section “X-X” where radial ridges  8010  and  8004  which correspond with ridges  7019  and  7018  provide spaces such as  8008  and  8002 . In this way, triglyceride fats transferred through radial holes such as  7034  and then through upper section through diffuser  7027  can pass between said discs  7030  and  7028 . Correspondingly, fluids transferred in the direction shown by arrow  7026  through conduit  7024  in shaft  7022  and then through annular apertures such as  7029  and then through the lower segment of diffuser  7027  can also transfer into space between rotating discs  7030  and  7028  at a controlled rate. Fluids transferred through conduit  7002  can, in this way, travel through a radial space parallel with disc  7030  and toward the perimeter thereof. Fluids pumped at a controlled rate in the direction shown by arrow  7026  also communicate with conduit  7024  and radial apertures such as  7029  and into the space between discs  7030  and  7028 . Therefore, in this way fluids transferred through conduit  7002  contact fluids transferred through conduit  7024  between said discs  7030  and  7028  first coming into contact after passing through diffuser ring  7027  and into said annular space between discs  7030  and  7028 . Therefore, in this way fluids transferred through  7002  come into intimate contact with fluids transferred through  7026  in the annular space between said discs  7030  and  7028 . Disc  7030  can be driven in the direction shown by arrow  7008  at a speed of, for example, between 5000 and 15000 rpm while disc  7028  can be driven in the direction shown by arrows  7009  and in the opposite direction of arrow  7008 . Fluids passing between said rotating discs  7030  and  7028  are thereby exposed to very high shear. Furthermore, fluids become mixed continuously at high speed and are unable to stratify or escape the high shear and severe blending conditions between said discs  7030  and  7028 . Conduit  7012  can be connected directly with a suitable valve and pumping arrangement with flow regulators maintaining a suitable pressure in the space between rotating discs  7030  and  7028  and enclosure  7010 . Fluids therefore are able to react during the time they are enclosed between said rotating discs and before transferring into the enclosed space within enclosure  7010  through radial slots such as  7036 . Said discs  7030  and  7028  can be held together by mechanical pressure with contact restricted by ridges such as  7019  and  7018 . The apparatus shown in  FIG. 7  can be arranged with multiple pairs of discs corresponding with multiple parallel rows of apertures such as  7034  and  7029 . In this way, manifolds may be arranged, for example, within boss  7006  and  7020  such that streams of materials and fluids can be transferred between each pair of plates such that a quantity of fluid transferred through conduit  7002  will be transferred into the space between each pair of discs and correspondingly fluids transferred through conduit  7024  can also be transferred between each set of rotating discs in a similar fashion to the description herein such that fluids from conduit  7002  come into intimate contact with fluids transferred through conduit  7024  and are then subjected to high shear as the fluids are pumped through the space between each set of plates. 
         [0057]    Referring again to  FIG. 7  and the disclosure above, the apparatus shown can be used to produce bio-diesel and any other fluid derived from ingredients that may or may not mix well together. The purpose of this apparatus is to ensure thorough mixing of fluids in proportionate quantities as required or desired by the reactions to facilitate the bringing together of all components needed for a particular reaction on a “micro” scale. 
         [0058]    Referring now to  FIG. 8 , an organic chemical reaction is shown with triglyceride and methanol molecules shown in proportionate quantities to the left of the arrow pointing toward the resultant organic chemicals of the reaction, one fatty ester molecule and one glycerol molecule. As can be seen for each triglyceride molecule, three molecules of methanol are required to produce a single fatty ester molecule and a single glycerol molecule. 
         [0059]    Referring now to  FIG. 9 , an apparatus is shown in a three dimensional cross sectional view. The apparatus shown in  FIG. 9  is intended for use in the production of fatty esters or bio-diesel and glycerol from raw materials comprising, for example, clean, filtered beef fat or tallow elevated in temperatures such that its flow characteristics are as needed to efficiently facilitate blending with methanol and/or ethanol and a catalyst such as sodium hydroxide, potassium hydroxide, but most preferably, CO 2  which may be used either as a sub-critical or in super-critical fluid phase. The apparatus comprises a series of concentric members wherein a conduit  9024  with liquid transferred there through in the direction shown by arrow  9022  is fitted with a flange section having a substantially flat face. In diametrically opposing position, a similar member comprising conduit wall  9076  with conduit  9078  is arranged to retain flange portion with center line  9023  common to both members  9076  and  9025 . Conduits (not shown) are sealingly attached to each member  9025  and  9076  such that fluid at a selected temperature and pressure can be transferred in the direction shown by arrows  9022  and  9080 . Enclosing members  9025  and  9076 , a pair of members  9027  and  9086  with spaces  9014 ,  9094 ,  9068  and  9036  are concentrically arranged such that the inner surface profile of said members  9027  and  9076 , when in operating position as shown in  FIG. 9 , generally follows the outer profile of members  9025  and  9076 . Enclosing members  9027  and  9086 , outer housing members  9028  and  9016  are arranged with spaces  9008 ,  9092 ,  9062 ,  9037  and  9013 , such that there is no contact between the outer members  9028  and  9090  with inner members  9086  and  9027 . The apparatus in  FIG. 9  generally comprises three pairs of opposing members, each pair retaining pressurized fluids. Cross section “A-A” (A) shows a cross sectional profile of the contacting surfaces of members  9027  and  9072 . As can be seen, member  9027  is arranged with radially extending ridges  9900  and  9902  with spaces  9904  and  9906 , for example, so that the contacting ridges such as  9900  and  9902  press against the parallel inner flat surface  9910  of member  9908 . Member  9908  of section “A-A” corresponds with member  9072 , and member  9912  in section “A-A” corresponds with member  9027 . Each pair of members such as  9025  and  9076  are separately and independently mounted to driving means such that, for example, member  9076  can be activated so as to apply pressure in the direction shown by arrow  9080  at which time, member  9025  can be held in rigid disposition. Similarly, member  9908  can be compressed toward member  9912 , thereby applying a controlled pressure to the face of ridges such as  9900  and  9901 . Applying pressure in this way can cause generation of heat through friction when member such as  9908  is rotated in the direction shown by arrow  9909 , either when member  9912  is held stationary or, alternatively, member  9912  can be rotated in the direction shown by arrow  9903 , by any suitable independent driving means. Each pair of members such as  9025  and  9076  or  9072  and  9027  can be rotated by variable speed driving means such that any suitable speed of rotation can be arranged. In operation, manifolds are provided to transfer pressurized fluids to each space between the concentric members, for example, members  9025  and  9027  and members  9027  and  9028  can be arranged to transfer pressurized fluid in spaces  9026 ,  9037 ,  9014 ,  9013 , and/or  9024  in the direction shown by arrows  9022 ,  9020  and  9018 . Additionally, fluids can be transferred from any suitable source via a suitable manifold arranged to transfer said fluid into conduit  9078  in the direction shown by arrow  9080  or in the direction shown by arrow  9084  into space  9094  and, in doing so, provide streams of fluid that will follow the internal profile of member  9086  and the outer profile of member  9076  through spaces  9094  and  9068  and then in the direction shown by arrows  9097  and  9066 . Similarly, fluid transferred into conduits  9024  and  9078  in the direction shown by arrows  9022  and  9080 , respectively, will follow the internal contour of conduits  9078  and  9024  in the direction shown by arrows  9080  and  9022 , respectively. Said fluid transferred into the central conduits  9024  and  9078  can transfer through spaces  9096  and  9032  radially extending outward and away from center line  9023  and into space such as  9010 . Fluids transferred via  9014  in the direction shown by arrow  9020  and into space  9094  in the direction shown by arrow  9084  can contact with other fluids transferred in the direction shown by, for example, arrows  9012 ,  9034 ,  9066  and  9097  and can reach the annular space  9010  immediately prior to transfer through annular space such as  9102  in a radially outward extending direction, as shown by arrow  9040 . In this way, fluids such as beef fat having been suitably refined and transferred through radial spaces  9096  and  9032  in the direction shown by, for example, arrow  9030  can be encapsulated or sandwiched within a fluid, such as super-critical CO 2 , transferred through, for example, spaces  9014  and  9094  in the direction shown by arrows  9012  and  9034 . Fluids transferred through conduits and spaces such as  9094 ,  9014 ,  9026 ,  9036  and  9068  can be heated as a consequence of friction between the faces enclosing spaces such as  9096  and  9032  by rotating members  9076  and  9025  in opposing directions and/or by applying pressure simultaneously in the direction shown by arrows  9080  and  9022 , whereby heat is generated in direct proportion to the energy spent in compressing the members together while rotating. In this way, sub-critical liquid CO 2  transferred through a space such as  9014  can be heated to, for example, above 100° F., therefore, causing super-critical phase to occur. Fluid transferred in the direction shown by arrow  9018  through space  9013 , or alternatively through conduit  9110  in the direction shown by arrow  9108  and through space  9050  in the direction shown by arrow  9052  can be arranged to reduce the combined temperature of fluid transferred from annular space  9010  through  9056  in the direction shown by arrow  9040 . The profile of each member can be arranged to create restriction or provide more space for fluids being transferred under suitable pressure through each annular space. Temperature can be controlled by either developing heat through friction as described above or the temperature of any fluid can be reduced when combined with a fluid of a lower temperature transferred in controlled mass flow via space  9050  in the direction shown by arrow  9052 . Fluids transferred through space  9013  in the direction shown by arrows  9006  and  9002  may be combined with fluids transferred through conduit  9106  and conduit  9048  prior to contacting fluids transferred through spaces  9102  and  9056  in the direction shown by arrows  9012  and  9040 , respectively, at a confluence with fluids transferred through  9004  in the direction shown by arrow  9014 . With the apparatus as shown in  FIG. 9 , all fluids may be transferred, ultimately into conduits  9078 ,  9094 ,  9014 ,  9013  and  9106  and combined in layers which can be thoroughly blended by the rotating of members such as  9086  or  9090  in opposing relative directions. In each case where opposing faces provide space through which fluids can be transferred, the respective members can be arranged to apply pressure and to generate heat which can be precisely controlled so as to suit a particular reaction. In this instance, such a method of generating a controlled quantity of heat can be used to convert sub-critical liquid CO 2  to a super-critical phase, thereby inducing the aggressive solvent property of super-critical CO 2  which can then be blended with, for example, beef or plant oils such that when such mixture is added to a controlled quantity of methanol and/or ethanol, bio-diesel and glycerol can be produced. The apparatus shown in  FIG. 9  indicates several conduit spaces which can provide for blending of up to six or more fluids together. However, in the production of bio-diesel, the fluids typically include a proportionately controlled blend of liquid CO 2  and beef fat maintained at a temperature such that both are in fluid state, which is then combined with liquid methanol and/or ethanol. Catalyst sodium hydroxide or similar optionally can be eliminated. 
         [0060]    The apparatus shown in  FIG. 9  is arranged such that the distance between the opposing faces, each side of spaces  9032  and  9097  will most preferably be on the order of 0.004″ or 100 microns and similarly, spaces at  9056  and  9102  defined by parallel surfaces of faces such as  9912  and  9908  shown in section “A-A” (A) can also be arranged at a distance of 100 microns between the faces. The distance between radial ridges such as  9902  and  9900  can be as much as 1.0″, however, a preferred dimension for distance B as shown in section “A-A” (A) will be 200 microns. Ridges such as  9900  and  9902  as shown in section “A-A” (A) allow fluid to be transferred through spaces  9904  and  9906 . When member  9912  is rotated in a direction such as shown by arrow  9903 , opposite to the direction of member  9908  shown by arrow  9909 , fluid transferred through spaces  9904  and  9906  can be thoroughly blended while controlled heat generated by friction at the ridges such as  9900  and  9902  can be advantageous to the reaction of fluids in said spaces. For example, beef fat or oil is not miscible with methanol and, in fact, the fluids of methanol and beef fat tend to separate, therefore, providing a difficult condition for reaction between methanol and beef fat. However, by proportionately controlling a mixture comprising measured quantities of fluid beef fat, methanol and CO 2 , the rotating action of member  9912  against member  9908 , results in the transfer of fluid in  9906  between the face of ridge  9902  and member  9908  and thereby subjecting this fluid to extreme pressure. Also, fluid in space  9904  is transferred via the minute space between  9900  and the flat face of member  9908 . Fluid transferred between said spaces is similar in volume across the face of all ridges such as  9900  and  9902  and this action can provide an aggressive mixing action for fluids being transferred through spaces such as  9904  and  9906 . Furthermore, long carbon chain molecules such as triglycerides can be stretched or contorted while transferring through the narrow spaces between a ridge such as  9900  and a face, such as  9908 . 
         [0061]    Referring again to  FIG. 9  and, in particular, section “A-A” (B), ridges  9932  and  9930  are shown with a wedge profile such that gaps  9931  and  9937  enables fluid transfer via space  9934  and  9936  to be forced into said gaps  9937  and  9931  and compressed such that any large molecules such as triglycerides can be stretched or, alternatively, any fluids transferred through spaces such as  9934  and  9936  are thoroughly blended when rotating member  9942  is rotated in the opposite direction to the arrow  9934  against the stationary member  9938  or, alternatively, when member  9938  rotates in the direction opposite to the direction shown by arrow  9939 . Section “A-A” (B) shows the alternative profile ridges, however, other aspects are similar to those of section “A-A” (A). More particularly, spaces  9934  and  9936  are exemplary and representative of all such spaces provide along the radial band following a path wherein member  9072  and member  9027  are held together under pressure and where contact between the two members occurs only at the ridges such as  9930  and  9932 . In this way, high pressure, such as 10,000 lbs per square, inch can be applied to the points of contact between said member  9942  and member  9938  of section “A-A” (B). 
         [0062]    Referring now to  FIG. 10 , a cross section through an apparatus similar to the apparatus disclosed above in association with  FIG. 9  is shown. Outer housing at  10024  is provided to enclose a series of rotating members including  10020 ,  10004  and  10100 . Each member such as  10024  is connected directly to a rotating means and conduit which enables the pressurized temperature controlled transfer of fluids in the direction shown by arrows  10180  and  10012  and through channel provided by spaces such as  10164  and  10040 . Fluids transferred between members  10020  and  10024  follow a conduit outwardly in the direction shown by arrows  10176  and  10036 . The plan shows a circular profile to the apparatus shown in  FIG. 10  and the members  10004  and  10100  can be rotated at any selected speed and in opposite directions such that fluid transferred into conduit such as  10016  are transferred through the conduit  10016  and in the direction shown by arrows  10184 ,  10008 ,  10172  and  10028 . Member  10100  is fixed rigidly to a driving means and is located in apposite disposition to member  10004  and can be rotated about a common center line  10000  which is common with member  10004 . Cross section “X-X” shows the end view of a segment shown by line X-X and tapered rollers  10268 ,  10208 ,  10212  and  10236  are held captive in recesses of member  10220  with radial channels  10200 ,  10204 ,  10216  and  10228 , radiating from center line  10000  which connects directly with channel  10016 . In the upper member  10228 , which corresponds with member  10020  in opposing member  10244  which corresponds with member  10091 , members  10020  and  10091  rotate in opposite directions as shown by arrows  10224 , member  10244  and  10248  in section “X-X”. Member  10244 , which corresponds with rotating member  10091  is shown with radiating channels  10264 ,  10256 ,  10252  and  10240  radiating from center line  10000  and communicating directly with channel  10096 . Rollers  10268 ,  10208 ,  10212  and  10236 , shown in section “X-X” are arranged to be retained by recesses in member  10220  and held against opposing flat inner surface of member  10244 . Therefore, as member  10220  rotates in the direction shown by arrow  10224 , member  10244  may be held stationary or rotate in the direction shown by arrow  10248 . Under these conditions, rollers such as  10268  and  10208  are rotated in a clockwise direction when viewed as shown in section “X-X”. It can be seen that fluid transferred through conduit  10016  in the direction shown by arrows  10184 ,  10008 ,  10172  and  10028  after passing through micro conduits such as  10044  and  10160 , the channel shown as  10232  in section “X-X” will enable the direct transfer of said fluid transferred through conduit  10016  and into space around tapered rollers such as  10268  and  10208 . Conversely, fluid transferred through conduit  10096  in the direction shown by arrows  10112 ,  10108 ,  10092  and  10120  will communicate via micro channels  10076  and  10132  and as shown in section “X-X”. After transfer through micro conduit such as  10264  and  10256  in member  10244 , the fluid having been transferred most preferably under selected pressure and at a selected temperature via conduit  10096  will contact tapered rollers such as  10268 ,  10208  and  10236  in section “X-X”. It can be seen, therefore, that when a selected first fluid such as methanol is transferred through, for example, conduit  10096  in the direction shown by arrow  10108  and a second beef tallow fluid is transferred via conduit  10016  in the direction shown by arrows  10008  and  10028 , both first and second fluids can meet and contact around the space between rollers such as  10268  and  10208  and the recesses in member  10220  retaining said tapered rollers under temperature and pressure control, when the second fluid has rate of mass flow proportionate to said first fluid transferred through conduit  10096 . The two fluids will make contact with each other as rollers  10268  and  10236 , for example, are rotated in a clockwise direction when viewed according to section “X-X”. Furthermore, pressure can be applied to both members  10020  and  10091  in the direction shown by arrows  10184  and  10012  and controlled pressure can also be applied to member  10091 . The only point of contact between members  10091  and  10020  is via said tapered rollers such as  10268  and  10236 . Said pressure applied via said roller such as  10268  can be controlled so as to provide a most efficient process such that when said first and second fluids are in contact in space around roller such as  10268 , pressure applied to members  10020  and  10091  is applied to the blended first and second fluids also. The rate of mass flow of said first and second fluids, the pressure applied via members  10020  and  10091  and the rotational speed of member  10020 , corresponding with member  10220 , in the direction shown by arrow  10224  against member  10091 , corresponding with member  10244 , rotating in the direction shown by arrow  10248  can be controlled at any suitable speed, but most preferably, on the order of 1,000-2,000 rpm or, alternatively, up to 10,000 rpm or more or less.  FIG. 10  shows that fluid can also be transferred in the direction shown by arrows  10180 ,  10012 ,  10176  and  10036  continuing in the direction shown by arrows  10156  and  10048  via channel  10052  so as to blend with fluid transferred through conduit  10060  in the direction shown by arrow  10056  and conduit  10152  in the direction shown by arrow  10148 . Fluid transferred in this way can combine and collectively travel in the direction shown by arrow such as  10068  and  10140  so as to then blend with combined fluids transferred via conduits  10016  and  10096  in conduit  10124  and  10084 . Finally, the combined fluids transferred into the apparatus shown in  FIG. 10  can be transferred via conduit  10124  and  10084  in the direction shown by arrows  10116  and  10104 . 
         [0063]    Referring again to  FIG. 10 , most preferably the apparatus can be used to produce bio-diesel at a high rate of production by ensuring the correct and thorough blending of immiscible fluids, such as methanol and fluid beef tallow or oil. The method described in association with  FIG. 10  provides a series of radially located rollers such as shown in section “X-X”, rollers  10268 ,  10208 ,  10212  and  10236 . Any convenient quantity of radially located rollers similar to those shown in section “X-X” can be provided around the full annular band created by the contact point of all rollers rotating in recesses such as shown by rollers  10268 ,  10208 ,  10212  and  10236  in section “X-X”. All rollers can be fitted and retained by recesses in a first member such as  10220  so as to rotate and roll across the annular band that said rollers can contact. Said first member  10220  may rotate in the direction shown by arrow  10224  in opposing disposition to said second member  10244  rotating in the direction shown by arrow  10248  and said members  10020  and  10091  may be held under pressure so as to clamp said rollers such as  10268  and  10236  shown in section “X-X”. Fluid transferred via radial micro conduit such as  10200  and  10264  can be blended thoroughly by the action of said rollers such as  10268  in the confinement of the space between the respective components including member  10220  and opposing member  10244  which apply pressure to fluids as they are blended by transfer through the respective micro conduits such as  10268  in member  10244  and via micro conduit such as  10204  in member  10220  of section “X-X”. Furthermore, it should be noted that when large molecules of organic compounds such as triglycerides are provided under fluid pressure in the manner described herein above then subjected to confinement between hardened tapered rollers such as  10268  in section “X-X”, the molecules can be stretched and when in a stretched condition are more likely to react with other elements or compounds such as methanol or ethanol. 
         [0064]    The apparatus described in association with  FIG. 10  (and  FIG. 9 ) provides a series of annular conduits through which miscible or immiscible fluids can be transferred for the purpose of blending together in a confined space. When blending such immiscible or miscible fluids in a confined space and subjecting the fluids to an intense mixing action, the desired reaction can occur rapidly and within the confinement of the space provided. After transferring into the confined space around rollers such as  10268  and  10236 , etcetera and being subjected to intense blending action facilitated by the confined rollers, a more complete reaction between the fluid compounds can occur. Referring again to  FIG. 10 , it should be noted that the fluids transferred through the annular passageway shown are provided under controlled pressure at a selected temperature and each annular conduit is separated from adjacent annular conduits by manifold attachments provided with suitable seals and bearings. Pressure provided via members such as  10004  and  10100  rotating in the opposing direction shown by arrows such as  10008  and  10108  can be provided by hydraulic piston and suitable retaining sleeve. The hydraulic liquid of the piston may be the fluid being transferred. A suitable screw and thread arrangement can be provided such that when a selected pressure has been facilitated, a lock nut can be arranged to fix the desired pressure for the duration of the production run. 
         [0065]    Referring again to  FIG. 10 , the preferred embodiment is shown in the apparatus and according to the disclosure above provides a means of producing bio-diesel and glycerol from, for example, beef fat and methanol using liquid phase or super critical CO 2  as the catalyst, enabling reaction between the triglycerides of the beef fat and methanol and/or ethanol. The reaction occurring is as shown in  FIG. 8  wherein three methanol molecules and a single triglyceride molecule react to produce a mixture of fatty esters and a single glycerol molecule. The volume of bio-diesel (fatty esters) produced is approximately 10 times the volume of glycerol produced when manufactured with apparatus similar to that shown in  FIG. 10  (or  FIG. 9 ) and, in particular, when CO 2  is used as catalyst. The requirement of washing with large quantities of water to separate any sodium hydroxide or potassium hydroxide, catalyst may be eliminated. More particularly, when using the apparatus described in  FIG. 10 , the production process is much more rapid, does not require large quantities of water and any remaining CO 2  catalyst evaporates when exposed to ambient conditions. 
         [0066]    In another preferred embodiment, bio-diesel and glycerol produced in the manner described in association with  FIG. 10  can be processed so as to crystallize glycerol and fatty esters by lowering the temperature to below the freezing point of these two products. More particularly, a mixture of glycerol fatty esters (bio-diesel) and L-CO 2  can be transferred through a similar aperture or nozzle into an expansion chamber wherein the pressure drop across the nozzle is sufficient to freeze the glycerol and bio-diesel, thereby causing it to crystallize while maintaining the majority of the CO 2  in liquid phase. For example, a pressure drop from 500 psia down to 350 psia will reduce the temperature well below the crystallizing point of bio-diesel and glycerol. A resultant blend of crystallized glycerol, crystallized bio-diesel and L-CO 2  can then be transferred to a suitable separation apparatus. The blend of crystallized glycerol and bio-diesel with L-CO 2  can be separated by centrifuging in an enclosed pressurized decanter style centrifuge. The density of glycerol is 78 lbs per cu.ft., while the density of bio-diesel is 58 lbs per cu.ft. The density of L-CO 2  can be adjusted such that bio-diesel will float and glycerol will sink under normal gravitational conditions. However, when transferred in continuous stream through a centrifuge separator, the solid, crystallized glycerol can be readily separated from the L-CO 2  and crystallized bio-diesel. Subsequently, the L-CO 2  can be separated from the crystallized bio-diesel. Any moisture present will be evaporated during the process and the crystallized bio-diesel can then be heated until liquid phase is reached. In this way, glycerol of high quality without impurities can be manufactured when using CO 2  in either liquid or dense vapor phase as the separating medium and catalyst. 
         [0067]    Referring to  FIGS. 1 through 5  and  FIGS. 7 and 9  through  10 , two sets of apparatus for the production of bio-diesel are disclosed. The purpose of this apparatus is to provide effective and efficient manufacture of bio-diesel and glycerol with equipment of substantially reduced physical dimensions when compared to typical bio-diesel plants currently in use. 
         [0068]    Following the production of bio-diesel and glycerol in a single continuous stream emanating from conduit  7012  in  FIG. 7  and manifolds  7000  and  4088  in  FIG. 1 , it may be desirable to separate bio-diesel from the mixture of components in a single stream and to ensure that it can be cleaned and then isolated in storage vessels prior to use as a fuel; also glycerol can be separated from the stream and isolated in separate storage. 
         [0069]    The following lists properties of the preferred components involved in the production of bio-diesel and glycerol according to the above disclosures; 
         [0000]    
       
         
               
             
               
               
               
               
               
               
             
           
               
                   
               
               
                 Specific Gravity Chart 
               
             
          
           
               
                   
                 Matter (and 
                   
                 Approx- 
                   
                   
               
               
                   
                 Abbreviated 
                 Process 
                 imate 
                 Solid or 
               
               
                   
                 Identifying 
                 Temperature 
                 Melting 
                 Liquid 
                 Density 
               
               
                 Item 
                 Mark) 
                 Range 
                 Point 
                 (@31° F.) 
                 Lbs/cu′ 
               
               
                   
               
               
                 1 
                 Glycerol 
                 &gt;29°-&gt;90° F. 
                 18° C. 
                 Solid 
                 78 
               
               
                 2 
                 Methanol 
                 &gt;29°-&gt;90° F. 
                 −65° C.  
                 Liquid 
                 49 
               
               
                 3 
                 Liquid Carbon 
                 &gt;29°-&gt;90° F. 
                 −57° C.  
                 Liquid 
                 58 
               
               
                   
                 Dioxide 
               
               
                   
                 (L-CO 2 ) 
               
               
                 4 
                 Water (H 2 O) 
                 &gt;29°-&gt;90° F. 
                  0° C. 
                 Solid 
                 62 
               
               
                 5 
                 Bio-diesel 
                 &gt;29°-&gt;90° F. 
                 20° C. 
                 Solid 
                 58 
               
               
                 6 
                 Tallow 
                 &gt;29°-&gt;90° F. 
                   
                 Solid 
                 55 
               
               
                   
                 (Beef fat) 
               
               
                   
               
             
          
         
       
     
         [0070]    The Specific Gravity chart above lists six preferred components associated with the reaction to produce bio-diesel as disclosed herein. The approximate melting point of each component is also shown with the temperature range of the reaction. The reaction as proposed between methanol and triglycerides produces glycerol and bio-diesel in a single stream and it is therefore desirable to separate the components of the resultant stream prior to using the products after manufacture. A decanter style centrifuge has the capacity to separate crystallized glycerol from the bio-diesel by using the correct style of decanter centrifuge which should be enclosed and able to withstand a pressure of approximately 500 psi. The blend may be continuously transferred into the decanter style centrifuge. Crystallized glycerol with a specific density of 78 lbs/cu.ft. is the most dense of the six materials listed in the above table (assuming all six components are present; it should be noted that the quantity of the methanol component can be substantially reduced when L-CO 2  is present and used as the catalyst and carrier or medium and the micro apparatus utilizing reaction conduits of approximate dimension 100 microns×200 microns or less or more), therefore methanol would be the first material to separate and settle against the inner surface of the rotating bowl of the centrifuge. The entire stream of fluids can be transferred through a restriction in the conduit through which it is flowing such that the controlled pressure drop across the restriction is sufficient to cause a temperature drop as required to solidify any component contained within the stream, as desired. For example, assuming that the temperature of the stream is about 75-80° F. and at a pressure of about 1,100 psi immediately after the reactions are complete, the stream could be transferred through a small orifice of suitable size such as 0.125″ diameter to about 0.25″ diameter thereby causing a substantial reduction of temperature; and when the temperature drops to &lt;18° C., all glycerol will solidify and the smaller the orifice is, the smaller will be the crystals of glycerol. Transferring said stream through a small aperture, thereby facilitating a significant pressure drop, into a vessel of sufficient volume (or comparable conduit), controlled at about 500 psi will ensure smaller crystals are formed as the selected pressure drop enables crystals of the selected component to solidify. The pressure drop could, for example, be arranged to occur as the stream is transferred into a decanter style or other suitable centrifuge. Bio-diesel is also crystallized at the lower end of the proposed temperature range and with a specific gravity of 58 lbs/cu.ft. can float on L-CO 2  when the pressure in the centrifuge is elevated to 600 psi. Therefore a procedure can be followed whereby in a first pass through a decanter style centrifuge, pressure can be held at an elevated pressure, say of approximately 600 psi and 34° F. when only the glycerol and water of the above six components will separate out and fall away from the center of the centrifuge and be held against the inner wall of the centrifuge thereby enabling separation with a standard screw conveyor. Glycerol can then be washed with an adequate quantity of water sprayed into the outer beach region of a decanter style centrifuge through which the glycerol is transferred. In this way, glycerol can be thoroughly washed without requiring copious quantities of water. The remaining fluid transferred from the first centrifuge pass, which may contain methanol, L-CO 2  and bio-diesel, can be transferred to a second or third decanter style centrifuge operating at an internal pressure of approximately 600 psi and a temperature of 30° F. In this case, bio-diesel will be the heaviest, or that component with the highest specific gravity, and will therefore settle against the inner wall of the centrifuge bowl, enabling removal by the conveyor (Archimedes screw). Methanol will accumulate as the inner most layer in the concentric layers of the operating decanter style centrifuge. A dam or weir at an end of the centrifuge can be provided to enable the removal of liquid methanol which has a very low freezing point and will therefore remain liquid during this process at 30° F. Finally, L-CO 2  can be boiled off to atmosphere, or alternatively filtered and recycled. 
         [0071]    Referring again the Specific Gravity Chart, a list of six components representing components that may be present during the production of bio-diesel is provided. However, the process is not limited to just these six components. Solid catalysts such as silica may be used in a bio-diesel production process, for example, and other catalysts are also appropriate for use as long as they can either be fixed to the inner surface of the process reaction tubes (see above) or alternatively provided as a suspension or solution blended with the stream of components. 
         [0072]    Referring now to  FIG. 11 , a diagram comprising a series of rectangles with connective arrows shows steps in a production configuration that can be arranged to produce bio-diesel and other components of a chemical reaction that uses plant matter as a source of triglycerides to produce bio-diesel. Rectangle  11002  represents an apparatus capable of grinding, chopping or generally cutting a stream of plant matter into very small pieces which can then be pulverized in equipment  11006  wherein a transfer conduit  11004  can be arranged to automatically transfer the processed plant matter to pulverizer  11006 . Conduit  11008  transfers the pulverized plant matter to a pumping station  11010  wherein a selected quantity of the pulverized plant material is compressed into a conduit by way of a reciprocating piston with connecting rod attached to a crank shaft (not shown in detail) wherein said crank shaft revolves at a suitable speed, thereby providing a reciprocating piston action such that said piston compresses a quantity of pulverized plant matter into said conduit followed by the opening of a space in said conduit, allowing a subsequent quantity of pulverized plant matter to be transferred therein which is then also compressed against the plant material having been compressed in the immediate earlier compression stroke of said reciprocating piston. 
         [0073]    In this way, plant matter can be progressively transferred from apparatus  11002  through said conduit  11004  in a tightly compacted condition, then pulverized in enclosed apparatus  11006  and pumped through conduit  11008  and combined with L-CO 2  transferred from storage source vessel  11003  through conduit  11005 . The blended stream of plant matter and L-CO 2  is then transferred via high pressure pump  11010  at a controlled temperature above 87.87° F. and higher than the critical pressure 1070 psia. Said first conduit inhibits the escape of L-CO 2  from said second conduit due to the tightly compacted condition of the plant matter sealing any pathway there through. In this way, pulverized plant matter can be mixed with L-CO 2  to provide a mix of L-CO 2  and pulverized plant matter in a continuous stream transferred under a selected pressure and temperature. Said homogenous blend of pulverized plant matter and L-CO 2  may also be transferred from said second conduit into a third conduit via a check valve. Said blend of pulverized plant matter and L-CO 2  can then be transferred through said third conduit and heated to a temperature by way of one or more band heaters provided in tight contact around said third conduit, thereby also elevating the temperature of the combined blend of L-CO 2  and pulverized plant matter to a pressure and temperature above the minimum threshold for super-critical CO 2 , thereby causing a phase change of said L-CO 2  to super-critical condition. In this way, plant matter having been pulverized and then blended with L-CO 2  can be compressed together with super-critical phase CO 2 . In this way, any fats or oils contained in the pulverized plant matter can be separated in a miscible blend with super-critical CO 2 . 
         [0074]    Referring again to  FIG. 11 , compressor  11010  elevates the pressure of said blended stream of L-CO 2  and pulverized plant matter such that L-CO 2  changes phase to a stream of super-critical phase which can then be transferred through high pressure conduit  11011  to centrifuge  11013  where liquefied oil can be removed from the pulverized plant matter and transferred through a high pressure conduit  11011  to centrifuge  11013 . 
         [0075]    Centrifuge  11013  shall most preferably be a vertically disposed decanter style and built in such a manner that the pressure exerted internally by the expanding force exerted by super-critical CO 2  will be safely contained. Centrifuge  11013  can be provided with at least two extraction ports through which a first stream extraction port oil separated from said pulverized plant matter can be extracted in the direction shown by arrow  11012  and a second stream of pulverized plant matter extracted is transferred via a second conduit  11014  to storage container  11020 . Oil transferred via conduit  11012  is blended with L-CO 2  and a quantity of methanol equal to about 5% of the total volume, and the combined materials are blended and heated in vessel  11016 . Blended materials comprising super-critical phase CO 2  and methanol are blended with oil extracted from said pulverized plant matter and the temperature and pressure of the combined blend of materials are elevated to approximately 250° F. and 150 atmospheres. 
         [0076]    Referring again to  FIG. 11 , in another preferred embodiment, the method of grinding and, most preferably, liquidizing any suitable plant matter, such as rapeseed involves the entire plant in the process, but in any event, those parts of the plant which yield the highest ratio of oil. The liquidized plant matter is then pressurized to a selected pressure such as above the lowest temperature at which CO 2  can exist in super-critical phase. Most specifically, the liquidized plant matter can be blended with super-critical phase CO 2  and thoroughly agitated until all oil formerly contained within plant cells has been extracted and separated from the source cellular repository. The most suitable pressure at which CO 2  will exist in super-critical phase or above critical pressure is 1069.96 psia and the minimum temperature at which CO 2  will exist in critical phase is 87.87° F. Therefore, in order to provide the aggressive solvent properties required to extract oil from plant matter, super-critical phase CO 2 , being an aggressive solvent, is most suitable for this purpose. In another preferred embodiment, plant matter may be shredded and processed by transferring through a grinder such as a Moyno® grinder pump and, in particular, with the employment of a Moyno® annihilator and/or a Moyno® pipeliner which has been designed and developed for industrial applications in food processing such as the processing of vegetable and fruit waste, paper and stock waste, poultry waste, and corn kernel. Additionally, it may be beneficial to install more than one grinder pump in series along the same conduit. Bailed plant matter can be stuffed into a Moyno® pump of any suitable design using, for example, the Moyno® 2000HS system such that the plant matter, whether dry or still wet after recent harvest, can be handled with such equipment as is manufactured by Moyno® and then pumped continuously through Moyno® grinders. Most importantly, plant matter can be processed and handled most readily when in a fluid condition; therefore, after processing the plant matter with the use of Moyno® grinders as described above, L-CO 2  can be blended with the finely ground plant matter to form a single continuous stream of plant matter and L-CO 2 . The continuous stream can then be processed further by way of transferring through a suitable centrifuge as designed and manufactured by American Beef Processing, LLC of Clackamas, Oreg. Equipment can be obtained from either Moyno® or American Beef Processing, LLC at 15501 SE Piazza Avenue, Clackamas, Oreg. 97015. 
         [0077]    A stream of processed plant matter and L-CO 2  can be transferred through a centrifuge so as to separate all solid matter in a single stream extracted from the fat and the extracted oil will be removed during the centrifugal process at suitable rate, such as 30,000 pounds per hour. 
         [0078]    An alternative method of separation to the centrifugal method proposed herein can be by way of a stratification separation column wherein the stream of L-CO 2 , oil and remaining solid plant matter is transferred in an enclosed conduit to a suitable column, most preferably manufactured from either stainless steel such as 316 or carbon steel, and allowed to stratify therein. The stratification process enables each component of the processed stream such as plant oil (corn oil) or any oil extracted from any suitable source, but most preferably, in this instance, plant matter, to be separated into layers of stratified material. For example, oil having a specific gravity of approximately 55 lbs/cu.ft. can stratify above water having a specific gravity of 62.4 lbs/cu.ft. Solid plant matter and, in particular, the cellulose cell walls having a different specific gravity, will also stratify. L-CO 2  has a specific gravity of approximately 29 lbs/cu.ft. when retained in super-critical phase and, therefore, being the lightest component separated at the stratification pressure vessel, will stratify and float to the upper levels in the column. 
         [0079]    Recently an improved method of producing bio-diesel from plant matter has evolved incorporating the use of super-critical methanol under treatment conditions of 350° C. and 43 MPa, however, while the reaction time has been reduced, it remains difficult to apply due to the high cost of pressure vessels large enough to contain the reacting materials for the duration of the reaction time. Furthermore, a temperature of 350° C. is too high to the extent that plant matter will decompose readily at this temperature and contaminants will be produced in quantities too large to prevent the deleterious consequences of decomposing plant matter at 350° C. The method disclosed herein employs the benefit of lowering the temperature at which a blend of methanol with sufficient CO 2  will enter super-critical phase. 
         [0080]    Additionally, the extraction of oil from plants can be achieved as described herein in association with  FIG. 11  wherein super-critical phase CO 2  is blended with a stream of pulverized plant matter. The aggressive solvent properties of super-critical phase CO 2  rapidly extracts any fat (triglycerides). Subsequent to the extraction of triglycerides, a measured quantity of methanol and/or ethanol can be added to the continuous stream of plant matter and CO 2  such that by elevating the pressure and temperature to approximately 250° C. and 2300 psig, bio-diesel can be produced in a continuous stream by transesterification of triglycerides extracted from the plant matter. Subsequently, the components of the continuous stream can be separated in a suitable enclosed and pressurized centrifuge. 
         [0081]    Referring now to  FIG. 12 , a diagram showing a preferred method of bio-diesel and glycerol production is shown in plan view. The diagram shown in  FIG. 12  shown as illustrative only and has not been drawn to scale. However, the apparatus for this preferred method of producing bio-diesel is shown in a convenient manner for the purpose of explanation. A stream of fatty adipose tissue sourced from beef cattle slaughtered, eviscerated, dressed and chilled for the purpose of harvesting beef for human consumption is transferred via conduit  12000  and into emulsifier  12002 . The stream of fatty adipose tissue is harvested simultaneously with the production of a second stream of lean boneless beef using equipment manufactured by American Beef Processing, 15501 SE Piazza Avenue, Clackamas, Oreg. The first and second streams of boneless beef are produced in production quantities typically on the order of approximately 50,000 lbs/hr for the lean stream and 35,000 lbs/hr for the fatty adipose tissue stream. The ratio of the first and second streams can vary according to the lean content of the primary stream fed into the separation equipment. However, most commonly, 50&#39;s or, in other words, a supply of boneless beef comprising 50% lean and approximately 50% fat is most commonly used. The special apparatus manufactured by American Beef Processing can be arranged to process more or less than 100,000 lbs/hr and typically the mass flow ratio of the fatty adipose tissue stream will be on the order of 40,000 lbs/hr. Protein content within the fatty adipose tissue and lean beef attached to the fatty adipose tissue can be removed by the method described hereunder. The equipment operates according to the following description. 
         [0082]    Conduit  12000  is a fully enclosed conduit through which boneless beef can be transferred under pressure and conduit  12000  is attached to the inlet manifold of an emulsifier such as is manufactured by Cozzini, Inc. Other manufacturers are also capable of building this equipment, however, the equipment manufactured by Cozzini, Inc. has been found to be reliable and capable of processing adequate quantities in a given production period. Furthermore, the fatty adipose tissue transferred under pressure via conduit  12000  can be transferred safely, reliably and substantially without leaking such that the stream of fatty adipose tissue, when transferred into emulsifier  12002  at a rate of approximately 40,000 lbs/hr can be reliably emulsified, such that the maximum particle size does not exceed the maximum size that can be reliably and consistently processed by the equipment described in association with  FIG. 12 . The input stream  12000  to emulsifier  12002  is desirably supplied at a mass flow rate of approximately 30,000 lbs/hr or more or less, but at such a quantity as to enable the emulsification. After emulsification, the stream of emulsified fatty adipose tissue is transferred via an enclosed conduit  12004  to enclosed scraped surface heat exchanger  12006 . Scraped surface heat exchanger  12006  can be manufactured by Waukesha Cherry-Burrell in Wisconsin and the arrangement of heat exchangers shown in  FIG. 12  includes three horizontally disposed conduits connected at each end to, firstly an inlet and secondly an outlet, such that scraped surface heat exchanger  12006  is connected directly to second scraped surface heat exchanger  12012  via conduit  12008  and scraped surface heat exchanger  12010  is connected directly to third scraped surface heat exchanger  12016  via conduit  12012 . Said flow of emulsified fatty adipose tissue may be transferred via conduit  12004  into a bank of scraped surface heat exchangers in a stream of substantially consistent rate of flow, and after said stream of fatty adipose tissue has been processed therein, the temperature of the fatty adipose tissue extracted from said bank of scraped surface heat exchanger via conduit  12018  may be approximately 115° F. The bank of heat exchangers may comprise any suitable number therein, however, in the arrangement as shown in  FIG. 12 , a total of three separate horizontally disposed scraped surface heat exchangers are shown. The temperature of said stream of processed fatty adipose tissue transferred via conduit  12018  to pump  12022  should be greater than 108° F. and less than 120° F. It is a purpose of the apparatus shown in association with  FIG. 12  to separate substantially all protein and solid matter such as collagen connective tissue and/or cartilinageous bone from a stream of clear, warm, filtered beef fat. The heated stream transferred into pump  12022  is transferred under pressure via conduit  12020  to first centrifuge  12026 . First centrifuge  12026  separates the stream of warm fatty adipose tissue into two components comprising a first stream of clear, warm, filtered beef fat via conduit  12021  and into filter  12032 . Said second stream of solids separated by means of first centrifuge  12026  comprises all solid matter derived from the stream of heated fatty adipose tissue and is transferred via conduit  12028  directly to positive displacement pump  12029  and into enclosed conduit  12030  under suitable pressure. A stream of protein, connective tissue, cartilinageous bone and other semi-solid matter pumped under pressure via positive displacement pump  12029  is returned to apparatus not shown in association with  FIG. 12 , however, said stream of solids is blended with lean beef separated from said stream of 50&#39;s referred to above prior to retail packaging or further processing into beef patties or the like. 
         [0083]    The stream of beef fat transferred via enclosed conduit  12021  and filtered in filter  12032  prior to transfer into pump  12036  via conduit  12034  is then blended with proportional quantities of methanol and/or ethanol and a proportionate quantity of L-CO 2 . The blend comprising beef fat, methanol and/or ethanol and L-CO 2  in suitable proportions is maintained at a selected temperature and pressure of up to 250° C. and 2250 psi for a period of time sufficient to facilitate the reaction between the three materials, such that bio-diesel or a mixture of fatty esters and glycerol is produced from the reaction shown in  FIG. 8 . 
         [0084]    Methanol is provided from a source and transferred by positive displacement pump  12084  via conduit  12082  in the direction shown by the arrow and a relatively proportionate quantity of L-CO 2  is pumped by positive displacement pump  12049  in the direction shown by the arrow via conduit  12078 . A blender which may be a continuous static blender  12048  or any other suitable type of blender is provided as shown. Generally, the apparatus shown in  FIG. 12  is arranged to provide three streams of liquid matter each provided under suitable pressure such that the combined stream will react according to the organic chemical reaction shown in  FIG. 8 . It is desirable in order to maximize efficiency of the reaction that the liquid materials be provided in measured quantities, precisely controlled, in a continuous stream. Temperature and pressure should be maintained at optimum values in order to achieve the most efficient production rate available. The combined stream may be transferred via one or more reactors each optionally containing an appropriate solid catalyst, if necessary, which should line the walls of each micro channel which are arranged in a series of parallel micro conduits within micro reactor arrays  12040 ,  12032  or  12027 . The blended stream of liquid materials pumped via positive displacement pumps  12036 ,  12049  and  12084  should be maintained at an optimum temperature and pressure of 250° C. or more or less and 2250 psig or more or less or at any other suitable temperature and pressure that will facilitate the most rapid and effective reaction between the three materials comprising the combined stream. Table #2 ( FIG. 13 ) shows a range of temperatures and pressures that can be maintained to achieve maximum efficiency of the reaction which is similar to the reaction shown in  FIG. 8 . The stream of liquid comprising glycerol and a mixture of fatty esters transferred via conduit  12030  to pump  12036  comprises residual methanol and CO 2  which is desirably extracted and disposed of by exhausting to atmosphere or, alternatively, recycling. However, in order to achieve maximum efficiencies, super-critical phase of methanol and super-critical phase of L-CO 2  is desirable during the reaction process. Pump  12036  controls the stream pressure such that it is continuously transferred into vessel  12041  via an orifice with a variable aperture size. The entire stream of fluids can be transferred via the aperture which is located within vessel  12041  such that a drop in stream pressure occurs as the fluids pass through said aperture. The cross sectional area of the aperture opening can be controlled and configured such that a pressure and substantial temperature drop occurs, causing certain fluids to crystallize. For example, the controlled pressure drop can be arranged such that glycerol is crystallized, thereby solidifying the fluids such that CO 2  will become gaseous and can be extracted from vessel  12041  at a rate and mass flow-controlled extraction enabling a precise control of pressure within said vessel  12041 . CO 2  extracted in this way can then be compressed and transferred through a suitable heat exchanger such that L-CO 2  can be transferred directly into a storage vessel and retained for subsequent recycling. The remaining fluids are transferred via conduit  12060  and positive displacement pump  12062  into centrifuge  12068  where glycerol having a specific gravity on the order of 78 pounds per cubic foot is readily extracted when suspended in L-CO 2  pressurized to approximately 500 psi and retained at approximately 32° F. L-CO 2  can be extracted and recycled and glycerol simultaneously extracted and transferred to a storage vessel and retained for subsequent use. Said glycerol formed in this manner is a purest form of glycerol devoid of contaminates such as sodium hydroxide which cannot be removed entirely when manufactured by way of the commonly used or conventional bio-diesel production process using sodium hydroxide as a catalyst. Bio-diesel produced in this way comprises the majority of the fluids transferred into centrifuge  12068  and thereby extracted from the stream of fluids. Bio-diesel produced in this way is also of the purest kind and washing with water is not required since there are no contaminates such as residual sodium hydroxide. Bio-diesel is transferred into suitable storage vessel, but most preferably, into road and/or rail tankers for immediate shipping to customers. Bio-diesel produced in this manner is the most suitable for use as an additive in fossil fuel diesel. Federal legislation requires that sulfur be extracted from all fossil fuels, however, without lubricants that are presently unavailable, fossil fuel diesel will be unsuitable for use in reciprocating diesel engines. It is therefore considered probable that bio-diesel produced in accordance with the methods disclosed herein, shall be used as an additive in the amount of approximately 2% of the total mass weight of the fossil fuels produced subsequent to September 2006. 2% bio-diesel produced in the manner herein disclosed provides sufficient lubricity when added to the fossil fuels processed in accordance with legislation. 
         [0085]    The three components, CO 2 , methanol (and/or ethanol) and triglycerides, will most preferably be transferred by positive displacement metering pumps sized suitably according to the relative proportions of each stream component. Such metering pumps are manufactured by, for example, Bran+Leubbe. Such metering pumps can be sized and manufactured according to requirements thereby enabling precise measuring and metering of the liquids under selective pressure and temperature. The pumps manufactured by Bran+Leubbe are available from 611 Sugar Creek Boulevard, Delavan, Mich. 53115. 
         [0086]    A typical reaction period for bio-diesel produced via the relatively low pressure method employing sodium hydroxide as the catalyst may be as much as 24 hours or more or less. A typical period is greater than 7 hours, however, the reaction time for production of bio-diesel as per the reaction shown in  FIG. 8  may be as short as 20 seconds, 30 seconds or 3 minutes or more or less, depending upon the ratio of CO 2  and methanol and/or ethanol maintained in super-critical phase for the duration of the reaction phase. Typically, the quantity of methanol and/or ethanol blended with sodium hydroxide in a reaction designed to address the failure of triglycerides to contact and react with methanol in the most common method employed by industry presently is two times the actual quantity of methanol actually required for the reaction. However, in all cases, separation of the resultant blend of liquid materials requires either use of a centrifuge or a separation tower or stratification column in which materials separate according to their specific gravity. Clearly, by minimizing the quantity of methanol that exceeds the amount required for a complete reaction is desirable and such minimum quantity can be achieved. 
         [0087]    Referring again to  FIG. 12 , an apparatus arranged to maximize efficiency is shown for materials that comprise L-CO 2  catalyst. Methanol in liquid form can exist at ambient pressure of 14.7 psi and a temperature of 20° C., however, at this temperature and pressure, CO 2  is a gas. In order to provide super-critical phase methanol and CO 2 , the pressure of the combined materials must exceed 2000 psi when the temperature is maintained at above 250° C. However, the ratio of methanol to CO 2  is less than 50% methanol and more than 50% CO 2 , wherein the CO 2  must be a saturated vapor and/or in super-critical phase at 250° C. 
         [0088]      FIGS. 14 and 15  show two views of an enclosed, pressurized hydrocyclone which can be constructed to provide yet another aspect of the present invention wherein the apparatus can be devised for continuously separating lean beef, beef fat and CO2 from a fluid stream that includes all three components. The enclosed and pressurized hydrocyclone comprises a uniformly proportioned, centrally disposed enclosure having a lower segment profile similar to that of a steep inverted cone, typically having a circular profile cross section through the horizontal plane profile, an input port for accepting a fluid stream and at least three (desirably at least four) output ports for transferring the separated components (i.e., beef fat, lean beef and CO2) out of the hydrocyclone. The hydrocyclone effects a density-based separation of the solid (and liquid) components when suspended in a fluid, wherein such a fluid stream entering close to the upper end and at a tangential orientation relative to the circular cross section of the hydrocyclone body, thereby accelerating the stream as it descends through the decreasing diameter (radius) of the steep cone, forcing the heavier components toward the walls of the hydrocyclone and the lighter components toward the middle of the enclosed space within the hydrocyclone. Thus, heavier components exit the cyclone through an output port at, or toward, the bottom of the hydrocyclone cone shaped segment, while lighter components exit the hydrocyclone through output ports located at, or toward, the top of the hydrocyclone body. In some embodiments, the fluid stream is pumped into the input port of the hydrocyclone (e.g., using a suitably sized centrifugal pump), which is in communication, via a sealed connection, with a grinder, which is itself in communication, via a sealed connection, with a source of beef, such that a continuous stream of beef is ground prior to entering the input port. The ground beef is combined with pressurized CO2 to form a suspension of beef particles in the CO2. The suspension may be transferred into input port of the hydrocyclone in a controlled, continuous stream at a velocity and rate of mass flow most suited to the hydrocyclone apparatus. The source of beef is desirably, but not necessarily, any suitable quantity of 50&#39;s, 65&#39;s, or even 75&#39;s boneless beef but most preferably that grade of boneless beef that yields the most lucrative, proportional quantities of fat and lean beef derived from the selected source. 
         [0089]    An illustrative embodiment of a hydrocyclone having four output ports and a means for separating lean beef from beef fat using the apparatus is represented in  FIG. 14 , which represents a three-dimensional view of the apparatus, and  FIG. 15 , which shows a cross-sectional view of the apparatus. As shown in these two figures, the hydrocyclone has a main body that includes an upper section  1424  having generally parallel side walls and an upper wall  1514 , and a lower section  1428 ,  1534  having a generally conical longitudinal cross-section. The upper and lower sections may be connected by a continuous annular weld  1426 . The hydrocyclone further includes at least one input port in communication with an input conduit  1436  through which a continuous stream of fluid may enter the upper section of the body of the hydrocyclone. A first output port  1434 ,  1530  in communication with the lower end of the lower section of the body is also provided. The first output port may be connected to the body by a continuous annular weld  1430 . The hydrocyclone includes three additional output ports disposed above the upper section of the body. The second output port  1404 ,  1562  extends upwardly from the hydrocyclone and is disposed opposite the first output port  1432 ,  1530 , such that the first and second output ports share a common center line. A third output port  1412 ,  1512  extends upwardly and outwardly from the top wall  1514  of the upper section of the body of the hydrocyclone. Finally, a fourth output port  1406 ,  1504  extends outwardly from the centerline of the hydrocyclone and is in communication with the body of the cyclone through a neck section  1558  connected to the upper wall  1514  of the upper section of the body. 
         [0090]    A process for separating the beef fat, lean beef and CO2 from a fluid stream containing beef solids (e.g., boneless, ground beef) suspended in fluid CO2 may be described as follows. The suspension may be prepared by blending together the ground beef with liquid carbon dioxide pressurized at least about 480 psia (e.g., 480 psia to about 600 psia) and maintained at about 34° F. (e.g., about 32° F. to 38° F.) in proportions of approximately one part ground beef to four or five parts carbon dioxide to provide a well formed suspension of solid beef components and a liquid carbon dioxide component. The suspension is continuously pumped into input conduit  1436 ,  1518 , as represented by arrows  1401  and  1516 . Inside the body of the hydrocyclone, the denser lean beef particles tend to migrate toward the walls of the body of the cyclone, traveling in a downward direction and exiting the hydrocyclone through the first output port  1432 ,  1534  in the direction shown by arrows  1434  and  1534 . The path of the lean beef particles is represented by arrows  1522 ,  1526 ,  1530 ,  1534 ,  1550 ,  1546 ,  1542 ,  1540 ,  1538 ,  1539 ,  1536 , and  1532 . The less dense beef fat particles migrate toward the center of the hydrocyclone, initially in a downward direction, before turning upward, and exiting through the third output port  1412 ,  1512  or the fourth output port  1406 ,  1504 . The path of the beef fat particles is represented by arrows  1520 ,  1524 ,  1528 ,  1532 ,  1544 ,  1548 ,  1552 ,  1554 ,  1503 ,  1505 ,  1561  and  1509 . The CO2, being the least dense material, exits at the top of the hydrocyclone through the second output port  1404 ,  1562  in the direction shown by arrow  1502 . The result is a separation of the fluid into three separate streams: one comprising predominantly lean beef extracted in the direction shown by arrow  1434 ; one comprising predominantly beef fat extracted in the direction shown by arrow  1408 ; and one comprising CO2 represented by arrow  1402 . 
         [0091]    Beef oil harvested from any suitable ground boneless beef source material and separated from the components combination of the source, according to any procedure disclosed herein above, can be transferred directly to the bio-diesel production processing system. 
         [0092]    For the purposes of this disclosure and unless otherwise specified, “a” or “an” means “one or more”. All patents, applications, references and publications cited herein are incorporated by reference in their entirety to the same extent as if they were individually incorporated by reference. 
         [0093]    As will be understood by one skilled in the art, for any and all purposes, particularly in terms of providing a written description, all ranges disclosed herein also encompass any and all possible subranges and combinations of subranges thereof. Any listed range can be easily recognized as sufficiently describing and enabling the same range being broken down into at least equal halves, thirds, quarters, fifths, tenths, etc. As a non-limiting example, each range discussed herein can be readily broken down into a lower third, middle third and upper third, etc. As will also be understood by one skilled in the art all language such as “up to,” “at least,” “greater than,” “less than,” and the like include the number recited and refer to ranges which can be subsequently broken down into subranges as discussed above. Finally, as will be understood by one skilled in the art, a range includes each individual member. 
         [0094]    While the preferred embodiment of the invention has been illustrated and described, it will be appreciated that various changes can be made therein without departing from the spirit and scope of the invention.