Abstract:
A method and apparatus for separating a first fluid from a fluid mixture. In one embodiment water containing methane is passed through an agitation chamber with a plate at the chamber&#39;s proximal and distal ends. Both plates have orifices permitting the mixed fluid to pass into and out of the agitation chamber. In one embodiment, the mixed fluid rotates about its axis of flow through the agitation chamber. In one embodiment, the mixed fluid passes through a separation chamber having a plurality of baffles that promote separation of the methane from the methane/water mixture. In one embodiment, the separated methane is removed from the water in a collection chamber that facilitates gravity separation of the mixed fluids.

Description:
The present application is a continuation of, and claims priority to, U.S. Pat. No. 8,366,808 filed on Jun. 14, 2010. The aforementioned patent and is hereby incorporated by reference in its entirety. 
     BACKGROUND OF THE INVENTION 
     A fluid may comprise a mixture of fluids with different properties. For example, some fluids are liquids containing entrained gas, other fluids may combine liquids having different physical properties such as oil and water mixtures. Water removed from coal seams often contains entrained methane and other gases. Methane may partially separate from coal seam water during pumping. However, this partial separation may be inefficient in that entrained methane often remains in the water pumped from the seam. The entrained methane is a valuable commodity in and of itself. As is well known, methane is an efficient and environmentally friendly fuel, producing water and carbon dioxide when burned. 
     Methane left in water can create numerous problems. Water-laden methane requires additional chlorine demand in water disinfection systems. The increased use of chlorine in water treatment increases EPA-regulated by-products. Additionally, the colorless and odorless methane can be an explosion and fire hazard in water supplies. Pumping methane water can also be difficult because the methane can create gas locks. 
     Entrained methane can be removed from water by letting the water rest for an extended period of time. Such is often accomplished in an enclosed tank, with valves and/or piping that vent the methane evolved to the atmosphere or by placing the water in an open pond, as occurs in the coal bed methane fields in the Powder River Basin of Wyoming. At times the removal is enhanced by air sparging (adding air to the water) or by adding chemicals to the methane/water mixture. Because methane is odorless and colorless, it escapes unnoticed into the atmosphere. 
     Methane is known as a particularly damaging greenhouse gas. Methane takes years to breakdown naturally in the atmosphere. When it decomposes, it creates carbon dioxide, a greenhouse gas. Methane is over 20 times more effective at trapping heat in the atmosphere than carbon dioxide. 
     The amount of methane escaping into the atmosphere is significant. It is believed Powder River Basin coal bed methane wells are between 75% and 98% efficient in separating methane gas from pumped coal bed water. If existing Powder River Basin coal bed methane wells average 85% efficiency, 675,000 mcf of methane escapes into the atmosphere from just Powder River Basin wells each day. 
     Coal bed water is not the only fluid containing potentially harmful fluids. Entrained gases and volatile compounds may be found in polluted groundwater. For example, radon is a harmful gas that may be found in ground water. Additionally, hydrocarbon gases other than methane may also be found in ground water. It is undesirable to vent the entrained gases or compounds in polluted groundwater to the atmosphere because they may be toxic and may also contribute to greenhouse gas pollution. 
     Additionally, it may be desirable to separate mixtures of fluids having different physical properties. For example, crude oil spilled or released into water can cause significant environmental damage. The oil/water mixture may also contain gases. Also, motor oil, or other liquids, may be spilled or released into groundwater. Methods exist for removing such fluids from water but the known methods require significant energy input, are relatively inefficient and slow and may introduce harmful greenhouse gases into the atmosphere. 
     Currently used methods and apparatus for removing unwanted fluids from fluid mixtures are slow and relatively inefficient and often release unwanted greenhouse gases. Heretofore, efficient and cost effective methods and apparatus for removing unwanted fluids from fluid mixtures were not available. Although specific problems are described in this background section, the invention is not limited to solving these particular problems. Embodiments of the present invention may be useful in solving other problems not specifically described in this section. Thus, the background section should not be used to limit the scope of the appended claims. 
     SUMMARY OF THE INVENTION 
     One embodiment of the invention provides a system and apparatus that efficiently and cost effectively removes a fluid from a fluid mixture, such as methane from water containing methane, radon from ground water or liquid hydrocarbons from water. 
     In one embodiment, a fluid mixture having a first fluid component and a second fluid component is introduced into a process stream. The local velocity of the fluid mixture is changed by passing the mixture through a plurality of restrictions. The change in local velocity causes at least a portion of the first fluid component to separate from the fluid mixture. At least a portion of the first fluid component separated from the fluid mixture is discharged along with at least a portion of the second fluid component. In certain embodiments, the first fluid component is collected. In other embodiments, the first fluid component is collected under negative pressure. In some embodiments, the temperature of the fluid mixture is changed such as, for example, by more than five degrees Fahrenheit. In other embodiments, baffles are used to change the rate of flow of the fluid mixture. The baffles may be generally horizontal, and in some embodiments, conical. 
     In one embodiment, the fluid mixture is passed through a chamber after causing the mixture to repeatedly change velocity. In one aspect of the invention, the fluid mixture enters the chamber through a first plurality of apertures. In another embodiment, the fluid mixture exits the chamber through a second plurality of apertures. In yet another embodiment, the fluid mixture is caused to rotate around the mixture&#39;s general axis of flow through the chamber by impinging upon a surface angled relative to the mixture&#39;s general axis of flow. In one embodiment, the fluid mixture is caused to rotate around the mixture&#39;s axis of flow through the chamber by introducing the mixture into the chamber through nozzles angled relative to the fluid mixture&#39;s general axis of flow. 
     In one embodiment, the process is used to process a mixture of water and methane. 
     In another embodiment, the restrictions through which the fluid passes are a plurality of apertures within a conduit, the apertures having a cross-sectional area smaller than the average cross-sectional area of said conduit. The fluid mixture is then passed through a chamber containing a baffle, the baffle facilitating the aggregation of gas bubbles in the fluid mixture. 
     In one embodiment, the mixed fluid includes a first fluid component and a second fluid component. The mixed fluid is cause to experience turbulent flow within a conduit. The turbulent flow causes a portion of the first and second fluid components to separate. The mixed fluid is caused to experience laminar flow within the conduit. The laminar flow facilitates further separation of the first and second fluid components. At least a portion of the separated first fluid component is removed from the conduit. At least a portion of the second separated fluid component is also removed from the conduit. In another embodiment, the turbulent flow is caused by passing the mixed fluid through a restriction. In yet another embodiment, the mixed fluid experiences centrifugal force. In one embodiment, the first fluid component is methane and said second fluid component is water. 
     Another embodiment of the invention comprises a fluid separation system. The system has a first chamber causing a mixed fluid comprising a first fluid component and a second fluid component to experience turbulent flow when passed through the first chamber. A second chamber causes the mixed fluid to experience laminar flow when passed through the second chamber. The turbulent flow and laminar flow causes a portion of the first fluid component to aggregate. A first fluid component removal orifice is in fluid communication with the aggregated first fluid component. A second fluid component removal orifice is in fluid communication with the second fluid component. In one embodiment, the second chamber contains a plurality of baffles. In another embodiment, the baffles are conical. 
     In yet another embodiment, a third chamber facilitates gravity separation of the first fluid component from the second fluid component. The third chamber has the first fluid component removal orifice positioned in fluid communication with the gravity separated first fluid component. The third chamber also has the second fluid component removal orifice positioned in fluid communication with the gravity separated second fluid component. In some embodiments, the mixed fluid contains a third fluid component. The third chamber facilitates gravity separation of the third fluid component from the first fluid component and the second fluid component. The third chamber has a third fluid component removal orifice positioned in fluid communication with the gravity separated third fluid component. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         FIG. 1  is a partial cut away perspective view of one embodiment of a fluid separation system. 
         FIG. 2  is a front view of one embodiment of an agitation chamber inlet plate. 
         FIG. 3  is a front view of a second embodiment of an agitation chamber inlet plate. 
         FIG. 4  is a front view of one embodiment of an agitation chamber outlet plate. 
         FIG. 5  is a top view of one embodiment of a first baffle. 
         FIG. 6  is a top view of one embodiment of a second baffle. 
         FIG. 7  is a cut away side view of one embodiment of a separation chamber. 
         FIG. 8  is a partial cut away perspective view of one embodiment of a fluid separation system. 
         FIG. 9  is a top view of one embodiment of an agitation chamber inlet plate with the top portion joining sub-plates removed. 
         FIG. 10  is a top view of one embodiment of an agitation chamber outlet plate with the top portion joining sub-plates removed. 
         FIG. 11  is a cut away top view of one embodiment of a collection chamber. 
         FIG. 12  is a partial cut away side view of one embodiment of a fluid separation system. 
         FIG. 13  is a plan view of one embodiment of a separation system having multiple separation chambers and agitation chambers. 
     
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
     This disclosure is intended to describe the novel features of the claimed invention. Those of ordinary skill in the art will recognize alternate equivalent methods and devices for removing fluids from fluid mixtures upon reading this disclosure. 
       FIG. 1  depicts a cut away perspective view of an embodiment of the fluid separation system  7  that is adapted for removal of a fluid from a fluid mixture, such as methane from water. The methane-laden water may be water pumped from a coal seam or from an aquifer. 
     While it is currently contemplated that the invention will be used with groundwater, i.e., water found below the earth&#39;s surface, the inventions general application is not so limited. For example, it is contemplated that the invention can be used to separate liquid hydrocarbons from water at the earth&#39;s surface, such as water contaminated with crude oil or petroleum derived products. Also, the invention is not limited to the separation of hydrocarbons from water as it can be used to separate radon from water as well. Additionally, as presently contemplated, the invention is not limited to separation of fluids from water. For example, it is contemplated that the invention can be used to separate gaseous hydrocarbons from liquid hydrocarbons. 
     After being removed from a coal seam or aquifer and being pumped to the earth&#39;s surface, water containing methane is introduced into the system at inlet  9 . An inlet valve  10  is placed in the flow path and may be used to control the rate of flow of the fluid mixture into conduit  11 . Inlet valve  10  is a typical ball valve as will be known to one of ordinary skill. A check valve  12  prevents back-flow. A strainer  14 , such as manufactured by Mueller Manufacturing, having approximately 20 openings per square inch, removes solid particulates that may be in the fluid. A flow meter  16  monitors the rate of fluid flow and can provide data used, in conjunction with inlet valve  10 , to control the rate of fluid flow through the fluid separation system  7 . With the embodiment described, the desired rate of flow is typically between approximately 7 and 10 gpm. The fluid mixture passes through screen  17  having approximately 10-20 openings per square inch. 
     As the fluid mixture passes through strainer  14  and screen  17 , the velocity of the fluid changes. Herein, velocity includes direction of flow and speed (the time rate of change of the position of discrete fluid components without regard to direction). The fluid&#39;s speed increases as it passes through strainer  14  and screen  17  because the cross-sectional area of the flow path is decreased and the speed of the fluid passing through the decreased area must increase to maintain the overall rate of fluid flow through the fluid separation system  7 . The velocity of the fluid also changes because the fluid must change direction to pass through the openings in strainer  14  and screen  17 . 
     After flowing through screen  17 , the fluid is introduced into an agitation chamber  18  that has a diameter approximately four to 9 times larger than the conduit  11  and is 2-3 times its diameter in length. Specifically, in the embodiment described, the conduit  11  has an inside diameter of approximately one inch and the agitation chamber  18  has an inside diameter of approximately eight inches. 
     At the proximal end of the agitation chamber  18  is an agitation chamber inlet plate  19 . In one embodiment, as shown in  FIG. 2 , agitation chamber inlet plate  19  has three inlet orifices  24  formed in nozzles  26  that are angled relative to the longitudinal axis of agitation chamber  18 . In the embodiment depicted, the inlet orifices  24  have an inside diameter of approximately ⅜ inch. 
     In the embodiment depicted in  FIG. 2 , the fluid exits the inlet orifices  24  at an angle relative to the longitudinal axis of agitation chamber  18  and impinges on the inner wall of the agitation chamber  18 . It is presently contemplated that nozzles  26  would be angled such that the resulting fluid flow tends to rotate around the longitudinal axis of the agitation chamber  18  as it progresses through the agitation chamber  18 . All of the nozzles can be angled approximately 30 degrees from the Z axis of  FIG. 2  and, as depicted, approximately 60 degrees down from the X axis for the upper right nozzle, approximately 60 degrees left of the Y axis of  FIG. 2  for the lower nozzle and approximately parallel with the Y axis of  FIG. 2  for the left nozzle. 
     In this embodiment, the velocity of the fluid changes because the direction of fluid flow changes from being generally parallel to the longitudinal axis of the agitation chamber  18  prior to entering nozzles  26  to being angled relative to the same axis. Also, the fluid&#39;s speed changes from a lower rate prior to entering the nozzles  26  to a higher rate as it accelerates and passes through the nozzles  26 . As the fluid exits the inlet orifices  24 , its speed decreases and, as the fluid impinges on the agitation chamber  18  inner wall, the direction of flow becomes rotational and velocity constantly changes with the rotational flow. Thus, both aspects of velocity, e.g., speed and direction of flow, are changed as the fluid enters the agitation chamber  18 . Additionally, the rotational flow imparts a centrifugal force on the fluid. 
       FIG. 3  depicts an alternate embodiment of the agitation chamber inlet plate  19 . In this embodiment, the agitation chamber inlet plate  19  has three inlet orifices  24 . The inlet orifices  24  have an inside diameter of approximately ⅜ inch. The inlet orifices  24  are formed into the agitation chamber inlet plate  19  and paths through the inlet plate  19  are generally parallel to the longitudinal axis of the agitation chamber  18 . An impeller  28  is adjacent the inlet orifices  24 . The impeller  28  has a diameter of approximately 7½ inches. As the fluid enters the agitation chamber  18  through inlet orifices  24 , it impinges on impeller  28  and causes impeller  28  to rotate. Impact with impeller  28  causes the fluid to deflect at an angle relative to the longitudinal axis of the agitation chamber  18 . 
     Many alternative structures could be used to change the velocity of the fluid in the agitation chamber  18 . For example, impeller  28  could be replaced with fixed vanes. Also, rather than imparting a rotational flow, the velocity of the fluid could be changed by repeatedly forcing the fluid in one linear direction and then another. 
       FIG. 4  depicts the agitation chamber outlet plate  30  that is located at the distal end of the agitation chamber  18 . In this embodiment, the agitation chamber outlet plate  30  has six outlet plate orifices  32 . The outlet plate orifices  32  change the velocity of the fluid. The outlet plate orifices have a diameter of approximately ½ inch. The outlet plate orifices  32  are formed in the outlet plate  30  and the fluid flow path through the outlet plate  30  is generally parallel to the longitudinal axis of the agitation chamber  18 . In this embodiment, the agitation chamber outlet plate  30  is approximately 18 inches from the agitation chamber inlet plate  19 .  FIG. 4  merely shows one embodiment of an outlet plate  30 . In other embodiments, outlet plate  30  may be designed with different orifices or other features. 
     After the fluid passes through the outlet plate  30 , it passes through a reducer to separation chamber inlet piping  34  and enters the bottom of the separation chamber  36 . The inlet piping  34  has an inside diameter of approximately 4 inches. 
     The separation chamber  36  provides conditions conductive to the collection or aggregation of the fluid to be collected. The separation chamber  36  changes the velocity of the fluid mixture. In general, the speed of the fluid mixture is greatly reduced as it passes through the separation chamber  36  and the flow is relatively calm because the restrictions on the fluids flow are reduced. When methane is processed, the separation chamber  36  encourages bubbles of methane to join and form larger bubbles. When the fluid to be collected is a liquid, the separation chamber  36  encourages droplets of the liquid to be collected to join and form larger droplets. 
     In the embodiment shown in  FIG. 1 , the separation chamber  36  is generally cylindrical and has a diameter of approximately 24 inches that is defined by sidewall  38 . The separation chamber  36  is approximately 36 inches tall. The fluid entering the separation chamber  36  next passes through arcuate slots  40  defined between the separation chamber sidewall  38  and a first baffle  42 , as shown in  FIG. 5 . The first baffle  42  is conical in shape. In one embodiment, the arcuate slots  40  are approximately 23 and ⅔ inches long adjacent the separation chamber sidewall  38  and are approximately one inch wide. The apex of the first baffle  42  is approximately ⅛th the separation chamber  36  diameter below the arcuate slots  40 . 
     The separation chamber  36  has a second baffle  44  above the first baffle  42  that is also conical in shape and has aperture  46  in place of the apex of the cone. The base of second baffle  44  is connected to sidewall  38 . The apex of the second baffle  44  is approximately ⅛th the separation chamber  36  diameter above the base of the second baffle  44 . The aperture  46 , as shown in  FIG. 6 , in the second baffle  44  has a diameter of 4 inches. 
     A third baffle  48  is above the second baffle  44 . The third baffle  48  defines arcuate slots  50  between the separation chamber sidewall  38  and the third baffle  48  periphery. The third baffle  48  is identical to the first baffle  42  and has its apex below slots  50 . The base of third baffle  48  is approximately ⅛th of the diameter of the separation chamber  36  above the apex of the third baffle  48 . 
     The second baffle  44  apex is approximately midway between the top and bottom of the separation chamber  36 . The base of the first baffle  42  is approximately midway between the apex of the second baffle  44  and the bottom of the separation chamber  36 . The base of the third baffle  48  is approximately midway between the apex of the second baffle  44  and the top of the separation chamber  36 . 
       FIG. 7  is a cross-sectional view of the separation chamber  36 . As depicted in  FIG. 7 , the first conical baffle  42  has arcuate slots  40  between the first baffle  42  and the separation chamber sidewall  38 . The second conical baffle  44  has an aperture  46  at its apex and is connected to the sidewall  38  at its base. The third baffle  48  is depicted with its apex below arcuate slots  50 . 
     The fluid exits the separation chamber  36  through collection chamber inlet piping  52  that has an inside diameter of one inch. The collection chamber inlet piping  52  connects to an inlet piping expander  54  that increases the diameter of the fluid flow path to approximately four inches. The fluid passes through inlet piping and inlet piping expander  54  to collection chamber  56 . Collection chamber  56  has a diameter of approximately four inches and is approximately 48 long. 
     Because methane separated by the process from the coal seam water is lighter than water, it tends to rise in the collection chamber  56  while the water falls in the collection chamber  56 . In one embodiment, a sight tube is connected to the collection chamber  56  so the surface elevation of the water can be monitored. It is generally desired that the water fill the bottom ⅔ to ¾ of the collection chamber  56 . One of ordinary skill in the art would recognize that known sensors could replace the sight tube and could be configured to automatically regulate inlet fluid flow to maintain the proper water level in collection chamber  56 . 
     Water is discharged from discharge outlet  58  at the bottom of collection chamber  56 . The discharge outlet  58  has a diameter of approximately two inches. 
     Methane is collected through collection outlet  60 . Collection outlet  60  has a diameter of approximately one inch. In some applications, it may be desirable to create a partial vacuum at collection outlet  60 . The collected methane may be used as a fuel source, as is commonly understood. 
     The fluid separation system  7  is sealed when used to collect methane, or other gases. In other words, the fluid mixture is not exposed to the atmosphere as it passes through the fluid separation system  7  and separated gases cannot leave the fluid separation system  7  except through the collection outlet  60 . If small amounts of gas remain in the fluid mixture at the end of the process, this unseparated gas can only leave the fluid separation system with the processed fluid mixture through discharge outlet  58 . 
     In some embodiments, it may be advantageous to modify the temperature of the fluid as it is processed.  FIG. 8  depicts a system adapted to modify fluid temperature. In one embodiment, the agitation chamber  118  has a temperature modifying agitation chamber inlet plate  119  at its proximal end. The temperature modifying agitation chamber inlet plate  119  is formed by creating a void  121  between adjacent sub-plates  123 , as depicted in  FIG. 9 .  FIG. 9  is a top view of the temperature modifying agitation chamber inlet plate  119  with the member joining the sub-plates  123  removed. Tubes  125  provide a fluid flow path through the temperature modifying agitation chamber inlet plate  119 . A void  121  is defined by the adjacent surfaces of the sub-plates  123 , the exterior walls of tubes  125  and the interior wall of the surface joining the adjacent sub-plates at their periphery. Inlet port  127  and outlet port  129  provide a flow path for heating or cooling fluids through the void  121 . 
     Temperature modifying agitation chamber outlet plate  130  may be similarly constructed with inlet port  131  and outlet port  132  providing a flow path for heating or cooling fluid between the outlet sub-plates  133  and around outlet tubes  134 , as depicted in  FIG. 10 .  FIG. 10  is a top view of the temperature modifying agitation chamber outlet plate  130  with the member joining the sub-plates  133  removed. 
     Additionally, an optional lower tubing coil  135  may be placed between the bottom of the separation chamber  136  and the first baffle  142 . The lower tubing coil  135  is depicted in  FIG. 11 . The coil may be made of ⅜th inch copper tubing that is spaced such that there is approximately a ⅜th inch gap between adjacent tubing outer walls. The lower tubing coil  135  has an inlet port  143  through the sidewall  138  and an outlet port  145  through the sidewall  138  that provides a flow path for heating or cooling fluids to pass through the lower tubing coil  135 . An optional upper tubing coil  147  may be placed between the second baffle  144  and the third baffle  148  as depicted in  FIG. 8 . The upper tubing coil  147  has an inlet slot  151  and an outlet  153  to provide a flow path for heating or cooling fluids to pass through the upper tubing coil  147 . 
     In embodiments, heating or cooling may be desirable depending upon the nature of the fluid processed. Heating fluids having relatively high viscosity may enhance separation. Conversely, some processed fluids may have a high native temperature detrimental to fluid separation. Cooling such fluids may enhance separation. In some applications, it may be desirable to heat fluid at one stage of the process and to cool the fluid at another stage of the process. It is contemplated that the change in processed fluid temperature will be greater than five degrees Fahrenheit. Described above are methods of modifying the temperature of the processed fluids. The description is not exhaustive and one of ordinary skill will be aware of equivalent methods of modifying the temperature of a fluid being processed. 
       FIGS. 12 and 13  depicts an embodiment of a separation system designed to separate fluids such as might be encountered at a crude oil spill or a waste oil stream.  FIG. 12  depicts the system laid out in a linear fashion.  FIG. 13  is a top view of the system as it might be constructed to maximize space utilization. An optional agitation chamber  218  with an agitation chamber inlet plate  219  and an agitation chamber outlet plate  230  may be provided if it enhances fluid separation. It may be desirable, for example, to pass a fluid through the agitation chamber  218  if the fluid contains a gas component. If fluid separation is enhanced by use of the optional agitation chamber  218 , it flows from the agitation chamber  218  through the fluid separation chamber inlet piping  234  into the separation chamber  236 . If the agitation chamber  218  is not used, the fluid to be processed may be introduced directly into the separation chamber inlet piping  234 . 
       FIG. 12  depicts a cross-section view of the separation chamber  236 . Separation chamber  236  is generally as described above and has an optional lower tubing coil  235  that may be used if fluid temperature modification is desired. The lower tubing coil  235  is placed between the first baffle  242  and the bottom of the separation chamber  236  and has an inlet port  237  through the sidewall  238  and an outlet port  239  that also passes through the sidewall  238 . Above the second baffle  244  is optional upper tubing coil  247  and the third baffle  248 . The upper tubing coil has an inlet  251  and an outlet  253 . 
     The fluid exists the separation chamber  236  through collection chamber inlet piping  252 . A valve  255  is placed in the collection chamber inlet piping  252  to permit isolation of an individual separation chamber  236  from the collection chamber  256 .  FIG. 12  depicts a single agitation chamber  218  and separation chamber  236  feeding a common collection chamber  256 . The collection chamber  256  in  FIG. 12  is depicted in cross-section. In the embodiments depicted in  FIGS. 12 and 13 , it is contemplated that four separation chambers  236  will feed the common collection chamber  256 . 
     If a gas is separated from the processed fluid, it is collected through outlet  260 . If fluids having different specific gravities are separated, such as oil and water, the fluid with the lower specific gravity collects in the upper portion of collection chamber  256  and can be collected through outflow line  262  to a storage container  264 . When a desired quantity is collected, valve  266  may be opened and the collected fluid removed. It may be advantageous to heat outflow line  262  and/or storage container  264  if the collected fluid is viscous. It is contemplated that in some embodiments the system can separate gas and liquids having different specific gravities from the same fluid mixture. 
     The fluid with the greater specific gravity naturally collects at the lower portion of collection chamber  256 . A siphon tube  267  draws the fluid from the lower portion of the collection chamber  256  and discharges it through outflow pipe  268 . The siphon tube  267  has a suction release aperture  269  positioned to break the suction drawing the fluid from the collection chamber  256  if the fluid level in the collection chamber reaches the suction release aperture  269 . Such prevents the fluid with the lower specific gravity from being drawn into the siphon tube  267 . 
     It is also contemplated that in some embodiments conventional sensors will be used to regulate the flow of processed fluid into the separation system such that the level of the fluid with the higher specific gravity remains above siphon tube  267  and below outflow line  262 . 
     It is contemplated that embodiments of the inventions disclosed herein may be used in series or in parallel depending on the nature and volume of the fluid being processed and the nature and number of fluids being separated from the processed fluid.  FIGS. 12 and 13  depict an embodiment adapted to process a larger quantity of fluid and separating three fluids from the processed fluid, specifically, a gas and two liquids having different specific gravities, more specifically, gaseous hydrocarbons, oil and water. 
     As depicted in  FIG. 13 , a main inlet line  270  supplies the fluid being processed to a pair of inlet valves  272 . As noted above, inlet valves  272  may be controlled to manage the fluid levels in the collection chamber  256  based upon output from conventional sensors in the collection chamber  256 . Check valves  274  are adjacent to the inlet valves  272 . The system depicted has a pair of optional agitation chambers  218 , as described above. Each agitation chamber  218  supplies fluid to two separation chambers  236 , as previously described. Each separation chamber  236  is connected to the collection chamber  256  by collection chamber inlet piping  252 . 
     In the embodiment described, for a flow rate of 250 gpm, it is contemplated that the separation inlet piping  234  has a diameter of 8 inches. The separation chambers  236  have a 60 inch inside diameter. The base of the first baffle  242  is 2 feet, 1 and 13/16th inches from the bottom of the separation chambers  236 . The base of the second baffle  244  is one foot, 3 13/16 inches from the base of the first baffle  242 . The apex of the third baffle  248  is one foot 7 5/16 inches from the base of the second baffle  244 . Each baffle  242 ,  244 ,  248  tapers approximately 1.5 to 2 degrees from horizontal as it progresses from base to apex. The separation chambers  236  are eight feet 5 inches tall. 
     The base of the collection chamber  256  has an outside diameter of 48 inches and the inlet of the siphon tube  266  is one foot 6 inches above the bottom of the collection chamber  256 . The collection chamber  256  is 13 feet, 6 and 11/16th inches tall. The bottom of the outflow line  262  is 15 inches below the top of the collection chamber  256 . The bottom of the collection chamber inlet piping is nine feet 11/16 inches above the bottom of the collection chamber  256 . 
     One skilled in the art will recognize that the principals of the claimed invention can be practiced in a number of different ways. By way of example, one of ordinary skill will recognize that the number, placement and shape of the baffles and heating elements may by modified to achieve the desired result. Moreover, the configuration of the baffles and the described inlet and outlet plates could be modified and achieve the same purpose. For example, the conical baffles described could be replaced by planar baffles positioned at an angle with apertures at the downstream side of the angled baffle and the downstream side of the angle baffle being upward of the lower portion of the baffle. Similarly, the inlet and outlet plates could be replaced by a series of baffles causing repeated velocity charges. 
     One skilled in the art will recognize that components may be eliminated without significantly affecting the functionality of the disclosed systems. For example, the strainer and screen could be eliminated and the system would perform substantially the same way. 
     The invention can be scaled for larger or smaller flows. The agitation chamber and/or separation chamber can be arraigned in parallel or series, or used in the opposite order, depending on the conditions of the fluid mixture to be processed and the requirements of the specific location. In some settings the agitation chamber may be undesirable. 
     After reviewing the disclosure of the claimed invention, numerous modifications would be apparent to one of ordinary skill in the art to achieve the same result as the claimed invention.