the systems herein described provide methods for handling raw animal waste and converting the waste into fuel , which may then be used for heat , transportation , or preferably direct conversion to power through a generator driven by an engine or combustion turbine . referring to fig1 , animal confinement 10 includes a manure collection area 12 for the collection of wastes and flushing water . the wastes and flushing water are transported to solid / liquid separator 14 utilizing a transporting mechanism 16 . in one embodiment , transporting mechanism 16 operates by gravity , but other embodiments of transporting mechanism 16 exist which may also use pumps and / or conveyors in addition to or instead of gravity to transport animal waste and other accompanying materials . as used herein , the term “ transport ” is utilized to describe methods for moving mass from one location to another , including , but not limited to , pumping , gravity , auger , conveyor , and the like . in a specific embodiment , a positive displacement pump designed for high solids contents is utilized for transporting animal waste from collection area 12 to solid / liquid separator 14 . one positive displacement pump is a grinding pump , one example of which is a moyno l - frame progressing cavity pump . solid / liquid separator 14 may include one or more mechanical and gravity separators which are further described below . a gravity separator is sometimes referred to as a settling tank . in one embodiment , solid / liquid separator 14 is utilized to deliver volatile solids from the waste , which have a significant btu content for use as fuel , to an energy conversion processor 20 . as further described below , the solid wastes are delivered to energy conversion processor 20 within a specified range of moisture content . the animal waste exiting manure collection area 12 is typically about 97 % to about 99 . 5 % liquid . this is a result of manure by nature being very wet . additional moisture is added due to urine and the water used to flush the animal waste from confinement 10 . small additional amounts of water are contributed to the animal waste by sloppy drinking and animal cleaning . hog manure , for example , is typically about 80 %- 90 % liquid by weight . each embodiment of energy conversion processor 20 has a range for the moisture content of the solid waste being converted that enables proper conversion of the solid waste . for example , the well - known gasification process typically requires a relatively dry feedstock , for example , a fuel with about a 20 % to about a 30 % moisture level . by contrast , other conversion processes such as liquification or pyrolysis allow much wetter feedstock streams , up to about an 80 % moisture level . as described above , the animal waste is transported into energy conversion processor , which may use pyrolysis , gasification , or one of a number of related conversion processes that utilize controlled temperature , pressure , and time to convert the waste into a one of a fuel gas , an oil , a solid , or a combination thereof . the converted animal waste is referred to herein as “ fuel ”. from energy conversion processor 20 , the fuel is filtered and processed by filter processor 22 as necessary for usage . in one embodiment , the system includes one or more optional fuel storage tanks 24 , or buffer tank ( s ). the fuel is then converted into electricity through a known device such as an engine or turbine - driven generator 26 . in the embodiment illustrated , a second power generator 28 is illustrated . in many locations , electrical power is more valuable during “ peak demand ” periods . one feature of the system illustrated is that power generator 26 is utilized to supply a certain quantity of power , while second power generator 28 supplies another quantity . power generator 26 and second power generator 28 may provide equal power or may provide different power amounts ( i . e ., be differently sized ). in a particular embodiment , power generator 26 supplies electricity and engine heat sufficient to keep the processes of the illustrated system continuously running except for maintenance . second power generator 28 is turned on when power demand is at a peak . in a specific embodiment , power generator 26 is a kohler 150reozv and second power generator 28 is a kohler 500reozv . operation of second power generator 28 , in one embodiment , is controlled by a controller 30 , which includes a timer ( not shown ), operating in conjunction with a level controller 32 , having a sensor input 34 . controller 30 may also be controlled remotely by a remote signal 36 from a utility or an operator of the energy conversion system illustrated . this operation enables the energy conversion system to meet electrical load demand and also maximize economic benefit to the system &# 39 ; s owner . such operation provides benefits to the public and the electrical grid operators by reducing loading on transmission lines , by providing demand - based distributed generation . additionally , fuel production will vary due to fluctuations in manure production and other factors . the twin power generator arrangement provides a solution for the fluctuations in fuel supply while allowing generators to run at peak efficiency . there is typically wastewater generated by the energy conversion system in the conversion process , either within energy conversion processor 20 or in filter / processor 22 . this wastewater is transported , by pump and / or gravity , to a water treatment apparatus 40 , which removes any remaining entrained solids , liquids and gases to levels approved by the applicable authorities . water from water treatment apparatus 40 is either discharged to water bodies , or used for crop irrigation , or any number of other useful purposes that displace water currently taken from ground sources and / or water bodies . in a particular embodiment , the water is transported back to confinement 10 for a variety of purposes . as illustrated in fig1 , a holding tank 42 has a level control valve 44 that allows holding tank 42 to fill as needed . a control valve and / or pump 46 transmits the water through a flush line 48 into manure pit 12 as needed in order to provide the flushing water needed to clean manure out of confinement 10 . in one embodiment , water is also be pumped to devices which filter the air exiting confinement 10 via ventilation system 50 . an example of such a device is an air scrubber 52 as described in u . s . pat . no . 6 , 059 , 865 . water washes down an inclined plate ( not shown ) of air scrubber 52 , as ventilation fans blow against the inclined plate . odor containing particles and gases are captured within the water stream . this water is shown as being returned to holding tank 42 . the water can alternately be returned to water treatment apparatus 40 or utilized directly for flushing of manure pit 12 . fig2 illustrates one embodiment of solid / liquid separator 14 ( shown in fig1 ). certain energy conversion processes utilize a low moisture level , for example , gasification . in such energy conversion processes , solid / liquid separator 14 may include one or more mechanical separators 60 . individual mechanical separators 60 may be a type of press ( e . g ., a belt press ), an auger , a conveyor , a centrifuge , a hydrocyclone , a screen separator , or another type of mechanical separator , alone , or in conjunction with one or more other mechanical separators that work in conjunction to remove substantially all of the useful volatile solids from the waste . at least some known mechanical separation equipment leaves much of the useful volatile solids in the wastewater . in the embodiment of solid / liquid separator 14 illustrated in fig2 , any solids retained in the waste are forwarded from mechanical separator 60 to settling tank 62 , either by gravity and / or by pumping . some examples of mechanical separator 60 are the kcs & amp ; c 48x30 centrifuge , or vincent kp - 6l screw press . settling tank 62 allows the retained solids to gravitate toward a bottom 64 of a fixed tank , while the liquid portion is forwarded for water treatment 66 . in additional embodiments , settling tank 62 may include more than one settling tank in series or parallel . the solids that gravitate toward bottom 64 of settling tank 62 are transported back to mechanical separator 60 , either directly , or to a buffer tank 68 , as illustrated in fig2 . the solids stream from mechanical separator 60 are forwarded , in one embodiment , to a shredder 70 . a shredder 70 may not be needed for some animal waste streams , and its function may be replaced by a standard pump or a grinding pump . the waste is then transported , either by pump or gravity , to a dryer 72 . in the embodiment shown in fig2 , dryer 72 is a helical auger in which heat and / or air is added to the unit , lowering the moisture content of the waste to meet the operating conditions of energy conversion processor 20 . in the embodiment shown , moisture content of the waste is controlled by a moisture sensor 74 that monitors the amount of heat and airflow entering dryer 72 . moisture sensor 74 provides an analog or digital signal to the moisture controller ( mic ) 76 . moisture controller 76 is configured to vary a process variable to control the moisture level of the waste within pre - defined limitations for use by energy conversion processor 20 . a particular embodiment utilizes an omega cdce - 90 - 1 moisture sensor , and an omega cdcn - 90 moisture controller . in this embodiment , moisture sensor 74 provides a proportional signal to moisture controller 76 . an output of moisture controller 76 is utilized to control devices affecting the moisture percentage of the waste . in particular embodiments , if moisture sensor 74 indicates that the moisture percentage is too high to be processed properly by energy conversion processor 20 , then a hot air flow that is applied to the waste stream entering energy conversion processor 20 is increased . the hot air may be generated utilizing a variety of methods and one exemplary embodiment is illustrated in fig2 , where a coolant 80 from a power generator 82 is passed through a heat exchanger 84 , where heat is transferred to the incoming air in order to raise its temperature , which increases its capacity to remove moisture from the process stream . a variable speed blower 86 has a variable frequency drive or other modulating device such as a mechanical damper , that is controlled by the signal output by moisture controller 76 . in a specific embodiment , heat exchanger 84 is a pipe - in - pipe heat exchanger manufactured by a variety of other manufacturers and blower 86 is manufactured by the new york blower company . in other embodiments , drying methods include raising the temperature of the waste through electric or fuel fired heaters or heat exchanged from other higher temperature areas of the process via fluid , gas or steam heat exchange media . alternately , gases from engine exhaust of power generator 82 or energy conversion processor 20 can be utilized directly , similarly to the hot air embodiment above described . in one embodiment , dryer 72 includes a perforated top screen ( not shown ) which allows the warmed moist air to escape . in other embodiments , the airflow is constant , but the amount of heat is varied , for example by a three - way valve modulating the amount of hot engine fluid ( e . g ., coolant 80 ) delivered to heat exchanger 84 . alternately other process variables such as rotation speed of dryer 72 or temperature of heating media may be controlled to obtain the same effect . other heat sources may be used , such as engine exhaust from power generator 82 , heat from energy conversion processor 20 , heat from the process stream 88 after energy conversion processor 20 , solar - heated thermal fluid , or heat from a separate combustion process , such as burning paraffins separated from the resultant fuel . fig3 illustrates an alternate embodiment where energy conversion processor 20 is configured to utilize or allow higher moisture content feedstock ( e . g ., animal waste streams ). in this embodiment , a portion of the solids stream from settling tank 62 is delivered to the line which contains the solid portion from mechanical separator 60 . the amount of this stream from settling tank 62 is controlled by moisture controller ( mic ) 76 , based on an input from moisture sensor 74 or a similar instrumentation means . alternately the amount of solids from settling tank 62 is controlled by simple experimental manual balancing . in the embodiment illustrated a three way control valve 100 and moisture sensor 74 are used to control the amount of solids from settling tank 62 into the waste stream . alternatively one or more two - way control valves or solenoid operated valves may be utilized . the waste stream is exposed to heat from heat exchanger 84 before entry into energy conversion processor 20 . the heat for heat exchanger 74 may be provided from a variety of sources . in a specific embodiment , heat may be provided to heat exchanger 84 from a power generator ( shown in fig1 ) from one or more of exhaust and engine cooling water . the waste stream in effect replaces the engine &# 39 ; s radiator , in part or in whole . additional heat sources may be used such as solar thermal , electric heat run by the unit &# 39 ; s generator or other power source , or direct firing of a portion of the fuel , or waste fractions of the fuel . the heated waste is then transported to energy conversion processor 20 and processed as described with respect to fig1 . fig4 illustrates an alternate embodiment of a solids / liquids separator 110 for energy conversion system which increases efficiency of separation between solids and liquids in the waste stream . in addition to mechanical separator 60 , a second mechanical separator 112 is included . mechanical separator 60 and second mechanical separator 112 may be of the same type of construction , but in a specific embodiment , mechanical separator 60 is a highly energy efficient type separator , for example , a press , while second mechanical separator 100 is a more energy intensive separator , such as a centrifuge . in the embodiment , second mechanical separator 112 processes less mass flow than does mechanical separator 60 thereby raising overall efficiency of the energy conversion system . specifically , mechanical separator 60 directs the high - solids fraction of the waste towards energy conversion processor 20 , while a high - liquids fraction of the waste is transported to second mechanical separator 112 . second mechanical separator 112 also directs its high - solids fraction toward energy conversion processor 20 , while the high - liquids fraction is directed to settling tank 62 . from settling tank 62 , a high - solids fraction of the waste is directed back to buffer tank 68 or alternately to one or both of mechanical separators 60 , 112 and another fraction is transported toward energy conversion processor 20 . three - way valve 100 , which is controlled by moisture controller ( mic ) 76 , based on the input from moisture sensor 74 . three - way valve 100 varies the amount of high - solids waste fraction transported toward either energy conversion processor 20 and buffer tank 68 , or alternately between first and second mechanical separators 60 , 112 . fig5 illustrates another embodiment of a solids / liquids separator 120 for energy conversion system which also increases efficiency of separation between liquids and solids in a waste stream . solids / liquids separator 120 includes a second settling tank 122 , which may be of the same type of construction as settling tank 62 , but typically will have a different geometry . settling tank 122 directs the high - solids fraction of the waste towards energy conversion processor 20 , while the high - liquids fraction of the waste from second settling tank 122 is transported to settling tank 62 . settling tank 62 transports its high - liquids fraction to waste water treatment ( e . g ., apparatus 40 shown in fig1 ). the prime advantages of gravity separation utilizing settling tanks are low energy consumption and high recovery of solids . putting two gravity separators in series ( i . e ., settling tanks 62 and 122 ) downstream of mechanical separator 60 is thought to recover approximately 97 % of the solids . the high - solids fractions of waste from both gravity separators 62 , 122 are transported back to buffer tank 68 or combined with an output from mechanical separator 60 and directed to shredder 70 and onto energy conversion processor 20 . a three - way valve 124 operates in the same fashion as three way valve 100 described above , that is , controlled by moisture controller ( mic ) 76 , based on an input from moisture sensor 74 . three - way valves vary an amount of high - solids waste transported toward energy conversion processor 20 , buffer tank 68 , and mechanical separator 60 . for all of the above described embodiments , it should be easily understood that many variations can be made and still be within the spirit and scope herein described . for example , altering the arrangements and quantity of separators , such as three or more separators in a parallel or series - parallel arrangements are certainly contemplated . fig6 displays one embodiment of a heat recovery system 140 which may be utilize to improve and / or optimize the processes performed by the energy conversion system . in the illustrated embodiment , the waste stream is heated via heat recovered from the cooling fluid of power generator 142 , typically a glycol / water mix , via heat exchanger 144 . the waste is further heated in a second heat exchanger 146 , using steam and / or exhaust gases available from energy conversion processor 20 . these may alternately be taken from a vessel within energy conversion processor 20 or a downstream apparatus such as a flash tank as utilized in the petroleum industry . another source of heat recovery is shown which circulates a heat transfer medium through heat exchangers 148 , 150 . the heat transfer medium transfers heat from the hot fuel from energy conversion processor to the incoming waste stream , preheating it , raising overall efficiency . additional process control instrumentation is also illustrated in fig6 by way of example only . recovery of constituents of exhaust gases is important with certain embodiments of energy conversion processor 20 . for example , one embodiment of energy conversion processors require carbon monoxide ( co ) and / or carbon dioxide ( co2 ), which are readily available in significant quantities from the exhaust of an engine and / or combustion processes . in the embodiment shown , a portion of the exhaust gas is separated by gas separator 152 for delivery to energy conversion processor 20 . the exhaust gas may be filtered , or chemically converted ( for example converting co2 into co and o2 ) to deliver the desired gas or gases to energy conversion processor 20 . in one embodiment , membrane technology is utilized within gas separator 152 to concentrate the amount of one gas , for example co , for delivery into the process . other more complex gas separation methods such as pressure - swing absorption , vacuum swing absorption , chemical separation , catalytic separation , and other gas separation methods may be utilized to accomplish the same goal of delivering a more desirable mix of gas to energy conversion processor 20 . the gas separation process typically utilizes a compressor for the feed gas ( exhaust ), or one or more vacuum pumps . fig7 illustrates another embodiment for a solids / liquids separator 170 for an energy conversion system which controls a solids percentage , primarily for a low - solids energy conversion processor 20 . solids / liquids separator 170 includes one or more gravity separators ( settling tanks 62 , 122 shown ). the high - solids fraction of the waste from each settling tank 62 , 122 is transported toward energy conversion processor 20 , except that a fraction of the high - solids fraction is directed through mechanical separator 60 , which raises the solids percentage of the waste to a desired level for input into energy conversion processor 20 . a three - way valve 172 is controlled by the moisture controller ( mic ) 76 , based on an input from moisture sensor ( mt ) 74 . three - way valve 172 could alternately be a combination of two - way valves and / or manual valves . the liquid fraction of the waste from mechanical separator 60 can alternately be transported to buffer tank 68 or directly to one of settling tanks 62 , 122 . fig8 illustrates one example of an energy conversion processor 200 . in the example illustrated , pump 202 raises pressure of the waste within energy conversion processor 200 . as described above , the waste has been controlled to a specified moisture level . the waste is pumped through a length of tubing 204 . a example includes 1000 ′ of 1 . 5 inch nps schedule 80 304ss with an inside diameter of about 1 . 5 ″, which coiled in about a 12 foot diameter , with 27 turns . a flowrate of approximately 4 . 6 gpm is pumped into energy conversion processor 200 . a step down transformer 206 converts 480 volt , single phase power from power 208 generator to a low voltage , for example 30 vac . temperature sensor 210 provides a signal to temperature controller 212 . the amount of power from power generator 208 delivered to energy conversion processor 200 is controlled by power controller 214 . power controller 214 , in one embodiment , is the phase angle scr ( silicon controlled rectifier ) type or another similar type . a specific scr type power controller is supplied by eurotherm . power controller 214 delivers an amount of power to step down transformer 206 proportional to the signal received from temperature controller 212 . power controller 214 regulates the voltage applied to the primary of transformer 206 , which regulates the voltage applied to energy conversion processor 200 by the same ratio . such an arrangement maintains the temperature of the waste at the outlet 216 of energy conversion processor 200 . another embodiment , not shown , utilizes multiple zones , for example , two transformers 206 , two power controllers 214 , two temperature sensors 210 , and two temperature controllers 212 , where each zone may have differing temperature setpoints or the same temperature setpoint to have a zone of temperature rise rather then a zone of maintaining temperature . in one embodiment , tubing 204 of energy conversion processor 200 includes a jacketed pipe wherein heat from a power generator is applied as one of heated fluid or heated gas to the jacketed pipe to maintain desired temperature setpoints . in this and other embodiments , heat from a power generator is therefore applied to the waste stream within energy conversion processor ( 20 , 200 ) by one or more of impedance and induction , in one or more distinct zones of heating . the above described embodiments are utilized to control an amount of moisture within a waste stream to attempt to provide an optimum waste for the particular energy conversion processor 20 . when energy conversion processor 20 is a gasification processor , a moisture percentage entering mechanical separator 60 , for example , an inclined screw press , is about 95 %. the moisture percentage in the high - solids stream exiting mechanical separator 60 is about 65 %. the mass fraction of solids forwarded to shredder 70 is then about 30 %. the remaining 70 % mass fraction of waste is forwarded to a gravity separator ( e . g ., settling tank 62 ). the solid fractions in the gravity separator are continually recycled to buffer tank 68 , where it is mixed with fresh slurry and reintroduced into mechanical separator 60 . for the waste stream exiting shredder 70 , hot air is introduced into dryer 72 ( shown in fig2 , and is regulated as described above to reduce the moisture percentage in the waste stream being fed to energy conversion processor 20 to about 25 %. when energy conversion processor 20 is a pyrolysis or liquification processor , a moisture percentage entering mechanical separator 60 , for example , a solid bowl basket centrifuge , is about 97 %. the moisture percentage in the high - solids stream exiting mechanical separator 60 is about 72 %. the mass fraction of solids forwarded to shredder 70 is then about 65 %. the remaining 35 % mass fraction is forwarded to a gravity separator ( e . g ., settling tank 62 ). the moisture percentage of the solid fraction in the gravity separator is about 90 %. the flow from gravity separator is divided at a three - way valve , with nominally 50 % of the flow directed to the pipe connecting mechanical separator 60 and shredder 70 . this results in a desired mixture moisture percentage of about 80 % in this case . the three - way valve position is regulated as previously described , to maintain this moisture percentage setpoint . the remaining high - solids stream from the gravity separator is continually recycled to buffer tank 68 , where it is mixed with fresh slurry and reintroduced into the mechanical separator . the above described embodiments and examples serve to illustrate how control of moisture content from a waste stream is utilized by a number of different energy conversion processor types in order to provide a method for disposing of and gaining beneficial use from animal production waste streams . the above described embodiments also do not involve methods that contribute to odor released into the atmosphere , providing a more desirable approach to the problem of animal production waste than known solutions which include lagoons and field spreading . while the invention has been described in terms of various specific embodiments , those skilled in the art will recognize that the invention can be practiced with modification within the spirit and scope of the claims .