Patent Publication Number: US-2023134703-A1

Title: Electric-powered, closed-loop, continuous-feed, endothermic energy-conversion systems and methods

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
     This application is a continuation and claims priority to U.S. patent application Ser. No. 17/409,159 filed Aug. 23, 2021, which is a continuation and claims priority to U.S. patent application Ser. No. 16/622,684 filed Dec. 13, 2019 (now U.S. Pat. No. 11,097,245), which is a 35 U.S.C. § 371 U.S. National Phase entry of International Application No. PCT/US2018/037445 entitled “Electric-Powered, Closed-Loop, Continuous-Feed, Endothermic Energy-Conversion Systems and Methods” having an international filing date of Jun. 14, 2018, which claims the benefit of U.S. Provisional Patent Application Ser. No. 62/519,213 filed Jun. 14, 2017, the entire disclosures of which are incorporated herein by reference. 
    
    
     TECHNICAL FIELD 
     The presently disclosed subject matter relates generally to energy-conversion processes and more particularly to electric-powered, closed-loop, continuous-feed, endothermic energy-conversion systems and methods. 
     BACKGROUND 
     Current energy-conversion processes, such as incineration, gasification, fluidized beds, updraft, downdraft, and low-temperature pyrolysis, all result in heavily regulated air emissions, waste water effluents, and/or other by-products, which can often limit the operating parameters and permitting of the system. 
     Further, current energy-conversion processes, such as incineration bio-digesters, low-temperature pyrolysis, and gasification systems, focus primarily on the capture of bio-gases yet only recover a small fraction of the available energy, and only minimally reduce the volume of feedstock solids, if at all. Conventional systems operate in heat ranges that cannot isolate metals, minerals, and nutrients in a reusable format. Consequently, the residuals must be landfilled or land applied, which is highly regulated if not prohibited in many jurisdictions. Disposal is further complicated by the presence of hazardous contaminates, medical residuals, and pathogens. Accordingly, there are both regulatory and financial implications with regard to disposal of these solids. 
     SUMMARY 
     In accordance with a first aspect of the present invention there are provided systems and methods for energy conversion. The systems and methods may include electric-powered, closed-loop, continuous-feed, endothermic energy-conversion systems and methods featuring mechanisms for natural resource recovery, refining, and/or recycling, such as secondary recovery of metals, minerals, nutrients, and/or carbon char. 
     Certain embodiments of the invention envisage a system comprising: a controller; a reactor managed by the controller; a shaftless auger in the reactor; and a heater surrounding the reactor and shaftless auger, wherein the system is closed-loop. In other embodiments, the system may further include components such as a scale, mixer, feedstock hoper metering stage, infeed sensor, and airlock. In still other embodiments, the system may include a compensator for maintaining pressure within the reactor. In yet other embodiments, the system may include a vapor pre-heating stage, a ceramic hot gas filter, a quench stage, a pass-through multi-tube plunging condenser, a compensator with an associated recirculator, a vacuum buffer tank, a regulator, a vacuum pump, a syngas buffer tank, and a catalytic scrub. Further, the system may include an automated plunging system. Still further, the system may include a pressure transition component. 
     In other embodiments, the system of the present invention may include a drag conveyor instead of a shaftless auger as described above. This embodiment may include an airlock with a high-temperature fluid bath. In still other embodiments, the system may include a multi-zone quench station and atmosphere fractioning unit. 
     Certain embodiments of the present invention envisage a method that may include, but is not limited to, the following steps: providing an energy-conversion system as described above; supplying feedstock material to the energy-conversion system; processing the feedstock material; supplying the processed feedstock material to the inlet of the reactor; advancing the processed feedstock through the reactor while the reactor facilitates a phase-change process of the feedstock from solid to liquid to vapor; maintaining through multi-zone heater accurate and consistent temperature within reactor; maintaining a positive pressure in the system; discharging from reactor outlets char and vapor obtained from reacted feedstock; removing particulates from the discharged vapor; quenching discharged vapor to prevent tar, grease, and/or wax build-ups; after quenching step, transitioning from the positive pressure to a negative pressure in the system; supplying the quenched vapor to a vacuum buffer tank; removing liquid from the vapor cooling the vapor performing a filter-less quenching gas clean-up operation and discharging syngas; and balancing the energy-conversion system through a closed-loop. 
     Other aspects and features of the present invention will become evident from a review of the Drawing and Detailed Description provided. 
    
    
     
       BRIEF DESCRIPTION OF DRAWINGS 
       Having thus described the presently disclosed subject matter in general terms, reference will now be made to the accompanying Drawings, which are not necessarily drawn to scale, and wherein: 
         FIG.  1    illustrates a block diagram of an energy-conversion system that includes a shaftless auger, according to one embodiment of the presently disclosed electric-powered, closed-loop, continuous-feed, endothermic energy-conversion system; 
         FIG.  2    illustrates a block diagram of an energy-conversion system that includes a drag conveyor, according to another embodiment of the presently disclosed electric-powered, closed-loop, continuous-feed, endothermic energy-conversion system; 
         FIG.  3    illustrates a block diagram of an energy-conversion system that includes a distillation and/or fractionating stage, according to yet another embodiment of the presently disclosed electric-powered, closed-loop, continuous-feed, endothermic energy-conversion system; 
         FIG.  4    through  FIG.  25    show various views of one example instantiation of the shaftless auger-based energy-conversion system shown in  FIG.  1   ; 
         FIG.  26    illustrates a flow diagram of an example of a method of operation of the shaftless auger-based energy-conversion system shown in  FIG.  1   ; and 
         FIG.  27    through  FIG.  56    show various views of one example instantiation of the drag conveyor-based energy-conversion system shown in  FIG.  2   . 
     
    
    
     DETAILED DESCRIPTION 
     The presently disclosed subject matter now will be described more fully hereinafter with reference to the accompanying Drawings, in which some, but not all embodiments of the presently disclosed subject matter are shown. Like numbers refer to like elements throughout. The presently disclosed subject matter may be embodied in many different forms and should not be construed as limited to the embodiments set forth herein; rather, these embodiments are provided so that this disclosure will satisfy applicable legal requirements. Indeed, many modifications and other embodiments of the presently disclosed subject matter set forth herein will come to mind to one skilled in the art to which the presently disclosed subject matter pertains having the benefit of the teachings presented in the foregoing descriptions and the associated Drawings. Therefore, it is to be understood that the presently disclosed subject matter is not to be limited to the specific embodiments disclosed and that modifications and other embodiments are intended to be included within the scope of the appended claims. 
     In some embodiments, the presently disclosed subject matter provides electric-powered, closed-loop, continuous-feed, endothermic energy-conversion systems and methods. The presently disclosed endothermic energy-conversion systems and methods feature mechanisms for natural resource recovery, refining, and recycling, such as secondary recovery of metals, minerals, nutrients, and/or carbon char. 
     In one embodiment, the presently disclosed electric-powered, closed-loop, continuous-feed, endothermic energy-conversion system includes a shaftless auger. In another embodiment, the presently disclosed electric-powered, closed-loop, continuous-feed, endothermic energy-conversion system includes a drag conveyor. In yet another embodiment, the presently disclosed electric-powered, closed-loop, continuous-feed, endothermic energy-conversion system includes a distillation and/or fractionating stage or component. In still another embodiment, the presently disclosed electric-powered, closed-loop, continuous-feed, endothermic energy-conversion system includes a catalytic-heated reactor. 
     In some embodiments, the presently disclosed endothermic energy-conversion systems and methods provide a positive energy balance. For example, in the endothermic energy-conversion systems and methods, any feedstock that is about &gt;3000 BTU/pound dry basis will result in positive net energy. 
     In some embodiments, the presently disclosed endothermic energy-conversion systems and methods is substantially emissions-free and provides substantially effluent-free conversion of animal-waste, bio-mass, coal, rubber and/or municipal-solid-waste into renewable energy formats including syngas, gasoline, diesel, electricity. Namely, the presently disclosed endothermic energy-conversion systems and methods provide a closed-loop system that has substantially no air emissions/pollution, waste water effluent/pollution, and produces no additional unmarketable products. As a result, there may be few or no regulatory constraints on operations and permitting. 
     In some embodiments, the presently disclosed endothermic energy-conversion systems and methods has capability to recover the non-energy fraction of the feedstock into a prescriptive carbon-char that has commercial re-sale value as a soil amendment, an animal feed supplement, or as a filtration media. Further, it has capability to recover the liquid condensable fraction of the conversion process. Further, it allows marketing and selling commercially recovered product where possible and refining product to allow re-sale into the market where needed. Further, the non-condensable fraction of the conversion process can be fractionated into a producer gas. 
     In some embodiments, the presently disclosed endothermic energy-conversion systems and methods may: (1) reduce feedstock volume by up to about 85% while preserving the resident metals, minerals, and nutrients; (2) condense the residual metals, minerals, and nutrients into a pathogen-free, medical residual-free carbon char that can be further fractionated into its component parts; (3) because of the reduced feedstock volume, minimize shipping expense and maximize re-sale/radius; (4) provide substantially pathogen-free, medical residual-free status that reduces or entirely eliminates regulatory barriers to beneficial reuse or use in whole as an animal feed supplement or a soil amendment to minimize with no regulatory constraint on commercial re-sale; (5) provide improved economics of char recycling/re-sale, which allows for an economically viable self-sustaining renewable energy loop; and (6) receive the residuals from current energy-conversion systems and process them as a feedstock. 
     In some embodiments, the presently disclosed endothermic energy-conversion systems and methods require no-landfilling or land-application of residuals. Namely, the system may allow for full conversion of substantially the entire feedstock by converting substantially all volatiles into renewable energy and then reformatting the residuals metals, minerals, and nutrients into byproducts with commercially viable beneficial extended life reuse. For example, the presently disclosed endothermic energy-conversion systems and methods may: (1) reduce or entirely eliminate the need for landfilling or land application of residuals; (2) reduce or entirely eliminate the expense of landfilling; (3) reduce or entirely eliminate regulatory burden and expense; and (4) be used to clean up large stockpiles of residual waste from existing current energy-conversion systems. 
     Referring now to  FIG.  1    is a block diagram of an energy-conversion system  100  that includes a shaftless auger, according to one embodiment of the presently disclosed electric-powered, closed-loop, continuous-feed, endothermic energy-conversion system. Energy-conversion system  100  is typically a closed-loop system that (1) eliminates substantially all emissions and effluents; (2) recovers substantially all residual carbon, metals, minerals, and nutrients for beneficial reuse; (3) reuses residual/waste heat; and (4) reduces or entirely eliminates parasitic loss of potential energy. 
     Energy-conversion system  100  includes a controller  105 . Controller  105  is used to manage the overall operations of energy-conversion system  100 . Controller  105  can be any computing device that is capable of executing program instructions. Controller  105  can be, for example, a server, a desktop computer, a laptop computer, a tablet device, a smartphone, a smartwatch, a cloud computing device, and the like. 
     Energy-conversion system  100  also includes a reactor  110 , also known as a conversion chamber or conversion reactor. Reactor  110  is an electrically controlled and heated reactor. Reactor  110  is typically a pipe or tube that is equipped with multi-zoned electric heat. Namely, a shaftless auger  112  is installed in reactor  110 . Further, a multi-zone heater  114  surrounds the assembly of the reactor  110  and shaftless auger  112 . In one example, reactor  110  is a pipe or tube that is about 30 feet (about 9.1 meters) long and about 12 inches (about 30.48 cm) in diameter. However, reactor  110  can be any length and diameter and the shaftless auger  112  can be sized accordingly. Namely, the length of reactor  110  may be determined by the amount of residence time needed in the system. Further, reactor  110  can be formed, for example, of carbon steel, stainless steel, or specialized alloys, such as, but not limited to, selected Inconel alloys (i.e., a family of austenitic nickel-chromium-based superalloys). 
     Conventional continuous-feed energy-conversion systems often utilize shafted auger systems that are problematic with exposure to high heat. In these systems, the shafted auger is aligned and centered with bearings at both ends of the conversion chamber, as the auger is subjected to heat creep or thermal growth occurs. The conversion chamber (i.e., the pipe), shaft, and flights may expand (i.e., thermal expansion) at different rates. This creates alignment problems because the shaft expands slower than the flights and therefore the shaft often experiences warping. The shaft additionally carries the weight of the auger and when subjected to heat will sag or deflect depending on the length. Further, in conventional systems, the weld connections between the flight and shaft also are stressed with creep and will ultimately fail. Tolerances from pipe to flight on the shafted auger have to be adequate to allow rotation in the presence of a warping and/or sagging shaft. 
     The inclusion of shaftless auger  112  in energy-conversion system  100  mitigates many of the problems associated with shafted augers. Namely, shaftless auger  112  is designed to rotate in direct contact to reactor  110  (i.e., the pipe or trough) and, at elevated temperature, can experience galling. Shaftless auger  112  is allowed to be supported by the pipe, which ensures alignment and removes the length limitation created by weight. Additionally, centering shaftless auger  112  on the non-drive-end of shaftless auger  112  is eliminated, which allows shaftless auger  112  to experience creep growth with no effect on bearings or seals. Shaftless auger  112  being in direct contact with the inner walls of reactor  110  (i.e., the pipe or trough) also promotes scouring and maintaining of direct surface contact with feedstock, thereby ensuring thermal conductivity. The mass of auger  112  being in direct contact with reactor  110  (i.e., the pipe or trough) also increases thermal conductive surface area, which ensures high conduction rate of heat energy to feedstock. 
     Shaftless auger  112  is typically a single penetration auger that reduces wear and tear on bearings and seals as compared with multiple penetration augers of conventional conversion chambers. Shaftless auger  112  is in direct contact with the inner walls of reactor  110  (i.e., the pipe or trough), which increases scouring and self-cleaning as compared with augers of conventional conversion chambers that have no contact with the pipe and provide minimal scouring. Shaftless auger  112  ensures high thermal conduction and energy efficiency by substantially eliminating deposited material between reactor  110  and shaftless auger  112 . Because there is no shaft, shaftless auger  112  eliminates differential growth rates between shaft and flights which cause metal fatigue and failure. Because there is no shaft, shaftless auger  112  eliminates chronic issues that conventional conversion chambers have with respect to warping of the shaft. Because there is no shaft, shaftless auger  112  eliminates high-heat weld failure on the auger as there is no need to connect flights to the shaft. Shaftless auger  112  allows fixed creep and growth direction of the auger in reactor  110  without a second penetration point. Shaftless auger  112  can be formed of specialized alloys, such as, but not limited to, selected Inconel alloys, and protected with dissimilar alloy wear strips to prevent galling of similar metals with direct contact of the auger to the pipe or trough. Galling is adhesive wear caused by microscopic transfer of material between metallic surfaces, during transverse motion/sliding. Galling occurs frequently whenever metal surfaces are in contact, sliding against each other, especially with poor lubrication. Also, shaftless auger  112  can be formed of the specialized alloys (e.g., Inconel 625 alloys) to prevent chlorine migration and hydrogen embrittlement. However, in other embodiments, shaftless auger  112  can be formed of carbon steel or stainless steel. Shaftless auger  112  creates an agitating and stirring effect of the feedstock, which facilitates more efficient heat distribution. 
     Using multi-zone heater  114 , reactor  110  is an electric heat conversion chamber; namely, a multi-zone electrically heated oven. In one example, multi-zone heater  114  provides six (6) individually controlled heating zones within reactor  110 . Multi-zone heater  114  provides heat energy for both start-up and the feedstock conversion process. Multi-zone heater  114  provides precisely controlled chamber temperatures for prescriptive outcomes, such as pathogen-free and/or medical residual-free. Multi-zone heater  114  provides for very precise control of temperature bands for prescriptive fractioning and refining of distillates and chars. Multi-zone heater  114  is capable to provide heat ranging from about 100° F. (about 38° C.) to about 2500° F. (about 1371° C.). Multi-zone heater  114  provides for substantially instantaneous response to sensor driven heat demand Using multi-zone heater  114  eliminates air emissions and the need for an exhaust stack. Using multi-zone heater  114  eliminates atmospheric heat loss through exhaust stack. Further, the use of electric heat in reactor  110  eliminates natural gas or propane emissions from the conversion process. As a result, the use of the electric-heat reactor  110  requires no air permit for the conversion process. Further, reactor  110  in not limited to electric heat only. In another example, reactor  110  can be a catalytically-heated reactor. 
     Processing the feedstock (or in-feed) that supplies the inlet of reactor  110  is a scale  116 , a mixer  118 , a feedstock hopper metering stage  120 , one or more in-feed sensors  122 , and an airlock  124 . 
     In energy-conversion system  100 , the feedstock can be, in one example, any biomass (i.e., any organic matter or organic waste that can be used as a fuel), such as, but not limited to, manure, coal, trash, rubber, and plastic. In another example, the feedstock can be mining waste, such as, but not limited to, mine tailings and water-based and/or oil-based drilling mud. However, the system configuration of energy-conversion system  100  is particularly well suited for processing “sticky” feedstock, such as rubber and plastic. At the site of energy-conversion system  100 , the feedstock is typically received at a scale  116  for weighing the bulk feedstock material. The feedstock then enters mixer  118 . Mixer  118  is used to ensure a homogenous mixture of feedstock entering the system. 
     Feedstock hopper metering stage  120  is used for metering the feedstock into reactor  110  at a certain rate. Feedstock hopper metering stage  120  can include, for example, an auger-driven metering mechanism and/or a belt-driven conveyor. Further, feedstock hopper metering stage  120  functions to pre-heat and dry the feedstock. Accordingly, feedstock hopper metering stage  120  includes a dryer mechanism, such as bed dryer that allows conduction drying rather than using convection drying with heated air or a combination of both conduction and convection. Drying is completed in a closed-loop environmentally friendly manner, which dramatically slows the heat dissipation and dramatically improves the energy balance. In feedstock hopper metering stage  120 , waste heat can be captured. Additionally, soluble nutrients can be recaptured with condensing of vapor from the dryer. Further, hot oil from heat recovery can be used to dry the feedstock while metering. 
     Further, feedstock hopper metering stage  120  includes a metered sorbent application that can be used for pre-combustion sequestration of contaminants, such as sulfur, chlorine, and dioxins. The metered sorbent application pre-treats gas while still in the vapor state. Namely, metered sorbents and reagents are added to feedstock prior to or just after the conversion process to sequester contaminates like sulfur and chlorine. Sorbent and reagents can be, for example, finely milled lime, trona, bentonite, sodium bentonite, sodium, and/or sodium bicarbonate, depending on the contaminate. Sorbents and reagents are subjected to minimum heat to promote active bond to contaminants. 
     In-feed sensors  122  are used to automatically control feedstock bed-depth and rate into reactor  110 , which enables an ultra-efficient conversion of the feedstock. In-feed sensors  122  include a positive flow advancement sensor that ensures a scouring effect at the inlet of reactor  110  by the introduction of feedstock at or below reactor level. 
     The outlet of feedstock hopper metering stage  120  supplies an inlet of airlock  124 , which is a passive airlock that is used to remove the air from the feedstock. In airlock  124 , feedstock material is advanced via a conical auger. The conical auger compresses the loose materials into a tube. The compressing action of the conical auger is the mechanism for removing the air from the feedstock material. Namely, the conical auger automatically compresses the loose materials to form about 45 pounds/cubic foot (about 720 kilogram/cubic meter) to about 50 pounds/cubic foot (about 800 kilogram/cubic meter) density plug/airlock, which enables oxygen-free feedstock supply into reactor  110 . The auger automatically creates an airlock plug with advancing material. The outlet of airlock  124  supplies the inlet of reactor  110 . Reactor  110  may have multiple outlets. 
     In energy-conversion system  100 , the dried and air free, or liquid soaked and drained feedstock is then processed through reactor  110 . Namely, shaftless auger  112  is used to advance the feedstock through reactor  110 . Increased heat transfer rates are achieved by the large amount of surface contact created by the increased density of feedstock with liquid increasing the phase-change process to vapor. Feedstock is turned and stirred through reactor  110  to ensure uniform conversion process. Continuous process vapor is mixed throughout the process and equalized prior to reaching the outlets. Feedstock exposure to heat energy is limited to ensure production of a market driven product meeting end users&#39; specifications. Reactor process pressure is less than about 10 inches (about 25.4 cm) of pressure to relieve stress on structural components, reduce constraints on seals, and to ensure that no air can enter reactor  110 . Pressure is maintained within reactor  110  with vapor created in phase change of feedstock and relieved by compensators (e.g., a primary compensator  136  and a secondary compensator  140  as described hereinbelow). By contrast, conventional energy-conversion systems are designed for positive or negative pressure. The regulation of pressure is challenged with clogging at discharge, feedstock input process, and even uniform heat throughout the reactor with utilization of burners, augers, and the inability to create and maintain an airtight environment. The presently disclosed energy-conversion systems can mitigate these drawbacks. 
     The electric multi-zone heater  114  also allows for extremely accurate consistent temperature settings for controlled reaction, thereby eliminating the cyclical nature of overheating and then under heating typically seen on a reactor with the combustion of product. This accuracy and elimination of cyclical heating increases helps ensure products that can meet specifications to allow marketability. 
     Further, in energy-conversion system  100 , the electric generated zoned heat (via multi-zone heater  114 ) supplies the energy required to facilitate the conversion process, which allows for a truly closed-loop system. Namely, as feedstock progresses through reactor  110 , the feedstock changes from a solid to a liquid and then to a vapor. If the feedstock has a quantified BTU per given mass, it can be accounted for in the sum of the gas, liquid, and char fractions. By contrast, conventional energy-conversion systems often utilize a percentage of the feedstock, produced gas, and/or the produced liquid to supply the energy required to advance the conversion process. Further, in energy-conversion system  100 , the amount of total energy generated from the conversion process is far more than the energy consumed by the process. That is, energy-conversion system  100  has a positive energy balance. Namely, in energy-conversion system  100 , any feedstock that is about &gt;3000 BTU/pound (about &gt;6613 BTU/kilogram) dry basis will result in positive net energy. 
     Additionally, reactor  110  has a specified “pathogen and medical residual destruction zone” in which the temperature and duration is controlled and monitored by imbedded electronic sensors (i.e., thermocouples, pressure indicators, and residence time sensors). Information from the sensors can be used to calculate and ensure that the FDA heat exposure standard of 5-logarithmics iterations for “pathogen-free” and “medical residual-free” classifications are achieved, recorded, and stored remotely in triplicate. 
     Energy-conversion system  100  further includes a vapor pre-heating stage  129 , a ceramic hot gas filter  130 , a first quench stage  132 , a pass-through multi-tube plunging condenser  133 , a second quench stage  134 , a primary compensator  136  with an associated primary recirculator  138 , a secondary compensator  140  with an associated secondary recirculator  142 , a vacuum buffer tank  144 , a regulator  146 , a vacuum pump  148 , a syngas buffer tank  150 , and a catalytic scrub  152 . 
     Namely, an outlet of reactor  110  supplies an inlet of vapor pre-heating stage  129 , an outlet of vapor pre-heating stage  129  supplies an inlet of ceramic hot gas filter  130 , an outlet of ceramic hot gas filter  130  supplies an inlet of first quench stage  132 , an outlet of first quench stage  132  supplies an inlet of multi-tube plunging condenser  133 , an outlet of multi-tube plunging condenser  133  supplies an inlet of second quench stage  134 , an outlet of second quench stage  134  supplies an inlet of primary compensator  136 , an outlet of primary compensator  136  supplies an inlet of a primary recirculator  138 , an outlet of a primary recirculator  138  supplies an inlet of secondary compensator  140 , an outlet of secondary compensator  140  supplies an inlet of secondary recirculator  142 , an outlet of secondary recirculator  142  supplies an inlet of vacuum buffer tank  144 , an outlet of vacuum buffer tank  144  supplies an inlet of regulator  146 , an outlet of regulator  146  supplies an inlet of vacuum pump  148 , an outlet of vacuum pump  148  supplies an inlet of syngas buffer tank  150 , and an outlet of syngas buffer tank  150  supplies an inlet of catalytic scrub  152 . 
     Conventional energy-conversion systems operate in heat ranges that cannot isolate the metals, minerals, and nutrients in a reusable format. By contrast, energy-conversion system  100  features commoditized natural resource recovery. Namely, energy-conversion system  100  operates in a heat range that prescriptively chelates or electrostatically bonds the targeted commodities to the carbon matrix created by the conversion process. The resulting char has commercial re-sale value as a soil amendment or and animal feed supplement. For example, energy-conversion system  100  produces a char  160  (discharged at an outlet of reactor  110 ). Generally, any feedstock material that remains solid (i.e., that does not turn to vapor) when processed through reactor  110  is discharged as char  160 . Char  160  can be, for example, a solid carbon char and other nutrients that can be sold to market. For example, char  160  can be sold to market as a soil amendment, or due to its pathogen-free, medical residual-free status, as a high-end animal feed supplement. 
     Vapor that is at a critical heat temperature of, for example, from about 900° F. (about 482° C.) to about 1000° F. (about 538° C.) exits reactor  110  through ceramic hot gas filter  130 . Ceramic hot gas filter  130  is a multi-zone ceramic hot gas filter that provides active vapor filtration to remove any particulate prior to condensing. Ceramic hot gas filter  130  allows systematic pulsing for purging of chars and contaminants. Ceramic hot gas filter  130  uses a supply of producer gas for pulsing. Ceramic hot gas filter  130  provides economic advantages by not supplying inert gas. Pre-heating pulse gas reduces the opportunity for a condensing moment, which would result in tar and/or wax build-up. 
     The outlets of reactor  110  through which the hot vapor exits utilize an automated plunging system  128 . For example, automated plunging system  128  features integrated multi-vapor discharge nozzles, wherein the nozzles may be integrated into filtering (e.g., ceramic hot gas filter  130 ), quenching stages, (e.g., first quench stage  132  and second quench stage  134 ), multi-tube plunging condenser  133 , and any combinations thereof. In reactor  110 , the nozzles are continuously scoured by automated plunging system  128 , which includes a set of continuous “shaft and shell” pneumatic or hydraulic plungers that are used to scour residual char deposit to maintain clear pathways for more efficient vapor discharge and collection. Continuous plunging slows gas velocities and allows suspended particles to drop out of vapor creating a cleaner gas prior to condensation. Reactor  110  features multi-port vapor discharge that is based on automated plunging system  128 . The presence of multi-port plunged vapor outlets ensures vapor discharge at a prescribed maximum velocity. 
     Maintaining a minimum temperature of entire vapor discharge system to the first stage of vapor condensing eliminates the opportunity to form and deposit waxes, tars, and/or acids. Conventional energy-conversion systems rely on vapor to heat the system as the system becomes active. Until the system reaches critical temperature, condensation occurs, thereby allowing deposits and acids to form. Once deposits are formed the system becomes coated, which promotes clogging and adding to system downtime and maintenance. By contrast, in energy-conversion system  100 , vapor pre-heating stage  129  (together with ceramic hot gas filter  130 ) reduces pre-condensing opportunities, minimizes corrosive build-up, reduces tar and wax deposits minimizing clogging opportunities, reduces acidic formation, reduces maintenance expense and downtime, and increases lifespan of capital equipment. Namely, vapor pre-heating stage  129  is used to pre-heat the gas leading into and flowing out of ceramic hot gas filter  130  in order to prevent the gases from condensing and clogging ceramic hot gas filter  130 . Using vapor pre-heating stage  129 , the gas can be heated to from about 450° F. (about 232° C.) to about 500° F. (about 260° C.). In operation, in pre-heating stage  129 , the vapor is heated by heating the components through which the vapor flows. Heating can be performed, for example, using heat trace tubing, hot oil, and/or steam. 
     Quenching of vapor with produced liquid fraction product is accomplished using first quench stage  132  and second quench stage  134 . Quenching promotes the elimination of tars, resins, and waxes (i.e., the heavy tars or oils) in gas fraction, removes particulate for the vapor stream, and allows for collection of specific fraction of condensable liquid. The vapor can be quenched using, for example, mineral oil or any other oil that can be used to absorb the tars, resins, and waxes. In some embodiments, quenching liquid can be filtered into a high temperature fluid bath (HTFB) to recapture nutrient and/or char. Any vapor remaining after processing by first quench stage  132 , multi-tube plunging condenser  133 , and second quench stage  134  is passed to primary compensator  136  with its primary recirculator  138 . Multi-tube plunging condenser  133  is arranged between first quench stage  132  and second quench stage  134 . Current condensing systems experience deposits of waxes, heavy oils, greases and tars. As deposits occur, condensing rate decreases, creating vapor carry over effects, clogging, higher maintenance costs and ultimately increased downtime. Multi-tube plunging condenser  133  mitigates these problems. For example, multi-tube plunging condenser  133  includes an open ended plunged shell and tube heat exchange condenser to eliminate tar, grease, and/or wax build-ups. Supported by automated plunging system  128 . Multi-tube plunging condenser  133  eliminates clogging of waxes, tars and heavy oils; promotes advancement of any condensed liquid; promotes heat transfer from vapor to condensing tubes; and reduces maintenance and down time. 
     In energy-conversion system  100 , there may be a pressure transition component. In particular, the system may include a transition from a positive pressure system to a negative pressure system. For example, reactor  110  through first quench stage  132  and second quench stage  134  is pressurized to about 7 inches (about 17.78 cm) of water column pressure. However, at primary compensator  136  the system begins to transition to a negative pressure system. Accordingly, primary compensator  136  and primary recirculator  138  allow for low-pressure vapor supply to negative pressure vapor removal. Further, primary compensator  136  acts as condenser that: (1) provides first phase tube-to-shell heat exchange, (2) provides second phase direct contact with cooling fluid, (3) provides cooling fluid the same as condensable liquid, (4) provides cooling fluid that creates turbulence with multi-port feed, and (5) allows for specific fraction collection on vapor. In one example, primary compensator  136  includes a tube that is about 53 inches (about 134.6 cm) tall. The amount of pressure can be set by adjusting the height of the tube. In one example, there is about 46 inches (about 116.8 cm) of negative water column pressure at primary compensator  136 . Further, the vapor enters primary compensator  136  and primary recirculator  138  at about 300° F. (about 149° C.) and exits primary compensator  136  and primary recirculator  138  at about 100° F. (about 38° C.) (at about ambient temperature). 
     Secondary compensator  140  with its secondary recirculator  142  allow for increased negative pressure vapor removal. Like primary compensator  136 , secondary compensator  140  acts as condenser that: (1) provides first phase tube-to-shell heat exchange, (2) provides second phase direct contact with cooling fluid, (3) provides fluid the same as condensable liquid, (4) provides cooling fluid that creates turbulence with multi-port feed, and (5) allows for multiple specific fraction collection on vapor. There is a heat exchange in secondary compensator  140  and secondary recirculator  142 . Therefore, vapor enters secondary compensator  140  and secondary recirculator  142  at about 100° F. (about 38° C.) (at about ambient temperature) and exits secondary compensator  140  and secondary recirculator  142  at about 34° F. (about 1.1° C.) or 35° F. (about 1.7° C.). It is important to maintain a temperature above freezing in case there is water present. 
     Accordingly, the primary compensator  136  and the secondary compensator  140  allow a continuous flow transition of the reactor vapor from positive pressure to negative pressure, acting as a system non-clogging or sticking pressure regulator. At the same time, the compensators act as first stage shell and tube heat exchange condenser and then second stage direct liquid contact heat exchange with similar circulated liquid being condensed. Specific temperature of circulating fluid is maintained with heat exchange to promote collection of desired fraction of vapor. Additional fractions and condensing stages can be achieved by placing multiple compensators in line. Additionally, as consecutive compensators are placed in line, vapor will enter the compensator with negative pressure and, as with primary compensator  136 , continuous flow transition will occur but to increased negative pressure while still condensing to desired fraction design temperature. Current systems operate either at positive or negative pressure and do not have the ability to make continuous flow transition. Reactor vapor that has not been condensed to it limits can deposit liquids, tars, and waxes, thereby causing sticking, clogging, and regulator failure. 
     Using primary compensator  136  and primary recirculator  138  and secondary compensator  140  and secondary recirculator  142 , anything that is condensable is condensed so that vapor only moves on to vacuum buffer tank  144 . Namely, vapor from secondary recirculator  142  supplies vacuum buffer tank  144 . Reactor gas processing systems, such as energy-conversion system  100 , are designed for continuous even flow. However, the production of vapor is often irregular and the use of buffering tanks (e.g., vacuum buffer tank  144 ) helps even the vapor flow and balance of the system. 
     Vapor then passes from vacuum buffer tank  144  to vacuum pump  148  via regulator  146 . Regulator  146  is used to precisely control the vacuum level. In vacuum pump  148 , vacuum is generated by a liquid ring compressor. Vacuum pump  148  is used to remove liquid from vapor and to cool gas on the pressure side of the vacuum. In vacuum pump  148 , the fluid is chilled by heat exchange. In one example, vacuum pump  148  is a 15 PSI vacuum pump. In vacuum pump  148 , the utilization of a liquid ring compressor allows the cooling of gas as it is being compressed. Further, in the event that any tars have made it past the condensing process, diesel can be utilized as circulating cooled liquid for maintaining the integrity of the compressor. The liquid ring compressor of vacuum pump  148  requires constant air circulation. Accordingly, the combination of vacuum buffer tank  144  on the upstream side of vacuum pump  148  and the pressurized syngas buffer tank  150  on the downstream side of vacuum pump  148  provides a control loop for balancing the system. 
     In energy-conversion system  100 , filter-less quenching gas cleanup can be performed using a multi-pass catalytic gas polishing system, such as catalytic scrub  152 . For example, catalytic scrub  152  provides a three-pass catalytic scrub operation. Catalytic scrub  152  is used for scrubbing pre-combusted gas, wherein the gas is easier to scrub while still condensed. Catalytic scrub  152  includes a unique vessel (not shown) through which the gas flows. Further, catalytic scrub  152  performs a gas polishing operation that ensures high quality gas in which sulfur, chlorine, and other gas contaminants have been substantially eliminated Catalytic scrub  152  is a gas polishing system that incorporates a unique concept, in that it is designed to pass the gas through a multiple chambered system utilizing catalysis previously used to scrub or clean post combustion or reaction exhaust gases, yet in catalytic scrub  152  pre-combusted gas is scrubbed. By contrast, conventional gas polishing systems typically flow scrubbed exhaust to atmosphere, not requiring an airtight structure. The polished syngas discharged from catalytic scrub  152  can be supplied to an electricity generator, boiler, heater, and the like. Syngas, or synthesis gas, is a fuel gas mixture consisting primarily of hydrogen, carbon, methane, propane, butane, carbon monoxide, and very often some carbon dioxide. 
     Further, in energy-conversion system  100 , the primary compensator  136  and the secondary compensator  140  in combination with the vacuum buffer tank  144 -vacuum pump  148 -syngas buffer tank  150  loop is the mechanism used to control the pressure inside reactor  110 . For example, this control loop can be used to hold the pressure inside reactor  110  at about 7 inches (about 17.78 cm) of water column. 
     Energy-conversion system  100  provides an emission free process. Namely, because of the absence of combustion of one or more of the products there is no requirement for stacks and no emissions created or emitted. In addition to the fact there are no emissions, an additional benefit of energy-conversion system  100  is that no loss of energy to the stack is present. By contrast, in conventional energy-conversion systems, a percentage of the energy is created from the feedstock and/or the products, which creates the requirement for heat exchange. Consequently, capturing 100% of that spent energy is next to impossible, which allows a large percentage of the energy to escape with the emissions up the stack to the environment. 
     Referring now to  FIG.  2    is a block diagram of an energy-conversion system  200  that includes a drag conveyor, according to another embodiment of the presently disclosed electric-powered, electric- or catalytically-heated, closed-loop, continuous-feed, endothermic energy-conversion system. Energy-conversion system  200  is substantially the same as energy-conversion system  100  shown in  FIG.  1    except that the shaftless auger is replaced with a drag conveyor. Further, the quenching portion of energy-conversion system  200  differs from the quenching portion of energy-conversion system  100 . 
     Like energy-conversion system  100  shown in  FIG.  1   , energy-conversion system  200  is a closed-loop system that (1) eliminates substantially all emissions and effluents; (2) recovers substantially all residual carbon, metals, minerals, and nutrients for beneficial reuse; (3) reuses residual/waste heat; and (4) eliminates parasitic loss of potential energy. 
     Energy-conversion system  200  includes controller  105 . Energy-conversion system  200  also includes a reactor  210 , also known as a conversion chamber or conversion reactor. Reactor  210  is an electrically controlled and electrically- or catalytically-heated reactor. Reactor  210  is a channel that is equipped with multi-zoned electric heat (e.g., multi-zone heater  114 ). Namely, reactor  210  is enclosed within multi-zone heater  114 . Further, reactor  210  in not limited to electric heat only. In another example, reactor  210  can be a catalytically-heated reactor. 
     In one example, reactor  210  is a channel that is about 54 inches (about 137.1 cm) wide, about 7 inches (about 17.78 cm) high, and about 75 feet (about 22.8 meters) long making multiple passes. However, reactor  210  can be any dimensions. Namely, the length of reactor  210  may be determined by the amount of residence time needed in the system. Further, reactor  210  can be formed, for example, of carbon steel, stainless steel, or specialized alloys, such as, but not limited to, selected Inconel alloys. The system configuration of energy-conversion system  200  is particularly well suited for processing a homogenous feedstock, such as manure or coal. 
     Further, instead of shaftless auger  112  shown in  FIG.  1   , a drag conveyor  212  is installed in reactor  210  for moving the feedstock. A drag conveyor (aka chain conveyor) is a conveyor in which an endless chain, having wide links carrying projections or wings, is dragged through a trough into which the material to be conveyed is fed. A drag conveyor is generally used for moving loose material. In energy-conversion system  200 , drag conveyor  212  is used to carry feedstock through reactor  210 . In reactor  210 , drag conveyor  212  may be used to: (1) provide a large surface area for maximum thermal conduction (i.e., collectively, the links of the chain provide a large heated surface area), (2) allow for an adjustable bed depth of feedstock, and (3) minimize the drive horsepower requirement for conveyance. Using, for example, manure feedstock in reactor  210 , the feedstock bed depth on drag conveyor  212  for optimal heat transfer (optimal cooking) is from about 4 inches (about 10.16 cm) to about 7 inches (about 17.78 cm) in one example, or is about 4.5 inches (about 11.43 cm) in another example. 
     Drag conveyor  212  may also be used for scouring the inside surfaces with flight design, which: (1) maximizes thermal conduction by minimizing material deposits, and (2) minimizes rotational balling of material. The components of drag conveyor  212  can be formed of specialized alloys, such as, but not limited to, selected Inconel alloys. The use of the specialized alloys (1) prevent galling of similar metals with direct contact, (2) prevent chlorine migration and hydrogen embrittlement, and (3) eliminate differential creep rate by controlling take up of the drag chain conveyor. However, in other embodiments, the components of drag conveyor  212  can be formed of carbon steel or stainless steel. 
     In energy-conversion system  200  and using drag conveyor  212 , feedstock can be conveyed through reactor  210  at high temperature if dissimilar metals are utilized for all contact surfaces including chain pins, links, flights, and sprockets. The thermal creep growth can be addressed using automatic tensioners on one end of drag conveyor  212 . A multi-pass drag chain allows for feedstock advancement in both or opposing directions on the same chain and creates the opportunity for prolonged residence time, rotation, turning, and stirring of feedstock. Certain feedstocks can experience a balling effect when conveyed using an auger, making uniform exposure to heat energy impossible. However, using drag conveyor  212 , the feedstock bed depth can be adjusted to ensure uniform exposure without rotation, thereby eliminating the balling effect. In conventional energy-conversion systems, drag chain conveyors have not been utilized due to galling and system airtight structure limits caused by pressure or vacuum. 
     Energy-conversion system  200  may also include the scale  116 , mixer  118 , feedstock hopper metering stage  120 , in-feed sensors  122 , and airlock  124 , wherein the scale  116 , mixer  118 , feedstock hopper metering stage  120 , in-feed sensors  122 , and airlock  124  are used for processing the feedstock (or in-feed) that supplies the inlet of reactor  210 . The outlet of airlock  124  supplies the inlet of reactor  210 . 
     Also different from energy-conversion system  100 , feedstock hopper metering stage  120  of energy-conversion system  200  features auger-less in-feed metering; namely, a multi-metered, drag conveyor-based in-feed mechanism that includes a dryer. Conventional systems rely on batch feeding or auger-driven in-feeds. Generally, systems are challenged either by inconsistent characteristics of feedstock and/or extremely difficult calculations to maintain an equal and consistent feed rate as moisture, surface tension, density, temperature, and pressure are all variables. A non-consistent feed rate can translate to inefficient, inconsistent, incomplete and/or over exposure to the heating and conversion process of the feedstock. To mitigate these drawbacks, feedstock hopper metering stage  120  of energy-conversion system  200  provides the multi-metered, drag conveyor-based in-feed that creates a uniform feedstock depth and width that maintains a balanced relationship to the heat-source throughout the conveyance process. The feedstock is subjected to metering at the dryer and prior to entering reactor  210  to ensure uniform and predictable bed depth. The customized dryer drag conveyer advances the uniformly shaped feedstock into a hot oil and steric acid mixture or similar oil/acid mixture, high-temperature fluid bath (HTFB)  126  of airlock  124 . Further, the dewatering airtight drag conveyor delivers the feedstock to the drag conveyor  212  in reactor  210 . 
     Rather than using a conical auger, airlock  124  of energy-conversion system  200  includes the steric acid HTFB  126 . Steric acid HTFB  126  can be used to displace air without a vacuum pump or the addition of inert gas. Namely, using steric acid HTFB  126 , the air in the feedstock is displaced with oil. The addition of steric acid to the HTFB accelerates and intensifies the moisture flash-off, which increases the de-polymerization of complex hydrocarbons and minimizes the formation of tars and heavy oils. The hot oil, steric acid mixture HTFB  126  may be used to: (1) increase the density of feedstock without mechanical interaction, (2) create an airlock without need for valves or slide-gates, (3) eliminate any remaining moisture from feedstock, (4) increase the exposed surface area of the feedstock, and (5) maximize the heat transfer rate in reactor  210 . Further, convention airlocks often include a negative-pressure vessel, which is a safety hazard and a historic point of failure. By contrast, hot oil, steric acid mixture HTFB  126  does not require a negative-pressure vessel and therefore the safety hazard and historic point of failure is eliminated. 
     In conventional reactor based conversion systems, feedstock moisture removal has always been a challenge and often the fatal flaw. However, using steric acid HTFB  126 , the “combustion-less flash-off” of all remaining moisture dramatically reduces both the time and the energy required to dry the feedstock, which in-turn dramatically improves the energy balance and the economics. The steric acid also promotes the conversion of problematic tars and waxes into lighter, smaller carbon chains. 
     Airlock  124  eliminates all moving parts as feedstock is subjected to the hot liquid bath (of steric acid HTFB  126 ) displacing all air, flashing off all remaining moisture, and allowing delivery to a dewatering conveyor of feedstock hopper metering stage  120 . Feedstock is advanced past the liquid barrier on the dewatering conveyor, which is an airlock secondary metering device. The passive airlock system of airlock  124  also creates a built-in pressure relief system for reactor  210 . Further, the exhaust heat from the backend electricity generator can be cycled back to feedstock hopper metering stage  120  and/or airlock  124  and used for drying. 
     In summary with respect to feedstock hopper metering stage  120  and airlock  124 , manure feedstock, for example, becomes fluffy and fibrous when dried, and full of air. Air is an insulator and prevents the feedstock from heating. Accordingly, using feedstock hopper metering stage  120  and airlock  124 , (1) the manure feedstock becomes saturated with oil (e.g., mineral oil), which displaces the air and provides a medium that absorbs heat readily; (2) the density of the feedstock material entering reactor  210  is increased; and (3) the manure feedstock that is saturated with oil maximizes the contact ratio to the heating mechanism (e.g., multi-zone heater  114 ) in reactor  210  (i.e., maximizes heat transfer rate between heater and feedstock). A further benefit of having oil in the feedstock is that the latent energy required to drive out oil is about less than 95 BTU/pound. By contrast, the latent energy required to drive out water is much greater at about 950 BTU/pound. 
     Additionally, in energy-conversion system  200 , rather than allowing the gas to exit the reactor to a separate quenching stage as described in  FIG.  1   , a gas collection system is provided at a certain portion along reactor  210 . The gas collection system supplies a multi-zone quench station  214  that is integrated directly into reactor  210 . The presence of multi-zone quench station  214  eliminates the need for automated plunging system  128 . Multi-zone quench station  214  along with a quench oil (Q-oil) filter  216  and an oil preheat stage  218  provides a closed-loop arrangement wherein a quantity of circulating oil  220  is circulated therethrough. Circulating oil  220  can be, for example, mineral oil or diesel fuel. Together, multi-zone quench station  214 , Q-oil filter  216 , oil preheat stage  218 , and circulating oil  220  provide a recirculating filtered hot oil quenching system that is used to remove any particulate prior to condensing. For example, circulating oil  220  is circulated through multi-zone quench station  214 , then through Q-oil filter  216 , then through oil preheat stage  218 , then returning to multi-zone quench station  214 . Q-oil filter  216  is a commercially available continuous self-cleaning hot oil filter. The solids that accumulate in Q-oil filter  216  can be fed back into the feedstock (or in-feed) and processed through reactor  210 . 
     Using multi-zone quench station  214 , hot circulating oil  220  is recirculated back onto the gas in reactor  210  at about 300° F. (about 149° C.), wherein oil preheat stage  218  is used to preheat circulating oil  220  to the critical temperature for quenching, which is typically about 300° F. (about 149° C.). In so doing, the gas is cooled to about 300° F. (about 149° C.). Some portion of the cooled gas condenses and the liquid recirculates. However, the lighter gases above about 300° F. (about 149° C.) that do not condense will pass onto the arrangement of primary compensator  136 , primary recirculator  138 , secondary compensator  140 , secondary recirculator  142 , vacuum buffer tank  144 , regulator  146 , vacuum pump  148 , syngas buffer tank  150 , and catalytic scrub  152  as described with reference to energy-conversion system  100  of  FIG.  1   . Again, reactor  210  will be held at about 7 inches (about 17.78 cm) of water column pressure. Again, in energy-conversion system  200  there is a transition from a positive pressure system to a negative pressure system. Further, char  160  is discharged from one or more outlets of reactor  210 . 
     Referring now to  FIG.  3    is a block diagram of an energy-conversion system  300  that includes a distillation and/or fractionating stage, according to yet another embodiment of the presently disclosed electric-powered, electric- or catalytically-heated, closed-loop, continuous-feed, endothermic energy-conversion system. Energy-conversion system  300  is substantially the same as energy-conversion system  200  of  FIG.  2    except that it additionally includes an atmospheric fractionating unit  230 . Further, crude oil  220  is used for the circulating oil in the multi-zone quench station  214 . 
     In pyrolysis, which is a thermochemical decomposition of organic material at elevated temperatures in the absence of oxygen (or any halogen), there is always the generation of char, liquid, and syngas. However, coal feedstock produces a larger liquid and syngas fraction than, for example, manure feedstock. The liquid fraction is needed to produce, for example, gasoline, diesel, and/or asphalt. Accordingly, energy-conversion system  300  that includes the distillation and/or fractionating stage is particularly well suited for processing coal feedstock. 
     In order to process the liquid fraction, energy-conversion system  300  will typically include optional equipment to dilute the heavier liquids resulting from some feedstocks. Accordingly, energy-conversion system  300  includes the optional atmospheric fractionating unit  230  that further includes a heavy oil fractionation process  232  and a gas-fired or catalytically-heated re-boiler  234 . Further, diesel generated using heavy oil fractionation process  232  is discharged to diesel storage  236 . Likewise, asphalt generated using heavy oil fractionation process  232  is discharged to asphalt storage  238 . 
     Additionally, to support atmospheric fractionating unit  230 , energy-conversion system  300  must provide a supply of additional diluting or cutting oil, such as crude oil  220 . Further, in energy-conversion system  300 , if oil or gasoline is to be generated, the gasoline fraction is processed through the compensators (e.g., primary compensator  136  and secondary compensator  140 ) while the diesel and heavy oils remain in the circulating oil. Additional separation can also occur through atmospheric fractionating unit  230 . Namely, in energy-conversion system  300 , crude oil  220  is used as the circulating oil for multi-zone quench station  214 . In multi-zone quench station  214 , oil preheat stage  218  is used to preheat crude oil  220  to the critical temperature for quenching, which is typically about 300° F. (about 149° C.). In reactor  210 , as quenching occurs, vapor is also created, wherein the lighter gases above about 300° F. (about 149° C.) that do not condense will pass onto primary compensator  136 . Namely, the gasoline and other light fractions are taken out of the crude oil. The gasoline and light fractions to pass through reactor  210  and are passed on to the arrangement of primary compensator  136 , primary recirculator  138 , secondary compensator  140 , secondary recirculator  142 , vacuum buffer tank  144 , regulator  146 , vacuum pump  148 , and syngas buffer tank  150 , which supplies the gas-fired or catalytically-heated re-boiler  234 . In so doing, the gasoline and other light fractions are condensed and discharged to, for example, gasoline storage  240  and other storage  242  (e.g., water storage), wherein the gasoline and other light fractions can be sold. Additionally, if stripping gas is required for fractionating, it can be blended with syngas and utilized in the gas-fired or catalytically-heated re-boiler  234 . 
     In energy-conversion system  300 , a portion (about half) of the crude oil  220  circulating through multi-zone quench station  214  is pulled off downstream of Q-oil filter  216  and supplied to the atmospheric fractionating unit  230  or any typical refining or fractionation system. Heavy oil fractionation process  232  of atmospheric fractionating unit  230  is used to fractionate the oil using the syngas from syngas buffer tank  150  and the gas-fired or catalytically-heated re-boiler  234 . Heavy oil fractionation process  232  is used to break down the crude oil  220  to a diesel fraction and asphalt fraction, wherein the light fractions that typically come off a refinery are recaptured into reactor  210 . This allows the pressure in a fractionation tower to be maintained to the same 7 inches (17.78 cm) of water column pressure that is in reactor  210 . In heavy oil fractionation process  232 , the light fractions are condensed and scrubbed. The gas, after it has been scrubbed, can be utilized in heavy oil fractionation process  232  as gas energy that is needed to reheat the heavy oil fraction. Namely, heating to about 700° F. (about 371° C.), which allows separation into diesel and asphalt fractions. 
     Typical large-scale refineries operate under high temperatures and very high pressure (many times atmospheric pressure) in the fractionation process. As a result, large-scale refineries include high temperature processes and ultra-high pressure vessels that are highly regulated. By contrast, a main benefit of energy-conversion system  300  is that atmospheric fractionating unit  230  operates at low temperature and at atmospheric pressure, wherein any vessels are not highly pressurized and therefore are not typically subject to regulatory compliance. Namely, atmospheric fractionating unit  230  is called “atmospheric” because it operates at or below atmospheric pressure, not at high pressure or ultra-high pressure. 
     Further, in a gas-fired re-boiler much of the heat and most of the pollutants are lost up the stack. However, with respect to processing the gas through a catalytically-heated re-boiler (e.g., catalytically-heated re-boiler  234 ), the primary byproducts are carbon dioxide (CO 2 ) and water (H 2 O), which can be recaptured and thereby eliminating the requirement for a stack. The dioxide (CO 2 ) and water (H 2 O) can be easily re-purposed for hydroponics, aquaculture, green houses, algae beds, and similar sustainable food initiatives. In aggregate, the environmental efficiency (decreased pollution/increased recycling) of the catalytic conversion system is far superior to that of the gas-fired alternative 
     In summary, energy-conversion system  300  provides a process of commoditized natural resource recovery and refining. Namely, the un-gasified feedstock residual will consist of both a liquid fraction and a solid carbon char. The liquid fraction will resemble crude oil, which can be further refined into gasoline, diesel fuel, or naphtha based on end-user specification. The solids fraction will be a carbon char that can prescriptively bond to and/or chelate any commoditized natural resources present in the feedstock, such as nitrogen, phosphorus, zinc, manganese, magnesium. The resulting char can then be re-formatted for beneficial reuse as a soil amendment, or due to its pathogen-free, medical residual-free status, as a high-end animal feed supplement. Further, energy-conversion system  300  features integration of selective fractional condensing. Namely, through a series of quenchings with a proprietary combination of circulating fluids, and the utilization of compensators at critical temperatures ranges, the liquid fraction of the processed feedstock can yield fractionated products including, but not limited to, gasoline, diesel, heavy fuel oil, asphaltenes, and lubricants which can be stored on-site in tanks or transported off-site by truck, rail, or pipeline. 
       FIG.  4    through  FIG.  25    show various views of one example instantiation of the shaftless auger-based energy-conversion system  100  shown in  FIG.  1   . Namely,  FIG.  4   ,  FIG.  5   , and  FIG.  6    show an isometric view, a side view, and a top down view, respectively, of energy-conversion system  100  in its entirety.  FIG.  7    through  FIG.  25    show various portions of the shaftless auger-based energy-conversion system  100  shown in  FIG.  1   . For example,  FIG.  7    shows an isometric view and  FIG.  8    shows a front view and a top down view of the reactor  110  and multi-zone heater  114  portion of energy-conversion system  100 .  FIG.  9    and  FIG.  10    show various cross-sectional views of the reactor  110  and multi-zone heater  114 -portion of energy-conversion system  100  and now showing shaftless auger  112 .  FIG.  11    shows an isometric view and  FIG.  12    shows a front view and a top down view of the reactor  110 -portion of energy-conversion system  100 .  FIG.  13    and  FIG.  14    show cross-sectional views of the reactor  110 -portion of energy-conversion system  100  and now showing shaftless auger  112 .  FIG.  15    shows an isometric view and an end view of the multi-zone heater  114 -portion of energy-conversion system  100 .  FIG.  16    shows a front view and a top down view of the multi-zone heater  114 -portion of energy-conversion system  100 . 
       FIG.  17    shows an isometric view, a front view, and a side view of the primary compensator  136 -portion of energy-conversion system  100 .  FIG.  18    shows an isometric view,  FIG.  19    shows a top down view, and  FIG.  20    shows a front view and a side view of the ceramic hot gas filter  130 -portion of energy-conversion system  100 .  FIG.  21    shows an isometric view, a front view, and a side view of the primary recirculator  138 -portion of energy-conversion system  100 . 
     The multi-tube plunging condenser  133  of energy-conversion system  100  includes a condenser portion and a hydraulic or pneumatic plunging portion. For example,  FIG.  22    shows an isometric view and  FIG.  23    shows a side view and a cross-sectional view of a condensing unit  133 ′ of multi-tube plunging condenser  133 , while  FIG.  24    and  FIG.  25    show an isometric view and an end view, respectively, of a hydraulic or pneumatic plunging unit  133 ″ (e.g., hydraulic cylinders) of multi-tube plunging condenser  133 . Condensing unit  133 ′ and hydraulic or pneumatic plunging unit  133 ″ are arranged end-to-end to form multi-tube plunging condenser  133  (see  FIG.  4   ,  FIG.  5   , and  FIG.  6   ). 
     Referring now to  FIG.  26    is a flow diagram of a method  400 , which is an example of a method of operation of energy-conversion system  100  that includes shaftless auger  112  installed in reactor  110 . Method  400  may include, but is not limited to, the following steps. 
     At a step  410 , an energy-conversion system is provided that includes a shaftless auger. For example, energy-conversion system  100  is provided that includes shaftless auger  112  installed in reactor  110  and all heated using multi-zone heater  114 . 
     At a step  415 , feedstock material is supplied to energy-conversion system  100 . For example, feedstock material, such as, but not limited to, any biomass (e g, manure, coal, trash, rubber, and plastic), mining waste (e.g., mine tailings and water-based and/or oil-based drilling mud), and “sticky” feedstock (e.g., rubber and plastic), can be received and weighed at scale  116  and then fed into mixer  118  that ensures a homogenous mixture. 
     At a step  420 , the feedstock material is processed and then supplied to the inlet of the reactor. For example, the feedstock material is fed into feedstock hopper metering stage  120  for metering the feedstock into reactor  110  at a certain rate. Namely, feedstock hopper metering stage  120  is used to pre-heat and dry the feedstock. Further, in-feed sensors  122  are used to automatically control feedstock bed-depth and rate into reactor  110 . Feedstock hopper metering stage  120  supplies the feedstock to airlock  124  that is used to compress the feedstock material (i.e., remove the air from the feedstock). 
     At a step  425 , the feedstock material is advanced through the reactor while the reactor facilitates a phase-change process of the feedstock from solid to liquid to vapor. For example, using shaftless auger  112 , feedstock is advanced and processed through reactor  110 , wherein reactor  110  facilitates the phase-change process of the feedstock from solid to liquid to vapor. Namely, multi-zone heater  114  is activated and used to maintain accurate and consistent temperature within reactor  110 . Increased heat transfer rates are achieved by the large amount of surface contact created by the increased density of feedstock with liquid increasing the phase-change process to vapor. Continuous process vapor is mixed throughout the process and equalized prior to reaching the outlets. Pressure is maintained within reactor  110  with vapor created in phase change of the feedstock. 
     At a step  430 , both char and vapor are discharged from respective outlets of the reactor. For example, char  160  is one output of reactor  110  of energy-conversion system  100  while vapor is another output of output of reactor  110  that is further processed. 
     At a step  435 , particulates are removed from the vapor discharged from the reactor. For example, vapor that is at a critical heat temperature of, for example, from about 900° F. (about 482° C.) to about 1000° F. (about 538° C.) exits reactor  110  through ceramic hot gas filter  130 , wherein ceramic hot gas filter  130  provides active vapor filtration to remove any particulate prior to condensing. 
     At a step  440 , vapor quenching operations are performed wherein mechanisms are provided for preventing tar, grease, and/or wax build-ups. For example, quenching of vapor with produced liquid fraction product is accomplished using first quench stage  132  and second quench stage  134 . Quenching promotes the elimination of tars, resins, and waxes (i.e., the heavy tars or oils) in gas fraction, removes particulate for the vapor stream, and allows for collection of specific fraction of condensable liquid. The vapor can be quenched using, for example, mineral oil or any other oil that can be used to absorb the tars, resins, and waxes. 
     At a step  445 , after quenching, energy-conversion system  100  transitions from a positive pressure system to a negative pressure system. For example, after quenching, primary compensator  136  and secondary compensator  140  allow a continuous flow transition of the reactor vapor from positive pressure to negative pressure, acting as a system non-clogging or sticking pressure regulator. 
     At a step  450 , the vapor is supplied to the vacuum buffer tank. For example, using primary compensator  136  and primary recirculator  138  followed by secondary compensator  140  and secondary recirculator  142 , anything that is condensable is condensed so that vapor only moves on to vacuum buffer tank  144 . 
     At a step  455 , liquid is removed from the vapor and the vapor is cooled. For example, vapor passes from vacuum buffer tank  144  to vacuum pump  148  via regulator  146 . Then, vacuum pump  148  is used to remove liquid from vapor and to cool gas on the pressure side of the vacuum. In vacuum pump  148 , the fluid is chilled by heat exchange. 
     At a step  460 , a filter-less quenching gas cleanup operation is performed and gas is discharged. For example, vacuum pump  148  supplies syngas buffer tank  150  which then supplies catalytic scrub  152 . Catalytic scrub  152  performs a gas polishing operation that ensures high quality gas in which sulfur, chlorine, and other gas contaminants have been substantially eliminated. In this way, energy-conversion system  100  is used to produce high quality syngas, or synthesis gas, which is a fuel gas mixture consisting primarily of hydrogen, carbon, methane, propane, butane, carbon monoxide, and very often some carbon dioxide. 
     At a step  465 , throughout all of the operations of method  400 , energy-conversion system  100  is continuously balanced. For example, the combination of vacuum buffer tank  144  on the upstream side of vacuum pump  148  and the pressurized syngas buffer tank  150  on the downstream side of vacuum pump  148  provides a control loop for balancing the system. In another mechanism, primary compensator  136  and secondary compensator  140  in combination with the vacuum buffer tank  144 -vacuum pump  148 -syngas buffer tank  150  loop is the mechanism used to control the pressure inside reactor  110 . For example, this control loop can be used to hold the pressure inside reactor  110  at about 7 inches (about 17.78 cm) of water column. 
       FIG.  27    through  FIG.  56    show various views of one example instantiation of the drag conveyor-based energy-conversion system  200  shown in  FIG.  2   . Namely,  FIG.  27   ,  FIG.  28   ,  FIG.  29   , and  FIG.  30    show an isometric view, a top down view, a side view, and an end view, respectively, of energy-conversion system  200  in its entirety.  FIG.  31   ,  FIG.  32   ,  FIG.  33   , and  FIG.  34    show the same views of energy-conversion system  200  as shown in  FIG.  27   ,  FIG.  28   ,  FIG.  29   , and  FIG.  30   , respectively, but simplified. 
     In energy-conversion system  200 , feedstock hopper metering stage  120  includes a dryer and a drag conveyor, as shown in  FIG.  35    through  FIG.  39   . Namely,  FIG.  35   ,  FIG.  36   , and  FIG.  37    show an isometric view, a side view, and a top down view, respectively, of the feedstock hopper metering stage  120 -potion of energy-conversion system  200 .  FIG.  38    and  FIG.  39    show cross-sectional views of the feedstock hopper metering stage  120 -potion of energy-conversion system  200  and now showing a drag conveyor  206  enclosed therein. 
       FIG.  40   ,  FIG.  41   , and  FIG.  42    show an isometric view, a side view, and a top down view of the airlock  124 -potion of energy-conversion system  200 .  FIG.  43    and  FIG.  44    show cross-sectional views of the airlock  124 -potion of energy-conversion system  200  and now showing a drag conveyor  208  enclosed therein. 
       FIG.  45   ,  FIG.  46   , and  FIG.  47    show an isometric view, a side view, and a top view, respectively, of multi-zone heater  114  of energy-conversion system  200 , wherein reactor  210  (not visible) is enclosed within multi-zone heater  114 . Further,  FIG.  48    and  FIG.  49    show cross-sectional views of multi-zone heater  114  and showing reactor  210 , wherein drag conveyor  212  is arranged within reactor  210 . Additionally,  FIG.  50   ,  FIG.  51   , and  FIG.  52    show close-up cross-section views of a portion of multi-zone heater  114  and showing more details of reactor  210  and drag conveyor  212 . Further,  FIG.  53    shows an isometric view and  FIG.  54    shows a side view and a top down view of reactor  210  absent multi-zone heater  114 . Similarly,  FIG.  55    and  FIG.  56    show cross-sectional views of reactor  210  and drag conveyor  212  absent multi-zone heater  114 . 
     Following long-standing patent law convention, the terms “a,” “an,” and “the” refer to “one or more” when used in this application, including the claims. Thus, for example, reference to “a subject” includes a plurality of subjects, unless the context clearly is to the contrary (e.g., a plurality of subjects), and so forth. 
     Throughout this specification and the claims, the terms “comprise,” “comprises,” and “comprising” are used in a non-exclusive sense, except where the context requires otherwise. Likewise, the term “include” and its grammatical variants are intended to be non-limiting, such that recitation of items in a list is not to the exclusion of other like items that can be substituted or added to the listed items. 
     For the purposes of this specification and appended claims, unless otherwise indicated, all numbers expressing amounts, sizes, dimensions, proportions, shapes, formulations, parameters, percentages, quantities, characteristics, and other numerical values used in the specification and claims, are to be understood as being modified in all instances by the term “about” even though the term “about” may not expressly appear with the value, amount or range. Accordingly, unless indicated to the contrary, the numerical parameters set forth in the following specification and attached claims are not and need not be exact, but may be approximate and/or larger or smaller as desired, reflecting tolerances, conversion factors, rounding off, measurement error and the like, and other factors known to those of skill in the art depending on the desired properties sought to be obtained by the presently disclosed subject matter. For example, the term “about,” when referring to a value can be meant to encompass variations of, in some embodiments, ±100% in some embodiments ±50%, in some embodiments ±20%, in some embodiments ±10%, in some embodiments ±5%, in some embodiments ±1%, in some embodiments ±0.5%, and in some embodiments ±0.1% from the specified amount, as such variations are appropriate to perform the disclosed methods or employ the disclosed compositions. 
     Further, the term “about” when used in connection with one or more numbers or numerical ranges, should be understood to refer to all such numbers, including all numbers in a range and modifies that range by extending the boundaries above and below the numerical values set forth. The recitation of numerical ranges by endpoints includes all numbers, e.g., whole integers, including fractions thereof, subsumed within that range (for example, the recitation of 1 to 5 includes 1, 2, 3, 4, and 5, as well as fractions thereof, e.g., 1.5, 2.25, 3.75, 4.1, and the like) and any range within that range. 
     Although the foregoing subject matter has been described in some detail by way of illustration and example for purposes of clarity of understanding, it will be understood by those skilled in the art that certain changes and modifications can be practiced within the scope of the invention.