THERMAL CONVERSION PYROLYSIS REACTOR SYSTEM

Abstract: A thermal conversion pyrolysis reactor system (10) is provided for use in providing a continuous flow type pyrolysis reaction for conversion of carbonizable input materials (12). The reactor system (10) utilizes a diffusion material (14) which is preheated and admixed with the input material (12) in order to facilitate pyrolysis and to partially catalyze reactions. Subsystems are provided to receive gaseous (30), liquid (32) and solid (34) outputs, the system (10) is particularly adapted for use with tire chips, medical waste and industrial plastic waste input materials. Carbon black and pelletized metallic and alloy materials are preferred diffusion materials (14).

Description: THERMAL CONVERSION PYROLYSIS REACTOR SYSTEM ' TECHNICAL FIELD The present invention relates generally to material reaction systems, and more particularly to thermal conversion pyrolysis reactors adapted to convert carbonizable materials into gas, liquid and solid residue. The preferred embodiment of the present invention is a thermal conversion pyrolysis reactor system especially adapted for decomposing carbon based materials in an oxygen free reactor environment. The invention is intended for use particularly with respect to pyrolysis of vehicle tires, industrial plastic waste and residential and hospital trash. This is a continuation-in-part of copending application, serial No. 07/863,747, filed by the inventors on 6 April ;i992. DESCRIPTION OF THE PRIOR ART Pyrolysis is the term utilized to described the process by which carbonizable materials are converted to solid, gas and liquid residues, without combustion or oxidization. Pyrolysis processes are utilized in order to obtain usable component materials from waste products while avoiding production of unnecessary oxygen compounds and polluting materials. Pyrolysis processes generally involve the pyrolytic conversion of carbon containing materials to hydrocarbon products. In order to avoid the introduction of unnecessar oxygen into their reaction process, leading to undesirable b products and side effects, it is important that the inpu feed system for the waste materials be structured so as t minimize the access of oxygen or ambient air. Several prio art patents have indicated mechanisms of preventing exces oxygen input. These have included such devices as air lock or other systems. One of these, U.S. Patent No. 4,235,676, issued to Chambers , shows an inert gases purge operatio which is utilized to continually remove the oxygen from th input to the pyrolysis chamber. However, the use of an inpu gas purge operation, even utilizing inert gases, decreases the heating value of f the hydrocarbon gases from the pyrolysis process and can also lead to difficulties in the handling of fugitive vapors from the reaction region. In order to provide a pleasant working environment for the personnel in the vicinity of the reactor, it is important to pay attention to restraining the fugitive vapors which may escape from the input portion of the system. Another area of technology in which attempts have been made to increase the efficiency of pyrolysis processes is in the area of development of high efficiency heat transfer processes to decompose the carbonizable materials. Some of these attempts have been indirect heat transfer processes such as the fluid bed apparatus described in U.S. Patent No. 4,210,491, issued to Sharmen ; the rotary drum mechanism of Jelinek, U.S. Patent No. 4,840,129 and the ChamJbers structure described above, which includes a furnace bed having a hollow shaft containing exhaust circulation to improve heat transfer processes. The same principle, in an inverse application, is illustrated in U.S. Patent No. 4,686,008, issued to Gibson . In this application the inner cylinder contains the heated exhaust gases and the outer chamber has the carbonizable materials, typically tire chips. It is a principle of thermodynamics that the heat transfer characteristics will decrease as the ratio of volume to surface area being heated is increased. Therefore, larger scale reactors according to the prior art structures are less efficient since a smaller component of the reaction material is receiving the heat transfer through the surface. Especially when the reaction material is a poor conductor of heat such as vehicle tire chips, heat transferred to the interior of the reaction shaft is unacceptably inefficient. Since indirect heat transfer processes have been found to provide only limited heat contact surfaces and not entirely successful results, attempts have also been focused on direct heat transfer processes. Some of these are shown in U.S. Patent No. 4,839,151, issued to Apffel , U.S. Patent No. 5,085,738, issued to Harris et al . and U.S. Patent No. 1 4,038,100, issued to Haberman . These prior art processes have 2 utilized teachings such as the use of superheated steam, 3 thermal radiation and direct microwave heating to transfer 4 heat to the tire materials in order to improve the pyrolysis 5 yield. Other techniques, such as immersion in a liquid metal 6 bath, have also been utilized but have been found to be 7 unacceptable due to undesirable byproducts. Direct 8 circulation of ceramic materials has also been utilized. Even 9 in these sorts of processes, however, possible reaction 10 between the waste material (which may include a very wide 11 variety of components) and the ceramic can be a problem. 12 The prior art has also addressed problems such as 13 clogging of the mechanisms and passages by carbonizable waste 14 materials during the pyrolysis process. U.S. Patent No. 15 4,412,889, issued to Oeck , shows applying a fluid cooling 16 jacket surrounding the inlet conduit in order to maintain the 17 input material at a temperature which allows it to be carried 18 through the conduit without clogging. This requires 19 additional heat input later in order to achieve pyrolysis. 20 Special conduit cleaning structures are also disclosed. Th 21 structures, while desirable in certain circumstances, ca 22 increase the complexity of the system and have 23 corresponding decrease in reliability. 24 Various prior art patents have also addressed th 25 nature and quality of the hydrocarbon products which ar 26 generated as a result of the pyrolysis process. To the exten 27 that the liquid phase output includes viscous oils and tar 28 and also to the extent that such may be part of the soli 29 phase output of the pyrolysis process, extra steps ar 30 required in processing in order to produce more usabl 31 materials. Prior art methods such as those disclosed in U.S 32 Patent No. 4,865,625, issued Mudge et al . , wherein "33 gasification process is utilized to catalytically destruc 34 the viscous tars and oils into gases, and U.S. Patent No '35 4,251,500, issued to Morita et al . , with a hydrocrackin 36 process for waste rubber with specific catalyst powders, hav 37 been shown. These processes introduce a level of complexit 38 which would be desirably avoided by minimizing the generatio of the undesirable viscous oils and tars in the original process. Some types of waste input materials, such as hospital waste, may contain certain drug residues or other unstable hazardous chemical compound. In many instances, these undesirable chemical compounds need to be incinerated in a controlled hazardous waste incineration process, since conventional pyrolysis tends to vaporize the compounds with potentially undesirable releases to the atmosphere. In order to deal effectively with this sort of waste product, the pyrolysis process must be modified in order to stabilize or detoxify the undesirable compounds. It has been shown in the prior art, such as U.S. Patent No. 4,122,036, issued to Lewis , that a pyrolysis process for transforming sewage sludge into activated carbon, with the activated carbon mixed with the sludge to continue the pyrolysis process, can be effective. Further, U.S. Patent No. 4,268,275, issued to Chittick , further shows pyrolysis reactions for converting organic material into carbon monoxide, hydrogen, water vapor and other oils and tars. When extra water is supplied into the pyrolysis process, the water vapor is further reacted with charcoal to produced carbon and hydrogen at substantially high temperatures. However, none of the art shown discusses thermal conversion to stabilize or detoxify the heated materials. None of the prior art processes and apparatus have successfully optimized the treatment of carbonizable waste input materials. Special structures have been proposed and constructed to deal with specific problems associated with input materials such as tire chips and hospital waste, but no single overall process has been successful in dealing with a very wide variety of waste input materials in an efficient manner. For this reason, there remains substantial room for improvement in the field. //// //// //// //// 1 BRIEF DESCRIPTION OF THE INVENTION 2 3 Accordingly, it is an object of the present invention 4 to provide an improved thermal conversion pyrolysis reactor 5 system which may be efficiently utilized with a wide variety 6 of carbonizable waste input materials. 7 It is another object of the preferred embodiment to 8 provide a pyrolysis reactor system in which the input feeding 9 operation is efficient, reliable and trouble free, while also 10 providing for removal of oxygen containing gases and fugitive 11 vapors. 12 It is a further object of the present invention to 13 provide a pyrolysis reaction system utilizing an efficient 14 diffusion material to provide maximum direct heat transfer t 15 the waste input material. 16 It is another object of the invention to provide 17 pyrolysis reactor system in which the diffusion material i 18 efficiently preheated in order to avoid undue energy los 19 from the system. 20 It is still another object of the present invention t 21 provide a material flowpath through a pyrolysis reacto 22 system which is resistant to clogging and is, to a degree, 23 self-cleaning. 24 It is yet another object of the present invention t 25 provide a pyrolysis system in which input waste material i 26 the form of shredded tire materials may be converted int 27 usable components, primarily hydrocarbon gases and lo 28 viscosity oils. 29 It is an additional object of the present invention t 30 provide chemical stabilization and detoxification o 31 hazardous chemical and drug waste materials during pyrolysis 32 Still another object of the present invention is t '33 provide a process in which diffusion material may b 34 recovered and re-used, and additional diffusion material ma '35 be produced as a result of the process. 36 Briefly, a preferred embodiment of the presen 37 invention is a thermal conversion pyrolysis reactor syste 38 which is adapted for the treatment of input carbonizabl waste materials ("Mass, Waste", or "MW") . The pyrolysis reactor system utilizes a substantially oxygen-free reaction environment to produce gaseous phase, liquid phase and solid phase output products from the waste input materials. A preheated diffusion material ("Mass, Diffusion" or "MD") , preferably in the form of carbon black, is introduced into the waste input stream in order to provide direct heat diffusion and, to a degree, catalytic conversion of the waste input materials into the desirable output materials. The preferred embodiment utilizes a waste input subsystem, a pyrolysis chamber subsystem, a diffusing material input subsystem, a heating subsystem and various output subsystems associated with gaseous, liquid and solid output materials. Each of the component subsystems of the pyrolysis reactor system is constructed in accordance with specific principles in order to achieve maximum efficiency and minimum complexity. An advantage of the present invention is that the waste input subsystem and diffusion material input subsystem each utilize a three gate arrangement with vacuum operation in order to remove oxygen and fugitive vapors efficiently, avoiding contamination of the pyrolysis reactor chamber. Another advantage of the present invention is that it utilizes a diffusion material to provide direct heat transfer to the waste materials, with the diffusion material selected to be corrosion resistant and to have good heat transfer properties. A further advantage of the present invention is that the diffusion materials are preheated utilizing exhaust heat from the reaction chambers so as to minimize energy loss and maximize recycling efficiency. Another advantage of the present invention is that the direct mixing of the diffusing material with the waste input material allows maximum direct heat transfer by conduction and increases overall heat transfer efficiency. Still another advantage of the present invention is that the material transport mechanisms prevent clogging and introduces a degree of self-cleaning into the system without 1 introducing cooling fluid or other structures which decrease 2 overall heat transfer efficiency. 3 A further advantage of the present invention is that 4 the use of thermally conducting diffusing materials results 5 in an improved quality of oils generated from hydrocarbon 6 based materials such as vehicle tire chips. 7 A still further advantage of the present invention is 8 that the use of carbon black as a diffusing material can 9 result in undesirable chemical compounds in the waste input 0 material reacting with the carbon black, or being catalyzed 1 thereby to react to form chemical compounds which do not 2 share the undesirable characteristics of the original 3 materials. 4 Yet another advantage of the present invention is that 5 the diffusion material is non-corrosive and corrosion 6 resistant and may be recovered, at least in part, from the 7 solid phase output of the reactor system in order to be 8 recycled for reuse. 9 Still another advantage of the present invention is 0 that it may be operated continuously with minimal necessity 1 for cleaning of the chamber or the transport path, and may 2 thus be operated with a minimal amount of down time. 23 A further advantage of the inventive system is that a 24 portion of the reaction products may be in the form of 25 combustible materials which may be recycled as burner fuel, 26 making the system substantially self-powered. 27 These and other objects and advantages of the present 28 invention will become clear to those skilled in the art upon 29 review of the following specification, the accompanyin 30 drawings and the appended claims. 31 32 BRIEF DESCRIPTION OF THE DRAWINGS "33 34 Fig. 1 is an overall diagrammatical view of a therma 35 conversion pyrolysis reactor system according to the presen 36 invention; 37 Fig. 2 is a diagrammatical view of the waste inpu 38 subsystem portion of the overall reactor system; Fig. 3 is a diagrammatical view of the pyrolysis reactor chamber subsystem of the present invention showing an alternative embodiment utilizing a preheating exhaust gas conduit convolution; and Fig. 4 is a diagrammatical view of the diffusion material input subsystem and the solid and liquid waste output subsystems according to the present invention. BEST MODE FOR CARRYING OUT THE INVENTION The best presently known mode for carrying out the invention is a thermal conversion pyrolysis reactor system which is adapted for use in pyrolyzing carbonizable waste materials into usable components. The reactor system is a flow process reactor which is adapted to be used in a commercial or municipal operation and with a wide variety of potential waste inputs. A preferred embodiment of the thermal conversion pyrolysis reactor system is illustrated in a schematic diagram in Fig. 1 and is referred to by the general reference character 10. In this illustration it may be seen that the pyrolysis reactor system 10 is adapted to receive input in two distinct forms, these being a waste input 12 ("MW") which is a carbonizable material such as tire chips, plastic bottles, hospital waste or the like, and a diffusion material input 14 ("MD") . The diffusion material 14 is a good heat retaining and conducting substance which is caused to mix with the waste input material 12 during the pyrolysis reaction in order to maximize the efficiency thereof. The pyrolysis reactor system 10 is adapted to convert the waste input material 12 into a gaseous phase output 16, a liquid phase output 18 (nonexistent or in significant in some situations) and a solid phase output 20. The thermal conversion pyrolysis reactor system 10 is adapted and constructed to be operated such that the various outputs are in the form of usable materials which require minimal additional processing, as opposed to many existing systems which create unacceptable pollutants and/or unduly complex 1 output materials. 2 The thermal conversion pyrolysis reactor system 10 may 3 be considered to be a combination of a variety of co- 4 operating subsystems. In the preferred embodiment 10, these 5 subsystems include a waste input subsystem 22, a pyrolysis 6 chamber subsystem 24, a diffusion material input subsystem 7 26, a heating subsystem 28 and gaseous output subsystem 30, a 8 liquid output subsystem 32 and a solid output subsystem 34. 9 The various subsystems overlap to a certain degree and 0 operate in conjunction to achieve the efficient overall 11 continuous flow pyrolysis reaction. 12 As is illustrated in Fig. 1, and in more detail in Fig. 13 2, the waste input subsystem 22 is adapted to efficiently 14 input the waste material MW 12 into the pyrolysis chamber 15 subsystem 24. The waste input subsystem 22 may be seen to 16 include a MW input hopper 36 in the general form of a funnel 17 into which the carbonizable waste material 12 is delivered. 18 Ordinarily, the MW 12 will be processed prior to input into 19 the MW hopper 36 so that it is at least a marginally flowable 20 material. That is, in the example of vehicle tires, these 21 will be cut or ground into small chunks or chips (i.e. 5 c 22 diameter or less) so that they may be delivered through pipe 23 and conduits and will not cause undue hangups in the wast 24 input subsystem 22. 25 The MW input hopper 36 is located at the top of th 26 waste input subsystem 22 to allow gravitational flow rf th 27 carbonizable waste material 12. The output of the MW inpu 28 hopper 36 is into a waste conduit 38 which extends verticall 29 downward. The waste conduit 38 represents an MW flow path 30 which includes, in vertical order, an MW slide gate 40, 31 first MW flat gate 42, an MW vacuum chamber 44, and a secon 32 MW flat gate 46. The MW slide gate 40, the first MW flat gat •33 42, and the second MW flat gate 46 control the flow of soli 34 materials through the waste conduit 38. The opening an *35 closing of the various gates is accomplished by an MW gat 36 operating mechanism 48. The gate operating mechanism 48 i 37 not shown in detail and may be any of a variety o 38 constructions. It is expected that the gate operatin mechanism 48 will be electrical, hydraulic or pneumatic. The gate operating mechanism 48 will be timed and programed to operate in sequential ordor. It .is expected that the preferred mechanism will be pneumatic because this allows for rapid and powerful opening and closing of the gates. The MW vacuum chamber 44 is connected via an MW vacuum p pe 50 to a blower/pump 52 (see Fig. 1) which also forms a portion of the heater subsystem 28. The blower/pump 52 creates a negative pressure within the vacuum pipe 50 and accordingly creates a negative pressure in the vacuum chamber 44. The advantage of utilizing vacuum to partially evacuate gaseous materials from the waste input material 12 and the waste conduit 38 is that it minimizes undesirable oxygen entering the pyrolysis chamber subsystem 24 and also captures and recycles fugitive hydrocarbon vapors which may escape from the pyrolysis chamber subsystem 24 through the waste input subsystem 22. An MW screen filter 54 (ordinarily a screen lining the interior of the vacuum chamber or a substantial portion thereof to minimize clogging effects) is provided within the vacuum chamber 44 about the interface with the MW vacuum pipe 50. The screen filter 54 prevents solid waste materials from clogging the vacuum pipe 50. An MW vacuum control valve 56 is provided in the vacuum pipe 50 intermediate the vacuum chamber 44 and the blower/pump 52. The vacuum control valve allows air to be drawn into the blower/pump 52 through an MW bypass 58, even when the vacuum chamber 44 has already been evacuated and the gates are closed. This permits continuous operation of the blower/pump 52. The sequential passage of a defined clump of MW 12 through the waste input subsystem is as follows. The carbonizable waste material 12 is deposited in the input hopper 36. The slide gate 40 is utilized to control the flow rate of the infeed material 12 into the waste conduit 38. The slide gate 40 is also a high strength structure which is designed to withstand the weight of the accumulated MW 12 in the hopper 36. When the slide gate 40 is opened the lowermost amount of the MW 12 will drop through the waste conduit 38 1 and be retained against the first flat gate 42. The slide 2 gate 40 will then close, essentially acting as an air lock. 3 It is understood the system is not intended to be strictly 4 airtight but that the sealing is of sufficient viability to 5 minimize the input of undesirable gaseous materials into the 6 pyrolysis chamber subsystem 24. 7 In actual construction, the "gates" are likely to be 8 specific components which include passages which form the 9 waste conduit 38 and the actual gate mechanisms. A series of 10 these conventional components can be connected together. 11 These are constructed to be reasonably airtight, except if 12 material gets jammed, so will often include some mechanism to 13 clear the closure position as well. The exact nature of the 14 gates is also primarily a matter of design choice. 15 Once the effective seal has been established by closin 16 the slide gate 40, the first flat gate 42 is opened such tha 17 the MW 12 drops into the vacuum cha'nber 44 (on the top of th 18 second slide gate 46) . At this point, the vacuum contro 19 valve 56 operates automatically in order to evacuate th 20 vacuum chamber 44 of gaseous materials by drawing the gase 21 outward through the vacuum pipe 50. The second flat gate 4 22 is closed during this process to prevent drawing vapors fro 23 the chamber subasse bly 24, except as such are alread 24 present from previous openings of the second flat gate 46 25 Ordinarily ten seconds is a sufficient evacuation interval 26 Subsequent to evacuation, the second flat gate 46 is opene 27 to drop the MW 12 from the vacuum chamber 44 downward throug 28 the waste conduit 38 and into the reactor input 60, where i 29 interfaces with the pyrolysis chamber subsystem 24 30 Simultaneously, fugitive gases from the chamber subsystem 2 31 will escape into the vacuum chamber 44 while the second fla 32 gate 46 is open, and will be evacuated by the vacuu P33 operation. 34 The MW 12 which is delivered into the reactor inlet 6 ' 35 will drop into a pyrolysis transport pipe 62 which extend 36 into a pyrolysis chamber 64 through a chamber wall 66. Th 37 pyrolysis transport pipe 62 extends laterally completel 38 across the chamber 64 and passes through the opposing chambe wall 66 to interface with the solid output subsystem 34 and the liquid output subsystem 32. As is shown in Fig. 1, a waste transport auger 68 is situated within the transport pipe 62 to continually urge the waste material 12 forward and through the transport pipe 62. The auger 68 is continually driven by an auger motor 70, shown in Fig. 1. The interior of the pyrolysis transport ("PT") pipe 62 is the locus where the primary pyrolysis reactions occur. The transport pipe 62 must be a strong, highly thermally conductive material, such as stainless steel, which is also resistant to material adhering to the surface and clogging the system. The upward facing surface of the pyrolysis PT pipe 62 is provided with a series of perforations 72. The perforations allow the escape of gaseous output materials 16 from the transport pipe 62, while not providing egress to a substantial amount of solid. The gaseous phase output 16 which is created within the pyrolysis transport pipe 62 during the pyrolysis process escapes through the perforations 72 and into the interior of the chamber 64. The interior of the pyrolysis chamber 64 is defined by the enclosing chamber wall 66. The chamber wall 66 is preferably constructed of a high strength, corrosion resistant, non-stick material such as stainless steel which is able to withstand the high temperatures which are generated therein. The interior surface of the enclosing chamber wall is required to be a nonreactive material, such as stainless steel, particularly in those portions which are exposed to hydrocarbon gases generated during the pyrolysis process. In order to reduce energy loss and to maximize safe and tolerable ambient conditions, a substantial layer of insulation 67 is provided about the entire chamber 64. The insulation layer 67 provides protection against radiative heat loss from the chamber wall 66 and prevents escaping thermal energy from the chamber 64 from interfering unnecessarily with the other operations of the system 20. In the case of the preferred embodiment 10, the elevated temperatures are provided by the heating subsystem 28, which is primarily illustrated in Fig. 1. The heating 1 subsystem 28 of the preferred embodiment 10 includes one or 2 more high power gas jet burners 74 which extend into the 3 chambe 64 through the chamber wall 66. The gas jet burners 4 74 receive input from a fuel, infeed 76, which will be 5 discussed hereinafter, and an air infeed 78, as shown in Fig. 6 1. The air infeed 78 is attached to the output of the 7 blower/pump 52. Consequently, some of the gaseous material 8 delivered to the gas burners 74 is that which is evacuated 9 from the vacuum chamber 44. The blower/pump 52 is always 10 maintained at sufficient volume and pressure to fully fuel 11 the gas burners 74 and further to maintain a relative 12 positive pressure within the chamber 64. The blower/pump 52 13 provides sufficient air flow to provide a turbulent burn 14 pattern in the gas burners 72, helping to avoid any "cold 15 spots" from incomplete convection in the furnace space 88. 16 In addition to the pyrolysis transport pipe 62, the 17 chamber 64 further encloses a diffusion material transpor 18 pipe 80. The MD transport pipe 80 extends across the chambe 19 64 above and parallel to the PT pipe 62. The MD transpor 20 pipe 80 is connected to the pyrolysis transport pipe 62 by 21 MD chute 82 situated near the point at which the pyrolysi 22 transport pipe 62 enters the chamber 64. The MD transpor 23 pipe 80 is further provided with a series of MD perforation 24 84, similar to the MW perforations 72 of the PT pipe 62. 25 A partition 86 extends from the sides of the PT pipe 6 26 to the associated chamber wall 66 to provide an effectiv 27 seal separating the interior of the chamber 64 into separat 28 vertical zones. The partition 86 and the PT pipe 6 29 reasonably isolate the portions of the chamber 64 which exis 30 below and above it. Since combustion gases and excess oxyge 31 are introduced into the chamber 64 by the heater subsyste 32 28, it is important that the MW 12 be isolated from these i -33 order to maintain the integrity of the pyrolysis reaction 34 That, portion of the chamber 64 which is situated below the P •35 pipe 62 and the partition 86 is an effectively sealed heatin 36 chamber or furnace space 88. Since actual combustion i 37 taking place constantly in the furnace space 88, and sinc 38 oxygen (as opposed to hydrocarbon gases) present as reactio material, unlike in the reaction space 90, internal insulation may be desirable in the furnace space 88. For this reason, with exception of the lower surfaces of the PT pipe 62 and the partition 86, the interior of the furnace space 88 may be provided with a heat retentive lining such as a ceramic fire brick, or the like. That portion of the chamber 64 which includes the interior of the PT pipe 62 and all of the interior of the chamber above the partition 86 constitutes the reaction space 90 in which the pyrolysis reaction occurs. The furnace space 88 includes the flame ends of the gas burners 74 and receives the combusted and uncombusted outputs therefrom. This will include noncombustible gases which may be received into the gas burners 74 from the blower/pump 52. The gas burners 74 will be controlled in order to maintain a highly elevated temperature within the furnace space 88, which, for the example of a pyrolysis system 10 adapted for use with vehicle tire chips, will be approximately 500°C. An exhaust tube 92 extends outward from the chamber wall 66 at the opposing end of the furnace space 88 from the gas burners 74. The exhaust tube 92 is adapted to carry exhaust gases 94 generated within the furnace space 88 to other locations. In the illustration of Fig. 1, the exhaust tube 92 is seen to connect directly to the MD input subassembly 26, where the high temperature exhaust gases 94 are utilized to preheat the diffusion material 14. In the alternate embodiment illustrated in Fig. 3, the exhaust tube 92 includes one or more convolutions 96 which cause the sealed exhaust tube 92 to pass through the chamber wall 66 and into the reaction space 90. This allows the exhaust gases 94 to pick up additional heat from the thermal energy within the reactor space 90 and to be heated to an even more elevated temperature when they reach the MD input subassembly 26. The diffusion material 14 (referred to as "MD" 14) is introduced into the pyrolysis chamber subsystem 24 through the MD input subsystem 26, illustrated in Figs. 1 and 4. It may be seen that the MD input subsystem 26 is very similar in construction and operation to the MW input subsystem 22. Accordingly, the MD input subsystem 26 includes an MD input hopper 98 which delivers the diffusion material 14, ordinarily carbon black in the preferred embodiment 10, downward into an MD conduit 100. Λn MD slide gate 102, a first MD flat gate 104, an MD screen filter 106, situated within an MD vacuum chamber 108, and a second MD flat gate 110 lie within the MD conduit 100 below the MD input hopper 98. An MD gate mechanism 112, similar to the MW gate mechanism 48, controls the operation of the various gates and a vacuum evacuation system including a MD vacuum pipe 114, a MD control valve 116 and an MD bypass 118, is also provided. As may be seen from Fig. 1, the MD vacuum pipe 114 is also connected to the blower/pump 52 to provide evacuation of the MD vacuum chamber 108 through the MD screen filter 106 and further to deliver any fugitive vapors which escape the reaction space 90 through the MD input subassembly 26 back into the blower/pump 52 for " attempted combustion by the turbulent gas burners 74. The bottom of the MD conduit 100 interfaces with an MD inlet 120 which provides access for the diffusion material 14 into the MD transport pipe 80. Within the MD transport pipe 80, an MD auger 122 is driven by an MD drive motor 124. The MD auger 122 is angled in the opposite direction to the waste transport auger 68 such that the diffusion material 14 is urged through the MD transport pipe 80 in the directio opposite to the direction that the MW 12 is urged through th PT pipe 62. The MD 14 is utilized for direct transfer of heat int the MW 12. The MD 14 is utilized to preheat the wast material and to facilitate the pyrolysis reaction b retaining and conducting heat into the MW 12 within the P pipe 62. Further, when the diffusion material 14 is selecte to be a material such as carbon black, it can serve t actually react with some of the components of th carbonizable waste material 12 or to catalyze reactions whic result in efficient pyrolysis and cracking of the material and lead to a greater yield of usable output. Since it is desirable to have the diffusion material 14 already established at a very high temperature and retained heat level prior to being delivered to the MD chute 82, which drops the MD 14 into the MW 12 being driven through the PT pipe 62 by the waste transport auger 68, the MD transport pipe 80 extends within the reaction chamber 90 so that it and its contents are preheated. Further, additional heat is delivered to the diffusion material 14 by the heated exhaust gases 94 which are carried in the exhaust tube 92, particularly when the exhaust tube 92 includes the convolutions 96 which result in additional heat being absorbed by the exhaust gases 94 before they are delivered into the diffusion material 14. The interface between the exhaust gases 94 and the diffusion material 14 occurs at a heat exchanger device 126 which is situated at the end of the MD transport pipe 80 which is adjacent to the MD inlet 120. The nature of the heater exchanger 126 may be any of several structures which permits the exhaust gases 94 to provide preheating to the MD 14 which is carried within the MD transport pipe 80. This may be as simple as a chamber formed about the MD transport pipe 80 with the exhaust gases 94 passing therethrough, or it may be a more complex and convoluted heat exchanger device 126. In the preferred embodiment 10, as shown in Figs. 1 and 4, the outlet of the heat exchanger 126 is in the form of an exhaust outlet 128 which has an exhaust fan 130 included therein. The exhaust fan 130 is operated in order to continually draw the exhaust gases 94 out of the furnace space 88 and through the heat exchanger 126, in order to maintain good combustion conditions within the furnace space 88 and also to continually preheat the diffusion material 14. The diffusion material 14, after being partially preheated by the exhaust gases 94 and the heat exchanger 126, is continually driven through the MD transport pipe 80 by the MD auger 122. The predominant portion of this travel path will lie inside the pyrolysis chamber 64 and in the reaction space 90. The elevated temperature within the reaction space 90, and the conductive transfer of heat to the MD 14 from the 1 gaseous output 16 of the MW 12, will cause further preheatin 2 of the MD 14 as it passes through the MD transport pipe 80. 3 The conductive heat transfer is permitted by the M 4 perforations 84 which allow the gases to intermix with the M 5 14. The MD perforations 84 further allow the escape o 6 expansion gases which may be created in the MD 14 as i 7 passes through the MD transport pipe 80. 8 At the end of the chamber 64 opposite the MD inpu 9 subsystem 26, the MD 14 is delivered from the MD transpor 10 pipe 80 to the MD chute 82. At this point the diffusio 11 material 14 is dropped into the pyrolysis transport pipe 6 12 where it is mixed (by the action of the waste transport auge 13 68) with the waste material 12 which is already present i 14 the PT pipe 62. This mixing of the diffusion material 14 wit 15 the waste material 12 improves the efficiency of th 16 pyrolysis process by conductive heat transfer and also, to 17 lesser degree, by direct reaction or catalysis. It may als 18 be seen that in points forward on the flowpath from the M 19 chute 82, the content of the PT pipe 62 will be a mixture o 20 the waste material 12 and the diffusion material 14, with th 21 pyrolysis process being continually in progress throughou 22 the length of the PT pipe 62. 23 The result of pyrolysis on the input waste material 1 24 is the geration of reaction products in the form of th 25 gaseous phase output 16, the liquid phase output 18 and th 26 solid phase output 20. The gaseous phase output 16 is handle 27 by a gaseous output subsystem 30 which is illustrated in Fig 28 1 while the liquid output 18 and the solid output 20 will 29 carried through the PT pipe 62 and be delivered to the sol 30 output subsystem 34, from which the liquid output subsyst 31 32 branches. The liquid output subsystem 32 and the sol 32 output subsystem 34 are illustrated in Figs. 1 and 4. - 33 Referring to Fig. 1, it may be seen that the gaseo 34 phase output subsystem 30 is adapted to receive the gaseo .35 phase output 16 which will be drawn through a gas outlet 1 36 situated at the top of the chamber 64. The gas outlet 1 37 connects the chamber 64 to a gas tube 134. The gas tube 1 38 extends upward and away from the chamber 64. The hydrocarb gases continue through the gas tube 134 and enter into a condenser unit 136. Within the condenser unit 136, the gaseous output 16 is primarily converted into hydrocarbon gases and various liquids. Typically, the condenser unit 136 may utilize oil quenching, water cooling or forced air condenser technology. From the condenser unit 136, the output is delivered through a condenser conduit 138 to a storage tank 140. From the storage tank 140, the liquid components are drawn off through a fluid conduit 142 for further processing. The fluid components may be in the forms of oils, hydrocarbon liquids or other fluids which can then be refined by conventional techniques. Primarily, the fluid contents will be hydrocarbons which can be utilized for a variety of purposes, once separated into components. Those portions of the gaseous output 16 which remain in the gaseous phase 16 after passing through the condenser unit 136 are then removed from the storage tank 140 through a gas conduit 144 which is connected to a gas pump 146. The gases which are delivered through the gas conduit 144 to the gas pump 146 are primarily combustible hydrocarbon gases, such as methane, which are suitable for use as fuel for the gas jet burners 74. Accordingly, the output for the gas pump 146 is into the fuel infeed line 76 where it forms the primary burner fuel. For those circumstances in which the supply of combustible hydrocarbon gases from the storage tank 140 is insufficient to fuel the burners 74, an auxiliary natural gas feed 148 is provided with an auxiliary gas valve 150 to control the flow of gas from an outside source, such as a tank or a utility line. It is expected that during full operation, the auxiliary gas valve 150 may be closed since enough hydrocarbon fuel will be generated to operate the burners 74, but it will be open at the time of startup and at any time during which the fuel flow from the storage tank 140 is insufficient to provide for the burners 74. It is also possible that, at times, the pyrolysis reaction and energy conservation techniques will be so efficient that more combustible hydrocarbon gas may be produced by the gaseous phase output subsystem 30 than can be efficiently combusted by the turbulent gas burners 72. For this reason, an excess gas bleed value 151 is provided to allow removal and storage of excess production. The components of the preferred liquid output subsystem 32 and solid output subsystem 34 are illustrated primarily in Fig. 4, wherein it may be seen that the material which is delivered to the output end of the PT pipe 62 by the action of the waste transport auger 68 will be delivered to a dro chute 152 which extends downward into a conveyor tube 154. The material within the drop chute 152 will be a mixture o liquid output 18 and solid output 20, in most cases. It i understood that in most cases that the liquid component o the output of the thermal conversion pyrolysis reactor syste 10 will be rather minimal, at least through the PT pipe 62, and what liquid material exists may be captured in th material of the solid output 20 so that it is not a separat component. However, in certain circumstances it is importan to provide for the collection of the liquid output 18 so tha it may be separately collected. The solid output material 2 is delivered up the conveyor tube 154 by a screw conveyo 156, while the liquid material 18 will flow down to th bottom of the conveyor tube 154 and through a drain tube 15 to a collector tank 160. A filter disk 162 may be provided i the conveyor tube 154 to prevent the solid output materia 20, which may be in the form of flowable powders, fro clogging the drain tube or flowing into the collector tan 160. The liquid phase output 18 which is collected in th collector tank 160 will be subjected to further treatment, a needed, depending on its nature and quantity. The solid phase output 20, which will be in the form o waste residue and diffusion material 14, will be transporte up the conveyor tube 154 by the screw conveyor 156, which i powered by a conveyor motor 164. The residue material i carried up the screw conveyor 156 to the top of the conveyo tube 154 where it is delivered to a residue chute 166. Th bottom of the residue chute 166 rests against a residue sli gate 168. The residue will rest on the residue slide gate 168 until the slide gate 168 is opened, when it will drop through a collection chute 170 into a collection hopper 172. In many embodiments it may be desirable to provide additional cooling to the solid residues. This may be accomplished by cooling jackets or heat exchanger devices about the conveyor tube 154. Forced air cooling may also be desirable as a means of reducing the residue temperature to facilitate subsequent handling. In the preferred embodiment of the present invention 10, one of the advantages is that the diffusion material 14 will be substantially recoverable from the residue. The mechanism for accomplishing this is that as the residue passes from the collection chute 170 into the collection hopper 172 it will drop onto a separator unit 174. The preferred separator unit 174 will be in a form of a fine mesh screen which has a mesh which is sufficiently open to allow the particulate carbon black diffusion material 14 to pass through into a MD collector compartment 176 in the collection hopper 172, with the MD collector compartment 176 being situated beneath the separator screen 174. The preferred separator screen 174, which is illustrated in Figs. 1 and 4, is inclined such that the larger diameter particulate residue will not pass through the separator screen 174 and will be caused to slide off the end of the screen 174 into a residue collector compartment 178. It is understood that the above discussion of the separator system presupposes a fine particulate form of MD 14, such as carbon black, which has a smaller particulate diameter than the remainder of the solid residue. If a pellet type MD 14 is utilized, the reverse may be the case and the MD may have a larger particle diameter. In such an instance the arrangement of the MD collector compartment 176 and the residue collector compartment 178 will be interchanged. As will be understood by those skilled in the art, various modifications and alterations of the specific structure described above as constituting the preferred embodiment may be utilized with acceptable results. For example, the specific structures of the chutes, gates and *ubes described above may be modified substantially while ---.till retaining the primary functional characteristics and providing results which are improved over those of the prior art. Certainly, the dimensions and materials may also be modified, particularly depending upon the specific purpose for which the thermal conversion pyrolysis reactor system 10 is intended to be used. One component of the process which is significant is the selection of the diffusion material 14. As described above, the preferred MD 14 is carbon black, a fine grained crystalline carbon material. Other diffusion materials may be appropriate, but they must be selected from those which have high thermal conductivity and substantial corrosio resistance. An alternate potential MD 14 is a corrosio resistant metal such as pellets of stainless steel. Som other metal materials, such as tin, lead and alloys thereof, are not suitable for use as the MD 14 because of their lo melting points, other materials which are excellent hea conductors, such as silver and copper, are highly suitabl for that purpose but can have undesirable side effects sinc there may be reactions between these metals and th hydrocarbon products involved. Ceramic diffusion material such as aluminum nitride, silicon carbide and the like ar corrosion resistant and could be utilized as the diffusio material 14. However, ceramic materials have a tendency t break up and are not as easily recycled so these are no preferred. Another group of materials which may be acceptable a the thermal diffusion material 14 are those of the class o tungsten compounds which are corrosion resistant. Thes include such tungsten compounds as tungsten dioxide, tungste trioxide and tungsten carbide. A potential disadvantage o the tungsten compounds is that they are very dense (heavy and may require a stronger material handling structure. Thi can be reduced somewhat by utilizing a mixture of tungste compounds with a lighter material, such as stainless steel. //// One of the advantages of materials such as carbon black is that the graphite structure provides a lubricating action as well as heat transfer. This acts to optimize the material flow through the reactor and to prevent problems such as clogging. This, with the rotational motion provided by the transport auger 68, provides a cleansing and lubricating effect which minimizes the necessity for stopping the process for cleaning. The combined effects of lubrication and heat transfer result in maximum efficiency of the process. Additionally, some of the diffusion material 14 may be added into the MW input hopper 36 from time to time in order to help clean the waste conduit 38 and the associated structure. The dimensions and materials of the reactor and the associated mechanism will be selected to suit the intended purpose, with any combinations being appropriate and with empirical adjustments of the ratio of diffusion material 14 to waste material 12. Those skilled in the art will readily recognize that numerous other modifications and alterations of the specific structures, dimensions, materials and components may be made without departing from the spirit and scope of the invention. Accordingly, the above disclosure is not to be considered as limiting and the appended claims are to be interpreted as encompassing the entire scope of the invention. INDUSTRIAL APPLICABILITY The thermal conversion pyrolysis reactor system 10 according to the present invention is adapted to be utilized in a wide variety of industrial and municipal applications wherein it is desired to convert carbonizable material into usable byproducts. The system 10 is adapted particularly for use with waste products such as vehicle tire chips, plastic bottles and hospital waste. Assuming initial products which generate a substantial amount of hydrocarbon gases upon pyrolyzation, the system 10 is adapted to be self powering, after initialization. //// 1 When it is dnr.irod to utilized the invention, the gas 2 jet burners 74 are activated to preheat the furnace space 88 3 to the desired temperature prior to inputting any material. 4 For the example where the waste material 12 to be pyrolyzed * 5 is shredded tire material, the operation temperature will be 6 in the range of 400° to 760°C (750° to 1400°F) although * 7 higher temperatures, within the tolerances of the materials, 8 may be utilized for a variety of purposes. It is desirable to 9 provide a heating temperature in the furnace space 88 which 10 is generally far higher than the vaporization temperature of 11 the MW 12 in order to maintain good operating efficiency. 12 Once the chamber has been preheated, it is desirable to 13 begin feeding the diffusion material 14 into the diffusion 14 material input system 26. This is accomplished such that 15 preheated diffusion material 14 is already in place by the 16 time the first dollop of waste material 12 reaches the 17 reactor chamber 64. The MD 14 is preheated first by the 18 action of the exhaust gases in the heat exchanger 126 and 19 then by the heat of the reactor chamber 90 as the MD 14 20 passes through the MD transfer pipe 80. 21 The waste material 12 placed in the input hopper 36 is 22 then delivered through the gate system (described above) to 23 the reactor inlet 60. In the incoming MW 12 will b 24 substantially evacuated of excess gases, with the desir 25 being to eliminate oxygen, in particular, by the action of 26 the vacuum force applied to the vacuum chamber 44. Althoug 27 it is expected that the MW 12 will be primarily in the for 28 of solids, it is possible there may be liquids components a 29 well. All of these will be delivered by gravity feed and th 30 operation of the gate operating mechanism 48 to the pyrolysi 31 transport pipe 62. 32 The action of the waste transport auger 68 will driv a 33 the waste material 12 forward through the PT pipe 62 to th 34 point at which it lies directly beneath the diffusio Λ 35 material chute 82, at which time preheated diffusion materia 36 14 will be deposited thereon and mixed therewith by action o 37 the auger 68. The MD 14 will act as a heat transfer mediu 38 and as a lubricant, and to a lesser degree, as a reactio catalyst. The heat transfer properties of the diffusion material 14 act to heat the MW 12 more rapidly such that a faster flow process may be feasible. This means that the auger motor 70 may be operated at a reasonable speed in such a manner that complete pyrolysis within the pyrolysis chamber subassembly 24 may be achieved in minimal amount of time. For a furnace chamber temperature of approximately 750°C (1382°F) , and an MD 14 of stainless steel and aluminum nitride pellets, it is expected that a resident time of approximately 25 minutes in the pyrolysis reactor subassembly 24 will be needed in order to pyrolyze the typical tire chip material. During the pyrolysis reaction, the MW 12 will be broken down in an oxygen free reaction to form hydrocarbon gas material and other gaseous phase output 16 and residual solid phase output 20. When the MW 12 selected is tire chips, only a very minimal amount of liquid phase output 18 is produced. The gaseous phase output 16 will escape from the PT pipe 62 through the perforations 72 on the upper surface thereof. These gases will then pass through the reaction chamber 90, with a certain amount acting to help preheat the diffusion material 14 and the MD transport pipe 80, and will exit the chamber 64 through the gas outlet 132. The gaseous phas output 16 will then be treated by the gaseous outpu subsystem 30, as described above, with a portion thereof being combustible hydrocarbon gases which are then delivere back to the heating subsystem 28 in order to provide fuel fo the turbulent gas jet burners 74. In this manner, the therma conversion pyrolysis reactor system 10 becomes substantiall self powered and can operate as a continuous flow proces without additional fuel. The solid phase output 20, primarily the diffusio material 14, additional carbon caused by pyrolysis of th carbonizable waste materials, and noncarbonizable material found in tires, such as the residue of steel cables an fiberglass or other synthetic cable materials, will b delivered through the end of the PT pipe 62 to the drop chut 152, where they will drop into the conveyor tube 154. An 1 liquid phase output 18 will then pass through the filter disk 2 162 and downward to the collector tank 160. The residual 3 solids will then be carried upward within the slanted 4 conveyor tube 154 by the action of a screw conveyor 156 to a * 5 residue chute 166. 6 When a desired amount of material has collected in the * 7 residue chute 166, the residue slide gate 168 will open and 8 deposit the material through a collection chute 170 on top of 9 the separator unit 174. The separator screen 174, situated 10 within the collection hopper 172, will then, via vibration, 11 allow the diffusion material 14 to pass therethrough into the 12 MD collector compartment 176, with the remainder of the 13 residue being delivered to the residue collector compartment 14 178. The diffusion material 14 which is collected in the MD 15 collector compartment 176 may then be reutilized for input 16 into the MD hopper 98. 17 The result of the output of the system 10 will be 18 exhaust gases 94 from the furnace space 88, which will pass 19 to the ambient atmosphere through the exhaust outlet 128, 20 liquid phase hydrocarbons which are the result of 21 condensation of the gaseous phase output 16, as converted by 22 the condenser 136, liquid phase output 18 collected in th 23 collector tank 160 and the solid residue 20 which resides i 24 the residue collector compartment 178. Given the parameter 25 of the MW 12, it is expected that each of these resultin 26 materials will be relatively easily handled and usabl 27 materials, as contrasted with the waste products which ar 28 input into the pyrolysis reactor system 10. 29 Although described above as applicable to vehicle tir 30 fragments, the pyrolysis apparatus and method can also appl 31 to other carbonizable materials such as wood chips, carpet 32 plastic, sewage sludge and the like. For general wast 33 materials, presorting is preferred in order to remov 34 materials which are resistant to the reactions or which coul -35 foul the apparatus. These will include materials such a 36 glass, aluminum cans and the like. The general goal is t 37 vaporize the infeed material as effectively and efficientl 38 as possible. The use of carbon black as the diffusion material 14 is particularly desirable when the input MW 12 is hospital waste or other materials which may contain unstable or hazardous chemical compounds. The carbon black is utilized to react with the infeed material during the thermal conversion pyrolysis process due to the fact that it will combine to stabilize and break down many of the hazardous chemical materials which might otherwise vaporize and contaminate the gaseous phase output subsystem 30 in a normal pyrolysis reaction. Under these circumstances the primary goal is to yield desired hydrocarbon vapors effectively and efficiently without the production of undesired byproducts. In light of the many efficiencies and advantages of the thermal conversion pyrolysis reactor system 10 of the present invention, it is expected to appeal to a great number of potential users. Efficiency of operation, minimum down time for cleaning, substantial self-powering, and recyclability of the diffusion material 14 provide advantages which make the structure attractive. Accordingly, it is expected that the thermal conversion pyrolysis reactor system 10 according to the present invention will have industrial applicability and commercial utility which are both wide spread and long lasting.

Claims: IN THE CLAIMS 1. A pyrolysis reactor system for use in pyrolyzin carbonizable input material (MW) , comprising: a reactor chamber subsystem including an enclosed reacto chamber; an MW input subsystem for inputting carbonizable materia into said reactor chamber subsystem; an MD input subsystem for inputting diffusion material (MD) into said reactor chamber subsystem; heating means for maintaining the interior of said reacto chamber subsystem at an elevated temperature, the elevate temperature being sufficient to pyrolyze the carbonizabl material; a gaseous phase output subsystem for receiving an processing the gaseous phase products of pyrolysis reactions fro said reactor chamber subsystem; and transport means for transporting the MW and MD from sai associated input subsystem, through said reactor chambe subsystem, and through nongaseous phase output subsystem situated at an end thereof; wherein, the MD is raised to an elevated temperature an mixed with the MW near the location at which the MW enters sai reactor chamber subsystem, such that the MD acts to conductivel heat the MW and enhance the pyrolysis process thereon as the M and MD are carried together through said reactor chambe subsystem. 2. The pyrolysis reactor system of claim 1 wherein sai transport means for transporting the MW and the MD include: a pyrolysis transport pipe extending generally horizontally within said reactor chamber for carrying t MW, the pyrolysis transport pipe having an input e adjacent to said MW input subsystem and an output e adjacent to the nongaseous phase output subsystem; an MD transport pipe extending generally horizontal within said reactor chamber for carrying the MD, the transport pipe being disposed above the pyrolysis transpo pipe and having an input end adjacent to said MD input subsystem and a terminal end; an MD chute disposed intermediate the terminal end of the MD transport pipe and a location near the input end of the pyrolysis transport pipe; an MD auger extending through the MD transport pipe and being associated with an MD auger motor such that the MD auger is rotated so as to drive the MD through the MD transport pipe to the terminal end and to urge the MD material to be gravitationally delivered through the MD chute to the pyrolysis transport pipe; and an MW auger extending through the pyrolysis transport pipe and being associated with an MW auger motor such that the MW auger is rotated so as to mix the MD entering the pipe from the MD chute with the MW received from said MW input subsystem and to drive the MW and the admixed MD from the input end to the output end. 3. The pyrolysis reactor system of claim 2 wherein the pyrolysis transport pipe is provided with perforations on the upper surface thereof to allow the escape of gaseous phase output from the pyrolysis reaction. 4. The pyrolysis reactor system of claim 2 wherein dividing means extend from the pyrolysis transport pipe to the walls of said reactor chamber so as to separate said reactor chamber into a furnace space situated below the dividing means and a reaction space situated above the dividing means, the interior of the pyrolysis transport pipe being a portion of the reaction space. 5. The pyrolysis reactor system of claim 4 wherein the MD transport pipe is situated within the reaction space and is provided with upwardly disposed perforations to permit gases within the reaction spsce to contact and transfer heat to the MD being carried through the MD pipe. 1 6. The pyrolysis reactor system of claim 2 wherein 2 exhaust gases from the furnace space are delivered to a 3 heat exchanger associated with said MD input subsystem for 4 transferring heat to the MD. 5 6 7. The pyrolysis reactor system of claim 1 wherein 7 said MW input subsystem and said MD input subsystem 8 each include degassing means for substantially removing 9 oxygen and fugitive gases from the MD and MW prior to 10 delivery into said reactor chamber. 11 12 8. The pyrolysis reactor system of claim 1 wherein 13 said gaseous phase output subsystem includes means for 14 delivering recycled combustible gases to said heating means. 15 16 9. A thermal conversion pyrolysis reactor system, fo 17 pyrolyzing carbonizable material ("MW") , comprising: 18 a thermal pyrolysis chamber, the interior of which is heate 19 to a temperature ("T") sufficient to substantially pyrolyze th 20 MW in a moderate length of time; 21 MW means for delivering the MW into and through said therma 22 pyrolysis chamber; 23 MD means for delivering a heat diffusion material ("MD") t 24 the interior of said chamber in a manner such that the MD i 25 mixed with the MW and is concurrently therewith delivered throug 26 said thermal pyrolysis chamber; 27 MD preheating means for heating the MD to a temperatur 28 approaching T prior to delivery to and mixing with the MW; and 29 output handling means for receiving and processing th 30 reaction products of the pyrolysis process and the unreacte 31 output of said thermal pyrolysis chamber. 32 33 34 35 "36 37 38 10. The thermal conversion pyrolysis reactor system of claim 9 wherein said MD means and said preheating means include an MD transport pipe extending substantially within the interior of said thermal pyrolysis chamber, such that the MD being delivered therethrough absorbs ambient heat from the interior of said thermal pyrolysis chamber prior to mixing with the MW. 11. The thermal conversion pyrolysis reactor system of claim 9 wherein said thermal pyrolysis chamber is separated into a furnace space wherein combustive heating is provided by turbulent burners to evenly heat the interior and a reaction space in which the MW and MD are situated during the pyrolysis reaction; and said preheating means include delivery of exhaust gases generated in the furnace space to preheat the MD. 12. The thermal conversion pyrolysis reactor system of claim 11 wherein said output handling means include means for recycling combustible gaseous reaction products for use in the turbulent burners. 13. The thermal conversion pyrolysis reactor system of claim 11 wherein said MW means and said MD means each include degassing means for substantially removing gases from the MW and MD prior to delivery to said thermal pyrolysis chamber, the gases removed by the degassing means being delivered to the turbulent burners. 14. The thermal conversion pyrolysis reactor system of claim 9 wherein said output handling means include means for separating the MD from other reaction products such that the MD may be recycled for additional use. 15. The thermal conversion pyrolysis reactor system of claim 9 wherein the interior of said thermal pyrolysis chamber is maintained at a positive pressure with respect to ambient such that entry of oxygen bearing gases thereinto is minimized. 16. In a thermal conversion pyrolysis reactor system for pyrolyzing carbonizable material ("MW"), including a heated reactor chamber, an MW input assembly, means for transporting the MW through the reactor chamber and output processing means for handling the products, byproducts and residues of a flow-type pyrolysis reaction process, the improvement comprising: providing a preheated thermal diffusion material ("MD") for admixing with the MW such that the MW is mixed and transported concurrently with MD within the chamber such that heat is conductively transferred from the MD to the MW so as to enhance the pyrolysis reaction and reduce the elapsed reaction time to acceptable completion. 17. The improvement of claim 16 wherein the pyrolysis reactor system is made self supporting by recycling combustible reaction products from the output processing means to burner components utilized to elevate the temperature of the heated reactor chamber. 18. The improvement of claim 16 wherein the MD is preheated by being resident for a substantial interval within the heated chamber prior to being admixed with the MW. 19. The improvement of claim 16 wherein the interior of the reaction chamber is maintained to be substantially free of oxygen by degassing the MW and M prior to entry thereinto and by maintaining the reactor chamber at a relative positive pressure.

Inventors: CHEN SABRINA CHIOU-CHAR, WU ARTHUR CHENG-HSIN, CHEN, SABRINA, CHIOU-CHAR, WU, ARTHUR, CHENG-HSIN
Applicants: CHEN SABRINA CHIOU CHAR, WU ARTHUR CHENG HSIN, CHEN, SABRINA, CHIOU-CHAR, WU, ARTHUR, CHENG-HSIN
Application year: 1993
Main classification: F28D7
IPC codes: B01J8, B09B3, C09C1, C10B7, C10B47, C10B53, C10G1, C10J3, F23K3