FLUID WALL REACTOR

Abstract: The reactor tube 20 for a high-temperature fluid wall reactor is heated to incandescence and radiates energy inwardly to a reaction zone. The tube 20 is perforated to form an inert gas protective fluid wall for preventing reactant products from contacting the tube. Inert gas jets 86 are formed each having a substantially radially-directed momen­ tum sufficient to repel the reactants. Sections of the reactor tube may remain unperforated, but are protected by the downstream flow of the injected inert gas. A whisker fiber material and continuous flow production methods are also provided. Feedstock comprised of forms of silicon and a reductant are vaporized in the tube 20 and rapidly cooled. Yield is enhanced by reducing feedstock particle size and providing a gaseous reductant, such as sand flour and methane, respectively. Process variables control yield, uni­ formity, and surface area of the material which is comprised substantially of silicon and/or silicon oxide whiskers in varying proportions.

Description: FLUID WALL REACTOR AND METHOD FOR PRODUCTION OF FIBERS FIELD OF THE INVENTION The present invention relates to a reactor tube for a high temperature fluid-wall reactor, and, more particularly, to a reactor tube for a reactor wherein the reaction zone spaced interiorly of the reaction tube is substantially heated by radiant energy passing through a fluid wall. The invention is also directed to a method for forming the desired fluid wall with the reactor tube as described herein. This invention further relates generally to fiberous material and, more particularly, to novel whisker-type fibers and methods for production thereof. BACKGROUND OF THE INVENTION The present invention relates to a reactor tube for forming a high-temperature fluid-wall reactor, and to the process for enabling such a reactor tube to form an integral fluid wall for preventing reactants from contacting the interior surface of the tube. The reactor of the present invention may utilize radiation coupling, so that electrodes radiate heat to the reactor tube, which is heated to incandescence and accordingly radiates energy inwardly to maintain the desired chemical reaction within the protective fluid-wall blanket. Heat generating reactors have been employed in various industrial processes, but conventional reactors utilizing convection and/or conduction generally are not suitable for many high temperature reactions. At elevated temperatures, the heat transfer material for such conventional reactors generally reacts with the feedstock and fails, or reactants accumulate on the heat transfer walls of such conventional reactors, thereby substantially reducing the efficiency of the thermal process. Examples of such conventional reactors are found in U.S. Patents 2,769,772, 2,926,073, and 3,565,766. U.S. Patent 2,750,260 discloses a technique for manufacturing titanium dioxide pigment by combustion of titanium tetrachloride with oxygen. The deposition of titanium dioxide particles on the walls of the cooling zone of the reaction apparatus is suppressed by slowly diffusing a purge gas through a porous wall. The mass of the purged gas is considered controlling rather than the gas pressure or pore size of the interstices through the wall, although the pore size less than 1 mm in diameter is preferred. In the combustion zone temperatures may reach 29400F (16000c), although in the cooling zone where the reactant deposition is suppressed, the temperature is in the range of only 1140OF (600"C). U.S. Patent 3,499,730 discloses a combustion reactor for producing pigmentary titanium dioxide by the combustion of titanium tetrachloride in the presence of an auxiliary flame. The combustion reaction is carried out in a central flame confined within a foraminous wall tube. In the reaction zone, the cooling zone, and the recycling zone, a selected gas passes through the foraminous wall of the tube to form a barrier layer of gas which keeps particles of titanium dixoide formed in the central flame away from the wall of the tube. The gas passing through the foraminous wall of the tube also prevents the tube from reaching the temperature of the reaction zone, so that the wall may be maintained at substantially room temperature. The foraminous wall of the tube may thus be made of steel, aluminum or other metal, and perforations in the tube consists of from 2% to 40E of the wall surface. U.S. Patent 4,044,117-to Matovich discloses a fluid-wall reactor for carrying out chemical reactions at temperatures significantly higher than that disclosed in the earlier referenced patents. The reactor includes electrodes surrounded by a heat shield for heating a reactor tube made of a refractory material. The reactor tube is heated to a high temperature, and in turn emits sufficient radiant energy to initiate and sustain a desired chemical reaction which occurs within the interior of the reaction tube. Since the Matovich technique employs radiant energy rather than conduction or convection, a reactor tube material having poor thermal conductivity but relatively high temperature integrity may be utilized to form the reaction tube This "radiation coupling" technique and its advantages over conventional reactors are fully discussed in the '117 patent. In an attempt to alleviate the reactant and tube material reaction, and to reduce the accummulation of reactants on the interior surface of the reaction tube, Matovich utilizes a porous tube material to permit an inert gas to pass through the tube and provide a protective fluid wall for the inner surface of the tube. Various wall construction materials and types of perforations are disclosed in the '117 patent, although the reactor tube is preferably made of a porous refractory material having pore diameters in the range of from about 0.001 to 0.020 in. (0.025 mm to 0.508 mm). The reactor disclosed in the '117 patent is thus considered a significant advancement over the prior art, since it teaches the generation of substantially increased reaction temperatures without significant deposition of reactants on the inner surface of the reactor tube. A suitable porous tube for such a reactor may be fabricated from graphite, with a wall thickness of about 0.75 in. (19 mm). Porous graphite is usually made by sintering particles of graphite coated with a carbonizable adhesive to bond the particles together. Interstices between the particles form a network of random pores though which gas can pass. It is both difficult and expensive, however, to maintain uniform porosity of the graphite material. In order to maintain reasonable porosity uniformity, the porous graphite tubes may be produced in small sections or blocks having a thickness greater than that desired. Known commercially available porous graphite tubes, not specifically intended for fluid wall reactors, are limited to a diameter of approximately 14 in. (356 cm). Since the desired fluid wall within the tube may be approximately 1 to 2 in. thick (25 to 51 mm) thick, the diameter of the inner reaction tone is limited to sizes which are frequently not commercially attractive. The reactor of the '117 patent, although generally considered adequate for small-scale experimental work, has a number of significant drawbacks when operated on an industrial scale. Perhaps the most serious drawback is its inability to maintain a sufficient fluid wall to prevent reactants from contacting and reacting with the inner surface of the tube, especially at the location where the feedstock is input to the reaction zone. At commercial feedstock input rates, the reactants and porous tube chemically react, thus substantially reducing the life of the reaction tube. Moreover, engagement of the reactants with the porous tube tends to plug the interstices through the porous tube, thereby further reducing the effectivness of the fluid wall and decreasing tube life In industrial applications, the porous reactor tube of Matovich also is not capable of efficiently transmitting heat to the reaction zone in order to sustain many desired chemical reactions. For example, when a hydrocarbon oil was introduced into a commercial embodiment of the reactor at a relatively low flow rate, oil may be decomposed into hydrogen and a high-quality carbon black. However, when it was attempted to increase the flow to a reasonable production rate, the produced carbon black became oily and otherwise deteriorated in quality. It was.found that although the electrodes of the reactor were operating at a temperature of about 4000F (22000C), the temperature of the inner surface of the reactor tube was only about 3100"F (17000C). Since the intensity of radiant energy emitted by a surface is approximately porportional to the absolute temperature raised to the fourth power, this decrease causes a reduction in the intensity of radiant energy by a factor of roughly 0.4. As a result of the reduced intensity of radiant energy in '±he reaction chamber, the decomposition reaction did not proceed to completion, thereby giving rise to carbon black of inferior quality. Also, after a relatively short reaction time of several hours, the porous tube failed, largely due to chemical reactions between the porous wall material and both the reactants and injected gas for the fluid wall. Some of the pores through the tube were plugged, and thus it was determined that the porous tube did not effectively maintain the desired fluid wall. The number of chemical reactions which can be sufficiently commercialized with a reactor utilizing the porous tube of Matovich is therefore limited, because of its inability to maintain an effective fluid wall (which severely limits the life of the reactor tube), and because of its thermal inefficiency (due to the difference between the electrode temperature and the reaction temperature). Further limitations to the Matovich reactor include the significant consumption of inert gas required to maintain a reasonable fluid wall. Significant consumption of nitrogen, a suitable inert gas, increases the reactor operating costs and demands large capacity downstream equipment- for purifying the nitrogen for discharge. At elevated temperatures, nitrogen is not totally inert and does react with the graphite tube material, which structurally weakens the tube. Because of its porous nature, this nitrogen/graphite reaction occurs throughout the tube, and substantially limits the effective life of a porous tube. Finally, the nitrogen passing through the porous tube reaches substantial thermal equilibrium with the tube, thereby increasing the exit gas temperature which, in some reaction processes, must then be subsequently lowered. Whiskers are generically extremely small fibers grown under closely controlled conditions whereby fiber strengths approaching the materials inter-atomic bond strength may be achieved. Such fibers may typically range in size from 1-30 microns in diameter and have aspect ratios from 500-5000:1. A general discussion of such fibers may be found in "Handbook of Fillers and Reinforcements for Plastics",, Chapter 25, pages 446-464, by Milewski and Katz, Growth and Properties of 'Whiskers'", Science, September 12, 1958, Vol. 128, No. 3324, by S. S. Brenner, page 569-574, and representative patent references covering such materials and methods of production such as U.S. Patent Nos. 2,823,979; 3,409,395; 3,421,862; 3,622,272: and 3,668,062, all of which are herein incorporated by reference. Commercial research and development involving such whisker materials was initially quite active due to their unique properties and associated potential uses. As but one example, their theoretical strengths led researchers to believe such fibers had promising applications as reinforcing materials in epoxy, thermoplastic, and other matrices. However, the initial interest and enthusiasm in the art subsided for several reasons. First, researchers were experiencing unanticipated difficulties in achieving or approaching the theoretical benefits of the fibers even on a laboratory scale due to numerous technical difficulties in handling and processing the materials. There were also serious difficulties encountered in even producing the whisker fibers themselves. More particularly, due to the slow batch-process techniques known in the art for growing whiskers and the difficulties in isolating them from other materials in the process output, these whiskers could not be easily grown in commercial quantities at reasonable prices. Moreover, even with some improvement tn production rates, further problems remained in maintaining, preselecting, and controlling the reproducibility of the processes and the resultant fiber characteristics. With regard to the fiber lengths produced in accordance with U.S. Patent No. 2,823,979, as but one example, such lengths ranged only between 50-600 nm. Theory suggested that by growing whiskers smaller and smaller in the form of cobwebs whiskers whereby diaineters might be on the order of 1/100th that of conventional whiskers, even greater material strengths and other benefits could be achieved. The term "cobweb whiskers" herein refers to inorganic fibers wherein the average diameter of the population is less than 100 nanometers. As indicated in the aforementioned article by Milewski, et al., this could mark the beginning of a major technological revolution in super-strength materials. In particular, one such form of cobweb whisker fiber has been reported in the art to be single crystal alumina whiskers. However, the composition of these whiskers has been suggested by the inventor perhaps to be silicon carbide instead. Such whiskers have been shown to possess incredibly high tensile strengths of between 2-4 million psi, and may have diameters on the order of 18 nm. However, in the case of the ultra-small or cobweb whiskers, the aforementioned difficulties with growing the large whiskers were encountered and rendered even more troublesome. Thus it appeared that the tremendous potentials once predicted with availability of whisker material were never achieved. This was primarily because production of the material was slow, discontinuous, unpredictable and the like, rendering production in commercial quantities impossible. The disadvantages of the prior art are overcome by the present invention, and an improved high temperature fluid wall reactor is hereinafter disclosed utilizing a perforated reactor tube. Also disclosed is an improved process for forming an effective fluid wall within a hightemperature reactor by forming a plurality of gas jets which overlap'to form the protective fluid wall but do not disturb flow within the reaction zone. Additionally, novel whisker-type fiberous material, reproducible methods and apparatus for producing same and improving yield and other fiber properties are disclosed. SUMMARY OF THE INVENTION A perforated reactor tube is provided for a hightemperature fluid-wall reactor. The reactor tube of the present invention permits an efficient transfer of heat from the heating elements through the reactor tube and to reactants passing through the tube. Inert gas passing through perforations in the tube enables the formation of an effective fluid wall to protect the interior surface of the tube from reactant chemical attack, and prevents reactant accumulation on the tube. The reactor tube of the invention preferably has a generally cylindrical shape and is made of a refractory aterial which permits the tube to be heated to incandescence. At least a length of the reactor tube is perforated to permit a gas which is substantally inert with respect to the tube material to pass through the tube to form a protective fluid wall between the tube and the inner reaction zone. Perforations are located, shaped and dimensioned such that inert gas jets comprise a portion of the fluid wall, with each gas jet having a substantially radial-directed momentum sufficient to repel the reactants. The gas jets overlap to form a continuous protective fluid wall, but do not disturb flow within the reaction zone. The reactor tube of the present invention may be fabricated from solid graphite, which can routinely withstand temperatures of 4500"F (2480eC), and can withstand temperatures of 5500"F (30400C) or even higher for shorter time periods. Solid graphite tubes may be fabricated relatively economically, with suitable perforations added at selected locations. The wall of the reactor tube is preferably made as thin as practical, consistent with the requirement that the reactor tube have sufficient mechanical strength to bear up under the operating conditions of the reactor. The increased thermal conductivity of a solid wall tube material compared to a porous wall tube material, in addition to the reduced thickness of the tube wall, substantially reduces the thermal impedence presented by the tube. The perforated reactor tube of the present invention thus more efficiently transfers heat from the electrodes of the reactor to reactants passing through the reactor tube. Refractory materials other than graphite may also be used t6 fabricate the reactor tube, provided the material retains sufficient structural integrity at the intended operating temperatures. According to one-embodiment of the present invention, a 4 ft. (1.2 m) long reactor tube having an internal diameter of 12.75 in. (324 coin) panda wall thickness of 1/4-in. (6 mm) is utilized. Perforations in the wall of the reactor tube are circular with a crosssectional diameter of .03 in. (.76 mm). The holes are located in a triangular lattice pattern with a spacing of .100 in. (2.54 mm) between hole centers. The perforations extend through the wall of the reactor tube in a direction substantially perpendicular to the wall. Approximately 120 scfm (3.4 scmm) of nitrogen is provided as the inert gas, and passes through the perforations creating a pressure differential of approximately 1 in. of water (2.5 gm./sq.cm,) at a reactor tube temperature of approximately 40000F (22000c). The diameter and spacing of the holes, the thickness of the wall, and the pressure differential cooperate to form a plurality of inert gas jets each having a substantial conical configuration, with the jet apex substantially adjacent the exit opening of the perforation. Although the gas dynamics of the fluid wall are not fully understood, especially because of the elevated temperatures, the momentum of each jetstream is believed to be sufficiently radially-directed to repel reactant particles. Moreover, the inert gas jets maintain such a momentum at sufficient distance from the perforation exits, so that the jets overlap creating an integral fluid wall. It is also believed, however, that the radially-directed velocity of the jets is minimal or non-existant before the jets engage the intended reaction zone, so that the jets do not disturb flow within the reaction zone. At the elevated temperatures previously noted, the injected inert gas achieves substantially laminar flow as the gas is swept downstream from the injection points. Laminar flow of the inert gas at a point downstream from the perforations enables the gas to maintain the desired fluid wall so that downstream perforations may be eliminated. At cooler temperatures, however, the gas is less reactive with the tube material. It may therefore be advantageous in certain cases for an upstream, and relatively cool, section of the reactor tube to be perforated while an adjacent downstream, and relatively hot, section of the reactor tube is unperforated. Also, successive sections of perforated and unperforated reactor tube may be provided in a single reactor, especially if the reactor zone is extremely long. The reactor tube of the present invention may be fabricated in sizes sufficient to enable commercial production operations requiring high-temperature chemical processes, e.g., the production of carbon black or the destruction of hazardous waste materials. The perforated reactor tube may be used to successfully maintain a suffi-cient inert gas fluid wall so that the reactants do not come into engagement with the inner surface of the tube. The solid construction of the reactor tube, and the use of perforated sections only in relatively cool zones, contribute to a markedly increased tube life compared to porous graphite tubes. Moreover, the process of injecting gas through the perforations in the solid tube according to the present invention requires subs tan- tially less inert gas than was previously utilized to achieve a fluid wall using a porous tube, thus lowering reactor operating costs. Moreover, the perforated tube of the present invention has a higher resistance to chemical attack than the porous construction tubes, thereby also contributing to longer reactor tube life. A novel cobweb whisker fiber and production method for same is further provided. In one embodiment of the invention, a feedstock comprised of 94.38 silicon dioxide sand1 5% carbon black, and 0.78 transformer oil are mixed until the sand particles are uniformly coated and the mixture is free flowing. The mixture is then introduced at the upper end of a high temperature reactor having a core temperature of 25000C (45000F) whereby the mixture free falls downward at a nominal flow rate of 2.7 kg/min (6 lbs/min) or more. The reactor core has a blanket of nitrogen gas passing through the core wall with a 3.4 m3/min (120 scfm) flow rate which shields the core from the finely divided feedstock as it vaporizes. The vaporized materials, residual feedstock and blanket gas then flow to a lower post reactor chamber having a temperature profile ranging from 1400"C (2600OF) at the top to 900"C (1600OF) at the bottom where the mixture is rapidly cooled, resulting in a supersaturated vapor. The mixture thence flows to a still lower cooled post reactor chamber having an inside wall temperature of 900C (2000F). After passing through this section, the gas stream and the majority of the novel fiber material formed by the process of the subject invention pass to a cyclone separator and bag filter. The majority of the fiber material of the present process is recovered from the gas stream. Heavier unreacted solids collect at a receptacle below the bottom chamber. The fiberous material of the present invention has been found and collected in the lower two chambers, separator output, the receptacle, and adjacent the feed tube wherein the feedstock enters the uppermost reactor chamber. The novel fiber material thereby recovered prior to postformation treatment is characterized by a predomnance of tightly bundled fibers comingled with a lesser quantity of individualized fibers. The fibers have been found to have a diameter substantially within the range of 2-50 nm with greater than 90S of the material often falling within this range. The bundles have been found to have a diameter substantially within the range of 500-5000 nm. After splitting the fiber bundles apart by mechanical means, individualized fiber lengths are substantially within the range of 10-2000 nm, with aspect ratios of 5:1 or greater. In one form of the invention, the remainîng soll3 cores seen after mechanical shearing indicate that many of the bundles have a substantially solid center. However, with respect to fiberous material produced in accordance with the methods and apparatus of the present invention, such solid cores are atypical with the material being substantially comprised of fibers. The aggregate fiber material is further characterized as being comprised of pure silicon and/or silicon oxide fibers in proportions varying from substantially 100g silicon to 100% silicon dioxide (so02). The term silicon oxide as used herein means SiOx with x being less than or equal to 2. A typical chemical composition has been found to be 55-60% silicon, 38-43% oxygen, and 1-4X carbon, with less than 1X other elements. In one form, individual fiber as initially formed is believed to be substantially silicon which may later either'partially oxidize to form a silicon core with a silicon dioxide coating or to more completely oxidize so as to be composed of silicon dioxide. The process of the present invention is characterized by forming novel whisker fiber material in a continuous free gas flow with rapid fiber formation time, a high reproducibility and yield, and uniform quality fiber material. Direct functional relation between reactor temperature and oil percentage in the feedstock versus yield has been determined, and the hereinabove described fiber material produced with a variety of feedstocks containing differing forms of silicon (e.g., sand, zircon sand, ground glass, soil, sand flour, pure silicon, silicon carbide, zeosyl (a precipitated silica), rice hulls, silicon monoxide, such as in the form of an unreacted sand with a substantial silicon monoxide content, or even a recycling of the fibrous material produced in accordance with the invention as the feedstock). In one embodiment, the feedstock is comprised of a source of silicon such as the aforementioned sand flour and a reductant which, in addition to the aforementioned methane, may be comprised of carbon black, carbon chloride, urea, rosin, hydrogen, silicon, and methyl silanes. A direct inverse functional relationship between the silica particle size and yield has been found. In a preferred embodiment, the feedstock is comprised of the aforementioned sand flour, rosin, and a gaseous reductant such as methane. Yields have been found to increase by use, either alone or in combination, of a substantially reduced feedstock particle size such as the aforementioned sand flour and the gaseous reductant, employed in the hereinbefore described manner, where yield is the fiber to feedstock ratio by weight. Yield and formation of more uniform fiber material with higher surface areas has been found to be a function of and thus controllable by the reaction temperature and the temperature differential between the reactor and the cooler post reaction chamber as well as the residence time of the fiber-forming material while within the hot zone of the reactor and post reactor chambers. From a properties or quality control standpoint, a water-cooled PRTy may be preferable since temperature would be more constant throughout the PRTZ and the production run. As noted, the temperature affects some properties such as its fiber diameter. These and other features and advantages of the present invention will become apparent from the following detailed description, wherein reference is made to the Figures in the accompanying drawings. IN THE DRAWINGS Figure 1 is a simplified pictorial view of one embodiment of a reactor assembly including the reactor tube of the present invention. Figure 2 is a pictorial view, partially in crosssection of a suitable high-temperature reactor section of the reactor assembly generally depicted in Figure 1. Figure 3 is a more detailed pictorial view of a suitable perforated reactor tube according to the present invention. Figure 4 is a cross-sectional view of a portion of the wali of a suitable reactor tube. Figures 5 and 6 are each simplified pictorial views of alternate embodiments of reactor tubes within suitable reaction chambers. Figure 7 is a transmission electron photomicrogram (TEM) of fiberous matrials of the present invention taken at a magnification of 104. Figure 8 is a TEM of the present invention taken at a magnification of 104. Figure 9 is a TEM of the present invention taken at a magnification of 105. Figure 10 is a TEM of the present invention taken at a magnification of 105. Figure 11 is a TEM of the present invention taken at a magnification of 105. Figures 12-15 are transmission electron photomicrographs of individualized fiberous material of the present invention. Figures 12 and 13 are TEMS of the present invention taken at a magnification of 104. Figures 14 and 15 are TEMS of the present invention at a magnification of 105. Figures 16 and 17 are spe-ctrograms of a representative sample of the fiberous material of the present invention. DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS Referring to Figure 1, a simplified view of high temperature reactor equipment is depicted, including a reactor section 10, a post reactor treatment section 12, and a water-cooled treatment section or heat exchanger 14. As described further below, reactor material (feedstock) and inert gas are (a) fed into the reactor housing 10, wherein the feedstock is heated to a high temperature to cause a desired chemical reaction, (b) passed downward into the insulated housing 12, wherein further decomposition of the reactant may occur, and (c) passed downward through heat exchanger 14, wherein the temperature of the gas and reactants are lowered for subsequent handling. For the present, it should be understood that numerous chemical reactions may be ideally suited for the apparatus herein described. The equipment shown in Figure 1 may be used commerically, for example, to generate carbon black from hydrocarbons or to decompose hazardous waste material. The reactor section 10 includes a generally cylindrical outer housing 16, a plurality of elongate heating electrodes 18 spaced inwardly of the housing 16, and a generally cylindrical reactor tube 20. The selected feed material may be input to the reactor by feed tube 22. The electrodes 18 generate radiant heat which is reflected inwardly by the housing 16, causing the reactor tube 20 to be heated to incandescence. Radiant heat from reactor tube 20 in turn radiates energy inwardly to sustain the desired chemical reaction within the reactor tube. Inert gas is input within housing 16 through ports 24, and passes through a plurality of apertures in the reactor tube to form an inert gas fluid wall or blanket 'Q6 on the inner surface of the reactor tube. The inert gas blanket thus encompasses the generally cylindrical-shaped reaction zone 29 within the reactor tube, with the interface 26 between the inert gas and the reactor zone shown representatively in Figure 1 by dashed lines. Referring briefly to the other equipment illustrated in Figure 1, the post reaction treatment section 12 includes a cylindrical insulated housing 30 which forms a PRTZ chamber 32. Employment of section 12 depends on the desired chemical reaction, and section 12 need not be provided in all cases. Basically, the PRTZ chamber 32 adds "residence time" to the products coming from the reactor section 10, so that further lower temperature decomposition of the gases may occur within the section 12. By way of example, the reactants may be heated to approximately 4000us to 4800"F (2430*C to 2650-C) within the reactor section 10, and may be maintained at a temperature of between 1800 CF to 3000 F (980at to 16500C) within the chamber 32. If desired, various gas ports 33 may be provided for injecting selected gases into the chamber 32. The reactants and gas are subsequently input to a water-cooled heat exchanger 14 confined within a cylindrical housing 35. Conventional heat exchanger tubes (not illustrated) may thus be provided within the chamber 34, with water inlet and outlet ports 36 connecting the heat exchanger tubes to water flow lines. (Alternatively, heat exchanger coils may be provided on the outside of the housing.) With reference to the exemplary temperatures listed above, gases and reactants from the chamber 32 may conventionally be lowered by the heat exchanger 14 to approximately 500"F to 1200"F (2600C to 650"C) for further handling. If desired, a gas exit port 38 may be provided from the housing 35, although more conventionally a gas exit port 44 may be provided from transition section 40. At the bottom of the transition section 40, a discharge control 42 may be provided for discharging solid material from the chamber 34, although no appreciable gas flow from control 42 occurs. The input gases as well as the readtion-generated gases are transmitted by conduit 46 to cyclone separator 48, which in turn separates the fine particles for discharge through port 50 and discharges gas to a bag filter (not depicted) for a final cleaning operation. It will be noted that as will be discussed, the fiber material thus produced may oxidize readily. Thus, in cases when it is desired to preserve the material in a non-oxidizing atmosphere, the fibers could be collected in a wet scrubber, in a resin or could be sprayed with a protective coating such as oil to prevent oxidization of the final product. Referring to Figure 2, a more detailed, although still highly simplified, pictorial view of the reactor section 10 is shown, partially in cross-section. Attached to the ends of cylindrical housing 16 are reduced diameter input cylindrical housing 53 and reduced diameter transition housing 54, each axially aligned with the axis of the housing 16. The housing 53 supports a water cooled, adjustable feed tube mechanism 56 which supplies feedstock for the desired chemical reaction. A suitable feed tube mechanism is described in detail in U.S. Serial No. 06/647,958, filed on September 5, 1984. The transition housing 54 provides both a physical and fluid connection between the reactor section 10 and the post reactor treatment section 12. A suitable packing material 58 may be provided between the tubular drip lip member 60 and the inner wall of the housing 53. Drip lip 60 may be fabricted from solid graphite, and serves both as an accumulation surfaces for melted solids and vapors which may condense within the housing 53, and a drip ring spaced from the reactor tube 20 so that melted solids and condensed liquids do not flow down onto the reactor tube. Electrical power for heating the reactor may be supplied through the power clamp connectors 62, which are connected to associated power feedthrough subassemblies 64. A plurality of elongate resistance electrodes 18 preferably are uniformly spaced about the interior of the housing 16, and each electrode may be physicall supported by and electrically connected at its ends to a suitable electrical connector 66. As previously noted, housing 16 reflects radiation inwardly, so that a substantial portion of the radiant energy from electrodes 18 is used to heat the perforated tube 20. More particularly, housing 16 includes a cylindrical shaped radiation shield 68, a cylindrical insulator layer 70, and a cooling jacket 72. The insulator layer 70 and cooling jacket 72 serve to prevent significgnt temperature increaees in the housing wall, and thereby maintain the structural integrity of the housing 16 and minimize housing warpage. A plurality of ports 74 secured to the housing 16 may be provided for attaching suitable sensing equipment to monitor conditions within the reactor. Figure 3 is a pictorial view of a suitable reactor tube 20 according to the present invention. Reactor tube 20 may be fabricated from a solid (non-porous) reactor material having a thermal conductivity in the range of 16 to 21 BTU/ft.-hr.-9F at 40000F (27.7 to 36.3 watts/meter C at 22000C), and a material strength of at least 2500 psi (176 ks/sq.cm.). Solid graphite tubes having an inner diameter of 12.75 in. (324 mm) and a wall thickness of 1/4 in. (6 mm) have been successfully employed. At room temperature, solid graphite has a material strength of approximately 5000 psi (351 kg/sq.cm.) compared to approximately 500 psi (35 kg/sq.cm.) for porous graphite, so that the structural integrity of the tube is substantially increased by using solid graphite. The perforations in the tube constitute only about 78 of the total tube area, so that the thermal conductivity of the perforated graphite tube is still approximately 19 BTU/ft,-hr.-OF af 4000"F (32.9 watts/ meters at 2200"C). This increase in thermal conductivity (approximately 3 to 5 times compared to a porous graphite) results in a significant increase in the temperature generated within the reaction zone. Further reduction in the thickness of the perforated graphite tube may be possible, although a significant advantage of the perforated tube 2C compared to the porous graphite tube is its substantially increased reactor life, and the tube life would probably be reduced if a thinner wall perforated tube were utilized. Also, tubes may be periodically removed from the reactor and cleaned (because of a buildup on the outside of the tube discussed subsequently), and much more care would be required when handling thinner wall tubes. Referring to reactor tube 20 depicted in Figure 3, the tube comprises sections 20A, 20B, and 20C, with each section being identical except for the perforations. In section 20A, the perforations 78 through -the tube wa'll are provided along circumferential lines 79A and along vertical columns 79B. (Although perforations would normally be uniformly provided around the periphery of the tube sections 20A and 20C, only portions of the tube are shown to be perforated for drawing clarity.) The holes 78 may be uniformly spaced from each other on the tube sections 20A so that the holes define lattice points of a triangular lattice pattern wrapped around the cylindrical tube. More particularly, holes 78 may be be cylindrical holes having a hole axis substantially aligned with the center line 76 of the tube 20. (The holes may be "gang drilled" in patterns 6 to 12 columns wide, so that the axis of each hole may not be directly in line with the center line 76.) The holes 78 may be spaced so that a uniform distance is provided between each of the rows 79A, which distance is approximately 1.55 times the uniform distance provided between each of the columns 79B nd the holes 78 are thus uniformly spaced from each other in a triangular lattice pattern. Tube section 20C includes cylindrical-shaped holes 80 similar to holes 78, except that holes 80 define lattice points of a rhomboid lattice pattern and are provided along circumferential lines 81A and along spiral columns 81B. The spiral or helical lines 81B may also be spaced at equal intervals, with a suitable pitch for the helical lines 81B resulting in hole 80A (spaced five or more rows above hole 80F) being directly vertical over hole 80F. Advantages of a triangular, rhomboid and square lattice pattern are discussed subsequently. For the present, however, it should be understood that exemplary cylindrical holes 78 and 80 may have a diameter of .030 in. (.76 mm) and may be spaced on the tube exterior surface at centerline spacings between holes of .100 in. (2.54 mm). Using an exemplary perforated tube having a 12.75 in. (324 mm) internal diameter (as previously described) which is 4 ft. (1.2 m) long and is perforated with holes having a diameter and spacing as described above and arranged in the configuration of holes 78 throughout the length of the tube, a suitable method for forming a fluid wall will be discussed. After the heating elements have radiated the tube 20 to its intended operating temperature, pressurized inert gas may be injected into the interior of the housing 16. Gases typically have a very low radiation absorption rate, so that the gas would not necessarily be heated to the temperature of the heating elements. A pressure differential of between 0.5 to 4 in. of water (1.3 to 10.1 gm/sq.cm.) may be created as the gas is passed through the perforations in the tube. This pressure differential preferably is sufficient to insure a uniform flow through the perforations in the tube, but is not so high as to cause unnecessary turbulence in the interior of the tube. Typically, gas may be injected into the tube described above at rates of between 40 to 240 scfm (1.1 to 6.8 scmm), and normally below 150 scfm (4.2 scmm). If desired, a low volume of sweep gas less than 20 scfm (.57 scmm), may be input into the top of the reactor through control valve 59 (see Figure 2). It is believed that flow in the tube perforations is laminar. Depending on the assumed temperature of the gas in the perforations and the gas flow rate, the exit velocity of the jet has been approximated at between 1 and 50 feet (.30 to 15.2 meters) per second. It is presently believed that the-jetstreams commencing--at the exit of the perforations are also laminar, although portions of these jetstreams could also be turbulent due, in part, to intermixing of jetstreams and cross-flow (axial flow) of gas injected upstream. Each inert gas jetstream is directed downward through the tube, as explained below. If the perforations in the tube are discontinued downstream, inert gas flow downstream of the perforations is believed to be substantially laminar. Thus, the combination of radially-directed gas jets and the subsequent axially moving inert gas form the desired fluid wall to enable the reaction process to occur without having reactants contact the interior surface of the tube. Tube sections may be from less than one foot to several feet in length, and perforations are normally uniformly provided substantially along the length of each perforated section and uniformly about the circumference of each perforated section. Typically, thousands of holes would be provided in a perforated tube section, and thus substantial costs may be incurred when manufacturing perforated tubes according to the present invention. The selection of a suitable hole diameter and hole spacing for the perforations will depend on the particular reaction process desired. If the perforated area per unit surface area remains constant, a decreased hole spacing will increase the number of holes and should theoretically provide a more uniform inert gas blanket. If the same flow rate of inert gas is utilized, however, a decrease in the hole diameter and hole spacing may increase the pressure differential across the tube, thereby raising the velocity of the inert gas jets. Also, a decreased hole spacing obviously increases the cost of manufacturing the reactor tube. A hole diameter of between 0.02 in. (.51 mm) to 0.20 in. (5.1 mm) should generally be satisfactory, with the uniform hole spacing of between .05 in. (1.3 mm) to .50 in. (12.7 mm). A hole size/hole spacing chart is listed below: Hole Diameter Hole Spacing Inches Inches ¯ ¯ Comments .02 - .035 .06 - .15 No reactant deposition on tube under various operating conditions. .05 - .07 .12 - .25 No reactant deposition on tube under many operating conditions. .08 - .10 .18 - .35 Little or no reactant deposition on tube under more controlled operating conditions. .12 - .20 .30 - .45 Probable upper limit for acceptable performance under conventional industrial operating conditions. Prom the above, it should be apparent that a reduced hole size and spacing is generally preferred, with machining costs being the primary motive for increased hole spacings. Also, the larger hole sizes and hole spacings may be more acceptable in perforated tube sections downstream from the feedstock input to the reaction zone. It may also be desirable to provide a cylindrical tube section 20B which is unperforated. Tube sections can be drilled and section ends either sealingly glued or machined to be fitted to unperforated tube sections, so that inert gas can pass into the interior of the tube only through the perforations provided. The inert gas forms a fluid wall between the reaction zone and the interior wall of the tube 20. A representative interface between the inert gas and the reaction zone is shown in Figure 1 by the dashed lines 28. Referring now to Figure 4, there is depicted a cross-section through a portion of a perforated tube provided with holes formed in a rectangular pattern. A tube wall having a wall thickness T of .25 in. (6 mm) has an exterior surface 82 and an interior surface 84. Circular perforations 90 having a diameter D of .03 in. are provided through the tube at a hole to hole center line spacing S of .100 inches. Inert gas flows through the perforations 90 and achieves fairly uniform flow within the perforations because of the D/T ratio. An inert gas jet 86 is formed commencing from the end of the opening 90, with the center line of adjacent lowër gas jets being designated as 86A-86E. The boundary layer 88 of each jet expands outwardly from the center line as the jet progresses from the interior surface 84, and thus each jet may be described as having a substantially conical configuration with the sidewalls of the cones (or the sidewalls of the jets) intersecting at some distance from the interior surface 84. After the jets intersect, a uniform fluid wall is thereafter established, and the jet velocity will continue to decrease as the jet moves further from the interior surface 84. Within the boundaries of a singular jetstream, the velocity of the gas at any point remains substantially constant, in both magnitude and direction, and there is no mixing of the gases within the jetstream on a macroscopic scale. Once the jetstreams shown in Figure 4 intersect, however, additional mixing or turbulence may occur, which further explains the 'difficulty in determining whether the jetstream is laminar or tubulent after jetatreams have intersected. In any event, the hole spacings are believed to be critical to the success of the present invention, and it is believed that the jetstreams maintain sufficient momentum at the point of intersection to form a uniform boundary layer sufficient to repel reactant particles. Inert gas injected above jet 86 as well as the downward flow of the reactants within the reaction zone in the interior of reactor tube 20 create a cross-flow generally perpendicular to the initial flow of jet 86 (the cross-flow direction being axial-with respect to the reactor tube 20). The center line 86A of jet 86 is therefore directed downwardly as shown in Figure 4 as the jet moves further from the interior wall 84; with the rate of downward change in the direction of jet 86 increasing as the radially-directed velocity of the jetstream is reduced and the jet is increasingly affected by the cross-flow. Since the actual pattern of the jetstreams is not known, the jet center line representations shown in Figure 4 should be understood to merely illustrate the functional concepts described herein. The gas streams should cooperate to repel reactant particles from engaging the inner wall 84 of the tube 20, and it is believed that this repulsion is made possible because each jet maintains a sufficient radially-directed momentum to repel reactant particles at least until the jetstream overlaps with other jetstreams. Once jetstreams having such momentum overlap, an effective continuous fluid wall is created. Thereafter, the radially-directed velocity of the jets will decrease and the inert gas ultimately will flow in an axial direction having no substantial radial component, as shown in Figure 4. It is also believed that the success of the present invention, in part, is due to the fact that the gas jets lose substantially all their radially directed velocity outside of the reaction zone. In other words, inert gas at or near the interface 28 with the reaction zone is not moving radially with respect to the center line of the tube 20, and therefore does not penetrate the reaction zone interiorly of interface 28 to disturb the fluid flow within the reaction zone. Also, it is believed that reactant gas flow within the reactor zone is substantially laminar, at least after a distance of several feet downstream from the feedstock injection, which enables the axially-moving inert gas to continue to act as an effective fluid wall downstream of the perforations. It should be apparent from the foregoing discussion that the various phenomenon contributing to the ability of the perforated tube of the present invention to successfully maintain a fluid wall sufficient to prevent reactants from contacting the inner surface of the tube is not fully understood. Theoretical gas dynamics concepts such as viscosity, laminar flow, and gas density and momentum are, of course, significantly altered by high temperatures. Also, empirical data is very difficult to obtain because of the elevated reaction temperatures previously discussed. The perforated tube described above achieves surprising and unexpected results, especially relating to its ability to form and maintain a fluid wall, and the above explanation for its success is presently believed to be valid. Figure 4 also illustrates perforation 92 having a larger diameter at the exterior wall 82. This increased diameter area 94 may be utilized to reduce frictional fluid losses at the entrance to perforation 92, and may also be desirable from a hole manufacturing standpoint if the wall thickness T exceeds .3 inches. The entrance of perforation 92 may also be cone-shaped or rounded to -further reduce frictional entrance losses and/or turbulence. Figure 4 also depicts downwardly angled cylindrical perforation 96. The axis of perforation 96, if extended, would intersect or pass closely to the center line 76 of tube 20, and in that respect perforation 96 is similar to perforations 90 or 92. The axis of cylindrical perforation 96 is projected downwardly (toward the fluid exit of tube 20) so that a jet commencing from perforation 96 is initially imparted with an axially directed velocity in the direction of the ultimate inert gas flow. This inclined jet concept has not been adequately tested to determine its effect, although it is believed that a plurality of downwardly injected jets may decrease turbulence within the tube and more readily enable the generation of an axially moving laminar fluid wall. It is also believed, however, that such downwardly inclined jets may have a detrimental influence on the ability of the jets to repel reactants, due to the reduction in the radially-directed momentum of the jetstreams. A preferred range of angles, if any, for the downwardly projected jets 96 therefore has yet to be determined. It has sometimes been observed that when the reactor is operating under conditions such that some reactive products contact the interior of the core (which condition would likely occur according to the teachings of the present invention only under abnormal operating conditions), vertical "paths" substantially corresponding to the width of the holes appear on the inner surface of the reactor tube 20 below each perforation. It ha also been observed that this "path" area below each hole may extend substantially beyond the spacing of the lower row of holes. This "path" effect is believed to be due to increased nitrogen flow over that portion of the tube surface1 which, in turn, may be due to the "wake" effect of the jet. In any event, this "path" is believed to be desirable especially under abnormal operating conditions, since interior surface tube material in this path remains substantially in its virgin state, while material between such paths experience a slight amount of degregation {microscopic builddown) over an extended period of time. An advantage of the spiral configuration of the holes 80 shown in Figure 3 is that the spiral offset allows the "path'1 inner tube surfaces to overlap, thus effectively obtaining a totally virgin-state inner surface of the tube rather than obtaining a "paths" along the vertical column 79B. In other words, an advantage of the spiral arrangement of the holes 80 as shown in Figure 3 is that the "path" below hole 80A may extend vertically downward five or more rows past hole 80F, and the elongate path under each of the holes thus overlaps to effectively provide a "virgin state" inner tube surface. Thus, it should be understood that regardless of the particular hole arrangement, an effective fluid wall should be formed according to the present invention to keep reactant products from contacting the tube interior wall under normal reactor operating conditions. Because of this "path" effect, the spiral hole arrangement may have advantages to minimize tube deterioration under abnormal operating conditions. As previously noted, extended life of the perforated reactor tube compared to porous-tubes is a significant feature of the present invention, and the drilled tube should be able to structurally withstand compressive forces on the tube when operating at high temperature for extended periods of time. It has been determined that the entrance openings for the perforations may tend to increase with a conical configuration as the tube life increases. This conical increase or erosion of the entrance areas of the perforations is generally symmetrical with respect to the center line of each perforation, and after a relatively long period of time, the erosion of the outer wall adjacent- the opening of each hole effectively decreases the compressive strength of the tube, the tube strength being effectively determined by the strength of the "columns" of core material between the columns of holes. These tube material columns are spaced between corresponding holes are thus truly vertical for a square or rectangular hole pattern, but would be spiralled for the hole pattern of holes 80. Since a strictly vertical column can support much more weight before failing than columns spiralling about a center line, a square or rectangular lattice pattern is preferably over the arrangement of the holes 80 to minimize the likelihood of tube structural failure over a long operating period. A triangular hole pattern offers increased "cleaned path" surfaces compared to a square hole pattern, while still retaining narrower vertical outer wall columns between holes. A hexagonal or outer hole pattern may also be used, depending on the desired tradeoff between reactor tube strength and the efficiency of the hole pattern in forming and maintaining a fluid wall. As indicated above, it may be desirable to include both a solid (non-porous) and unperforated section of the tube within the reaction zone. A perforated section of the tube may be essential in the vicinity where the feedstock is input into the reactor. At this input location, individual particles of reactant material and reaction-created gas molecules may have a substantial radial as well as axial velocity, due to the intensity of the chemical reactions and the creation of new reaction gases. This supposedly turbulent condition results in reaction particles in the range of up to approximately 0.5 mm being thrust with a radially-directed velocity toward the reactor tube, and these particles are repelled from contacting the inner surface of the reactor tube by the opposing radially-directed momentum of the overlapping jets. Several feet downstream from the feed material injection locations, however, the individual reactor particles and reaction gas molecules within the reaction zone will necessarily have achieved substantially axially movement with respect to the tube. It has been determined that although radially-directed inert gas jets may be necessary in the region adjacent the feed input, the injected inert gas flowing downstream continues to maintain a fluid wall blanket. This axially moving fluid wall creates a sufficient barrier to prohibit the inner axially moving reaction gases and reactant particles from coming into engagement with an unperforated tube wall section. Moreover, this axially moving inert gas can create an effective fluid wall under these conditions over a distance of at least several feet. The flow of the inert gas downstream of the jets and the flow of reaction gases at this location are thus considered laminar. Figure 5 illustrates a simplified cross-sectional view of a reactor chamber including a modified reactor tube. (In both Figures 5 and 6, the holes shown are intended simply to illustrate a perforated tube, and the hole spacings are not in proper proportion to the reactor tube.) The reactor includes the cylindrical housing 16 for the heating elements 18, as previously discussed. The feed tube 22 terminates within the upper housing 53, and the lower housing 54 provides a transition to the downstream equipment. The reactor tube shown in Figure 5 comprises three separate reactor tube sections: a perforated tube section 102 extending from the top of the tube until about the middle of' the housing 16, a solid and unperforated tube section 104 extending from tube 102 to position adjacent the lower end of the large cylindrical housing 16, and a perforated tube section 106 extending from the tube 104 to the lower end of the reactor tube. Each of these tube sections is axially aligned and may be sealingly joined by conventional means. Inert gas may be injected through one or more of the ports 110 for passing inert gas through the perforations in section 102 to form the desired fluid wall comprising a plurality of radially projecting jets in the vicinity of the feedstock input. By the time the feed material and reactor gases reach the middle of the housing 16, the reactor material and gases within the reaction zone should be moving substantially axially with respect to the axis of the tube. An unperforated tube section 104 of several feet or more in length may thus be provided, with the fluid wall being maintained by the laminar axially moving inert gas flow, as described above. Within cylinder 54 adjacent the exit of the reactor section, turbulence within the reactor tube may be increasing, and the fluid wall may begin to break-down. Accordingly, another perforated section of reactor tube 106 is provided to insure that the reactant particles do not come into engagement with the lower end of the reaction tube. It has been further observed that material may eventually accumulate on the outer surface of the reactor tube as the reactor is operated over a long period of time, especially in a relatively cooler zones of the reaction chamber. It is believed that this buildup of material is at least partially caused by condensation of carbon or graphite vapors formed outside of the reactor tube in the hot zone adjacent the heating elements. This vapor cools and condenses when entering a cooler zone, and may thus build up on the outside of the reactor tube, thereby possibly plugging some of the perforated holes. Accordingly, it may be necessary to periodically clean the outer wall of the perforated sections of the reactor tube to remove this buildup. To reduce the above buildup on the outside of the reactor tube, inert gas may be input into the reactor only in the vicinity of the perforated tube sections. To further reduce or eliminate the buildup, inert gas may be input into a chamber in fluid communication with the perforations in a perforated section of the tube, but sealed from the adjacent unperforated sections of the tube. An unperforated section of the tube is preferably provided in a hot zone, since this is the zone which would otherwise most likely experience tube failure due to the extended temperatures and corrosion of the outer wall. Accordingly, it may be desirable under certain conditions to inject inert gas only in the vicinity of the cool perforated tube sections, or to isolate the exterior of the unperforated hot-zone tube section from the exterior of the perforated cool-rzone tube section,, thereby reducing the buildup on the outside of the perforated tube section. Referring again to Figure 5, inert gas may thus be injected through ports 110 in housings 53 and 54, while port 110 in housing 16 is sealed. The closing of port 110 in housing 16 should reduce the buildup on the outside of perforated tube sections 102 and 106, since the injected gas need not pass by the elements 18 before entering the perforations in the tube. Referring to Figure 6, another reactor is shown, with a reactor tube comprising alternating perforated and unperforated sections 114, 116, 118, 120, 122, and 123. Each of the perforated sections is sealed outwardly from the unperforated sections by graphite packing rings 125 and/or other horizontal barrier layers. Thus, the perforated section 114 is sealed from the chamber outside of the unperforated section 116 containing the heating elements 18. Similarly, perforated section 118 is sealed from adjacent unperforated sections by horizontal barriers 128 and 130. Each of the perforated sections shown in Figure 6 is provided with its own inert gas input 110. Accordingly, inert gas entering the reactor tube need not be in fluid communication with the hot portion outside the unperforated section of the tube adjacent the heating elements 18. As previously indicated, the fluid dynamics of the inert gas will largely depend on the gas temperature. In the embodiment shown in Figure 6, the inert gas may not be as hot as the gas passing through the tube of the embodiment shown in Figure 5. In order to maintain the desired inert gas characteristics, the inert gas provided to the perforated sections of the tube shown in Figure 6 may be preheated by conventional means. Figure 6 illustrates that a short perforated tube section 118 may be provided between an otherwise elongate hot zone. Laminar flow of inert gas within the unperforated section 116 may begin to break down, and perforated tube section 118 is provided to reestablish a strong fluid wall and again commence uniform laminar flow of the inert gas adjacent the interior of the unperforated section 120. Figure 6 also illustrates that unperforated sections of the reactor tube may be provided in the area generally adjacent the heating elements, while perforated tube sections are provided in the relatively cool reactor zones. Finally, restricting the flow of inert gas from the heating elements 18 as shown in Figure 6 may extend the life of the heating elements, although additional life from the elements 18 may also be obtained by using another inert gas, such as argon. To further maximize the efficiency of the fluid wall formed within the perforated reactor tube, it may be desirable to provide perforated tube sections wherein the hole size, hole spacing, and hole orientation vary depending upon the intended placement of the tube section relative to the feedstock input location and the heating and cooling zones. As an example, perforations in sections 118 and 122 may be angled downwardly, as previously described, to achieve a uniform downstream laminar fluid wall without generating a strictly radiallydirected pattern of jets, since fluid gas and reactants entering these zones should be moving substantially in the axial direction. Similarly, it may be possible to increase the hole spacing in sections 118 and 122 or reduce the gas flow rate per unit area for these tube sections compared with the hole spacing and gas flow rate used for section 114. It may be feasible to replace unperforated tube sections with sections having large diameter perforations at very large spacings, and to substantially reduce the gas flow per unit area to such a tube section. The gas passing through such large perforations may act primarily to enhance uniform laminar flow, and overlapping of gas jets having a substantially radially-directed momentum would not be obtained. It should be apparent that the embodiments herein described achieve numerous advantages over reactors utilizing porous tubes as described in'U.S. Patent 4,044,117. The perforated tube allows for a much stronger fluid wall to repel reactants than was obtained using the porous tube. The perforated tube of the present invention requires much less inert gas than the porous tube, thus both reducing reactor operating costs and allowing the downsizing of gas purification equipment. The increased thermal conductivity of the reactor tube compared to porous reactor tube results in a higher reaction temperature and therefore increases the reactor efficiency. Compared to porous reactor tubes, the perforated reactor tube of the present invention has a relatively high resistance to chemical attack due to its non-porous nature, and is much stronger than a porous reactor tube, as previously explained. It is therefore believed that the perforated tube may typically have a reactor life of at least fifty times the life of a porous tube. The present invention thus makes feasible the commercial operation of a reactor utilizing a perforated tube diameter of from 14 to 60 inches. Such a reactor may, for example, be used to commercially produce carbon black, to gasify coal by pyrolysis, to decompose hazardous waste materials, to thermally crack petroleum products, or to reduce oxides of inorganic compounds in the presence of hydrogen. Numerous other possible uses for the high temperature fluid wall reactor are disclosed in U.S. Patent 4,044,117, which are incorporated herein by reference. In another embodiment of the invention, .03 inch (.70 mm) diameter holes are provided in a drilled section of a 12.75 inch (324 mm) ID, 14.75 inch (354 mm) OD core, at .1 inch (2.54 mm) hole spacings. A 13 foot (4.0 m) long cylindrical core has at least 3 feet (.91 m), and preferably at least 4 feet (1.2 m), of total drilled core sections, with approximately 6 feet (1.8 m) of the core heated directly and an additional 2 to 4 feet (.6 to 1.2 m) heated by radiation spillage. In order to produce an effective inert gas blanket, the holes are preferably drilled perpendicular to the core axis, rather than at an inclined angle. Two 2 foot (.61 m) sections of drilled core, each at least substantially in or adjacent the "cool" zone of the reactor, are separated by a 6 foot (1.82 m) solid core section in the hot zone. The drilled core sections may be isolated from the electrodes in the manner as shown in Figure 6. In the above embodiment, a PRTZ section approximately 5 feet (1.5 m) diameter and 20 feet (6.1 m) long may be. utilized. This post reactor treatment section need not necessarily be insulated. The PRTZ section may be cooled on the outside, irrespective of whether insulating material (e.g., insulating brick) is or is not utilized. Alternatively, the PRTZ section may be cooled by a simple water-cooled tank internal to the shell, as previously described, and again insulating material may or may ndt be utilized depending on the desired reaction and preferred temperature gradient within the PRTZ section. The above-described reactor core may be used in the destruction of soil contaminated with hazardous waste. Between 3.0 and 12.0 scfm (.09 to .33 scmm) and preferably between 4.5 to 9.7 scfm (.13 to .27 scmm) of nitrogen per square foot (.093 square meters) of drilled core area is utilized to form an effective blanket. Injection of inert gas rates greater than that necessary to form a blanket may cause increased turbulence in the core and therefore decrease core life and reactor efficiency. In order to minimize hole plugging on the outside of the drilled core sections and to provide an effective blanket of inert gas, nitrogen is preferably heated to at least 800"F (427"C). Preferably a high purity inert gas is utilized to decrease core degradation; nitrogen with less than 1 part per million oxygen and water may be produced by conventional equipment, or may be commercially purchased. Excess hydrogen in the nitrogen may decrease core life, especially if the drilled core sections are positioned in the hot section of the reactor. A relatively "tight" soil column in the reactor may be obtained inputting as much as 40 pounds (640 kg) of soil per minute into the reactor (freefalling), and injecting approximately 200 scfh (5.7 scmh) of nitrogen in the feed tube area to stabilize soil flow. The injection of a low-volume nitrogen gas with the feed material results in the velocity of the gas about the feed material approximating the feed material velocity, thereby reducing aspirating gases and decreasing turbulences. Injection of too much gas in the feed tube area may tend to blast soil particles toward the reactor wall, and may therefore be dangerous to core life and/or decrease the effectiveness of the desired reaction within the core. Even though the nitrogen may be preheated to 800at or more, placement of the drilled core sections in the relatively "cool" zone of the reactor may substantially decrease the ability. to form an effective blanket. It should therefore be understood that, depending on the nature of the chemical reaction intended, it may nevertheless be beneficial to place the drilled core sections in the "hot" zones of the reactor adjacent the cool zones, rather than in the cool zones themselves. Although this modification may increase core degradation, the benefit of a more effective blanket of inert gas may be obtained. Also, it is believed that the maximum practical length of solid core section (no drilled holes) may be approximately 6 feet (1.8 m) while still maintaining an effective blanket of inert gas, and accordingly, placement of the drilled core sections toward but not in the cool zones may decrease the need for any drilled core sections toward the middle of the hot zone. It should be understood tha modifications to any reactor described herein may be necessary depending on the intended.reaction. For example, in some reactors, a "tight" input material column may not be desirable from the standpoint of the reaction efficiency, but generally may be desirable from the standpoint of core life A trade-off of relevant considerations will thus be necessary. It is believed, however, that the central concepts described herein relating to the formation of a drilled core reactor and the injection of an inert gas with a radially directed momentum sufficient to repel reaction particles in the vicinity of the drilled core, followed by laminar flow of inert gas in an axial direction to maintain an effective fluid wall, remain valid concepts for the apparatus and methods of the present invention. It is also within the concept of the present invention to utilize inductive heating rather than resistance heating. Thus, the electrodes described herein could be replaced with inductive heaters, which would similarily radiate energy to the reactor tube, which in turn would radiate the reaction zone to sustain the desired chemical reaction. Large inductive heaters are commercially available, so that the commercial scale-up of such a reactor is feasible. The use of inductive heaters compared to resistance heaters may also increase the heat transfer efficiency to the feedstock, and may eliminate some difficulties associated with the use of resistance electrodes operating within high temperatures environments. The reactor tube of the present invention is thus particularly useful for a high-temperature fluid wall reactor wherein the reaction zone spaced within the interior of the tube is substantially heated by radiant energy. In many instances, this radiant energy is absorbed by the reactant itself, which raises the temperature within the reaction zone so that reaction gases within the reaction zone (having a relatively low radiation absorption coefficient) are heated by both convention and radiation. U.S. Patent 4,044,117 teaches that if the reactant itself does not exhibit a high radiation absorption rate, a "target material" may be added to the reaction zone to raise the temperature in the reaction zone. The tube of the present invention is well suited for radiation coupling type reactors, wherein radiation heaters rad-iate a tube which in turn radiates a radially inward reaction zone. Alternatively, a tube material having a very low radiation absorption coefficient may be used, so that radiation from heaters passes through the tube, and the reaction zone is thus radiantly heated directly by the heaters exterior to the tube. Any number of high quality graphite materials may be used for the core. Suitable core materials are Stackpole 2020 or Stackpole 2191, each a fine grain graphite material commercially available from Stackpole Corporation in st. Marys, Pennsylvania. This core material may be purified by a vacuum of gasing, or *F" purifying Processes, both standard techniques in graphite technology, which reduce impurities in the material and increase core life. Vacuum out gasing may typically reduce iron content in the drilled core from 600 to 50 parts per million, and similarly reduce calcium from 200 to 20 parts per million and silicon from 300 to 30 parts per million. Another carbon/carbon composition material is available from Carbon Carbon Advance Technologies, Inc. in Fort Worth, Texas. This material, made from mats of graphite cloth impregnated with carbon resin which is then graphitized, is stronger than Stackpole 2020, and should therefore experience less degradation and have a longer life. The use of high quality graphite core materials, coupled with commercially available graphite purification techniques and due care to minimize reactor leaks, wubstan- tially reduces core degradation and therefore increases core life. Due to substantially increased thermal conductivity over porous core materials, as previously mentioned, a 1 inch (2.5 cm) core wall thickness may be utilized with the above high quality materials and purification techniques to obtain substantially increased core life. Also, this higher quality, stronger, and thicker core material may withstand higher maximum pressure differentials, in the range of from 10 to 15 inches (25.2 to 37.9 gm./sq. cm) of water. For the embodiment described above, increases in pressure above this range result from substantial hole plugging, and thus the decreasing effectiveness of the blanket and/or the possibility of core collapse necessitate cleaning. Since the above techniques substantially reduce core degradation, the benefits of long cleaned "paths" on the inner surface of the core are minimized, and accordingly the advantages using a spiral "offset" drilled hole arrangement are not as significant, although this arrangement is still generally preferable. These techniques have not, howvever, aso reduced the likelihood of drilled hole plugging either on the outside surface of the drilled core (if positioned in the cool zone), or on the inside of the drill core (if positioned in the hot zone). This hole plugging is believed to be attributable to condensation of vaporized electrode material on the somewhat "cooler" core surface. As holes plug, the pressure differential may increase to the range previously noted and, if the differential rises above that range, the reactor may have to be shut down and the core cleaned. Minimizing such hole plugging may be obtained by isolating the drilled holes from gases in fluid communication with the electrodes (although an effective blanket must still be maintained), by using higher quality electrodes witn less impurities to decrease vapprization, or by increasing electrode surface areas to decrease heat flux through the electrode cross-section. Electrodes fabricated from and purified by the techniques described above with respect to cores may therefore minimize hole plugging. The reactor tube may be fabricated from graphite, as described above, although many other refractory materials may be used. Examples of other suitable reactor tube materials include carbon, silicon carbide, boron nitride, and silicon nitride. The reactor tube material may in turn determine the preferred technique for perforating the tube. Conventional rotary drilling has been utilized for graphite tubes, although both ultrasonic drilling and laser drilling have also been successfully employed. If laser drilling is employed, perforations may be frustro-conically shaped rather than cylindrical, but this should not retract from the ability of the perforated tube to generate a protective fluid wall. Various gases other than nitrogen and argon may be used. The selected inert fluid should be substantially transparent to radiation, and should also be substantially inert with respect to the reactor tube material at various temperatures. Other suitable inert gases include hydrogen, helium, and xenon. With regard to the feedstock material for forming the fiber aterial of the present invention, although such feedstock described in example 2, for example, has been found typically suitable, several other ¯orm,ulations have also been successful. These include differing types or inorganic material such as sand, ground glass, soil, and zircon as a source of silicon, and differing types of oil and carbon blacks, > .alogenated organics, and propane as a source of carbon to enhance the reaction. As aforementioned, carbon black is not considered essential to Lne reaction or production of the fiberous material of the present Invention, with other reductants also being employed such as hydrogen, silicon, and hydrocarbons such as methane, propane, or the like. Moreover, various hydrocarbon silanes, as aforementioned, may also be effectively employed not only to reduce the silica feedstock to silicon tacnoxide as a reductant, but also to provide additional silicon to the reaction to enhance fiberous material yields over the theoretical maximum which employs only silica as a silicon source in the reaction. Initially, varipus forms of sand and soil were mixed with oil and/or ZEOSYLe from the J. M. Huber Corporation, Havre de Grace, Maryland (forms of silicon dioxide wIth very fine particle size) and sometimes with hexachlorobenzene or carbon tetrachloride and the fibrous material was produced. Thereafter, nblack" sand-(e.g., sand, carbon black, and oil) ws employed, and again formation of the fiber material was detected. From these and various other experimental runs, it was determined that a silicon form of the fiber material of the present invention could be formed with feedstock comprised of a variety of forms. It has appeared that some forms of silicon such as silicon dioxide (silica) and some form of carbon are important Sn the feedstock, inasmuch as pure forms of silica without carbon did not appear to form significant amounts of fiber material. However, the amount of carbon present in the feedstock was not seen to be critical to operation of the process. Addition of some form of oil to the silicon and carbon, however, was found to significantly increase production of the fiber material. In the preparation of the typical feedstock, the silicon source (such as sand), the carbon and the oil are mixed until all the sand particles are uniformly coated with oil and carbon and the mixture is free flowing. The mixture is then poured into the feed tube in a manner so as to evenly disburse it, whereupon it free-falls through core 211, which is protected by. the inert gas blanket (such as nitrogen). Thereafter, the vaporized feedstock passes to the PRTZ 32 from the core. With respect to preparation of a preferred form of the feedstock wherein the aforementioned sand flour source of silicon and methane gas as the form of reductant are employed, the sand flour feedstock may be introduced at feed rates between 1-6 pounds per minute into the previously described feed tube along with methane at a rate of 100-1100 standard cubic feet per hour. It will be appreciated that the methane may in some applications be in the form of a strip gas if desired which may only have a composition of 80% methane or the like. The methane and sand flour are thus mixed together in the feed tube before entering the reactor core, with the methane serving not only as a reductant but as a dispersement for the sand flour particles. It will be appreciated that during decomposition of the methane, relatively large volumes of hydrogen are produced thus serving to further disperse the silica particles. It has been found that in utilizing the aforementioned sand flour/methane feedstock fn the hereindescribed process, yields of- fiberous material have ranged between 20-70% by weight, and when appropriate ratios of the sand flour feedstock and methane are employed as hereinafter described in the following examples, substantially all of the sand flour is believed to react into silicon monoxide and thence into the.desired fiberous materials. A few additional aspects of the process of the present invention should be mentioned at this point. As previously noted, it has been found that the desired fiber material product may be recovered primarily in the bag filter, with lesser amounts being found in the various solid discharges co-mingled with greater amounts of unreacted solids. However, it has also been observed that the material collects and fs recoverable in pre-reactor portions of the equipment such as in the inlet area about feed tube 22. Additionally, such material has been found formed in other post reactor areas as well, such as internally of the PRTZ vessels 12 and 32 in layers as much as 1/16th to 1/4th inch in thickness. It has also been observed as indicated In Example 1 which follows that yield of the material increases with reaction temperature up to 2500"C or so. However, it will be appreciated that even higher reaction chamber 10 temperatures are expected as being even more favorable with respect to increased fiber yields, and thus the process is not intended to be limited to the aforementioned 25000C temperature. With respect to alternate embodiments of the apparatus of the present invention, as aforementioned, the PRTZ 34 may be of varying diameters, water-cooled on the outside, and the upper PRTZ may further include insulation such as insulating bricks on the inside. It has been found that the average temperatures in the PRTZ 34 were highest in a first embodiment when a smaller diameter wate-cooled insulated PRTZ 34 was employed; next highest in a second embodiment when a larger (5 foot diameter) PRTZ 34 with insulated brick and water-cooling on the outside was employed; and "coolest" in a third embodiment when the latter second embodiment was employed without the insulated brick. However, fiber yields were greatest with respect to the second embodiment and accordingly for most applications this embodiment is thought to be preferred from a yield standpoint. The next-most preferred embodiment is presently thought to be the third embodiment which exhibited higher yields than that of the first described smaller diameter PRTZ. With respect to the second embodiment, the temperature at the PRTZ--top, middle, and bottom ranged, respectively, from 1700-2500eF, 1400 1500OF, and 900-1400eF. With respect to the third embodiment, these same ranges were, respectively, 1200-1500eF, 600-1000"F, and 5OO-7O0F, based on runs using a standard mix feedstock such as &num;5 sand with carbon black and oil at approximately a 5 pound/min. feed rate. As process conditions change (as, for example, by variations in the nitrogen or feedstock rates or the reactor temperature, it is believed that the location at which the fiberous material is initially formed varies in functional relation thereto). It is further believed that this is due to a change in temperature profile as well as differences in the saturation of the vapor phase silicon monoxide and other vapors in the reaction. It is accordingly a feature of the invention to vary the location and/or temperature within the apparatus at which the fiberous material initially forms in a manner so as to intentionally affect the fiber diameter and other properties as hereinafter described. As but one example, it is believed that upon more rapid quenching of the vapors exiting the reactor and entering the PRTZ, the fiber diameters will be correspondingly smaller than if the vapors are quenched at a less rapid rate and, moreover, the surface area of the fibers will be correspondingly higher. As illustrative of this, in runs wherein the PRTZ 34 was insulated or wherein a water-cooling quench tower was employed, the average surface area of the fiberous material was in the range of approximately 35-50 m2/gm. However, when the insulation was removed from the PRTZ or, in the alternative, the aforementioned insulated brick was removed, BET surface areas on the order of 80 m2/gm were produced. In like manner, process changes which tended to increase the internal temperatures of the PRTZ, such as employing a finer particle size feedstock which absorbs relatively more radiation and results in a higher gas temperature have tended to lower BET surface areas to as low as 13 m2/gm. In order for the carbon or other reductant to produce the silicon dioxide, it is believed to be desireable to provide for an intimate contact between the materials. Accordingly, It has further been found that the mixing of the feedstock such as silicon dioxide with a melted rosin has improved this contact and thus improved yields. To further enhance this contact1 providing a gaseous reductant such as methane rather than carbon black has been found to further Improve yield, particularly when a finer'feedstock with increased surface area for such contact (such as sandflour rather than a number 5 sand) Is alsoemployed. Accordingly, it has thus been found that increasing the surface area between the silicon source and reductant in order to enhance mixing, such as by providing the aforementioned methane gas as a reductant and a finer particle size silica encourages the decomposition reaction of silicon dioxide and increases the fiber material yield. Initially, various forms of sand and soil were mixed with oil and/or Zeosil or Hysil (forms of silicon dioxide with very fine particle size) and sometimes with hexachlorobenzene and the fibrous material was produced. Thereafter, "black" sand (e.g., sand, carbon black, and oil) was employed, and again formation of the fiber material was detected. From these and various other experimental runs, it was determined that a silicon form of the fiber material of the present invention could be formed with feedstock comprised of a variety of forms. It has appeared that some form of silicon such as silicon dioxide and some form of carbon are important in the feedstock, inasmuch as pure fores of silicon without carbon did not appear to form significant amounts of fiber material. Properties of the Fiberous Material It will be understood that some of the physical and chemical properties of the fiber material produced by the present invention may vary dependent upon several factors herein described, such as the composition of the feedstock, feed rate, reactor chamber temperature, and the like. However, several characteristics have been found to be common to the various forms of the novel fiber material which will first be discussed hereinafter in more detail. Figures 7-11 are transmission electron photomicrographs (TEMS) of representative samples of the novel fiber material without individualizing at various indicated magnifications. With reference to Figure 7 first, one form of the novel fiber material produced in accordance with the process of the present invention and collected, for example, in the described bag filter generally may be seen to be of a composite form. More particularly, the material is found to comprise a predominance of rather tightly nested or intertwined bundles of fibers together with a lesser amount of individual fibers, e.g., fibers which exist independently in a non-bundled form relative to the other fibers. Representative bundles of fibers may be seen indicated in Figure 7 by reference numbers 280 and 281, respectively. Several individual fibers may be seen in Figure 8 as indicated by reference numbers 282 and 283, respectively. It will also be noted in Figure 8, reference number 284 that at times these bundles have been observed to be hooked or Intertwined together into larger clumps. The bundles of fiber have been found to have diameters substantially within the range of between 500 tit 5000 nm. With respect to the diameters of each individual fiber, whether in the bundled (which are more clearly seen in Figures 9-11) or non-bundled (Figures 12-15) form, it has further been determined that such fibers have diameters substantially within the range of between 2 to 50 nm. In some instances 90% or more of the material as collected from the reactor prior to any further processing thereof exhibits these diameter ranges. Reference to the representative fiber samples pictured In Figure 7 indicates how tightly interwoven and densiffed the fiber material of the present invention can be in bundled form. Measurement of fiber length has been found difficult in some cases due to this phenomenon of fiber bundling as well as the predominance of such bundled fibers over individualized fibers when the material is first collected from the reactor apparatus at various locations previously described. However, various processes have been found for separating fibers comprising the bundles into individualized fibers, representative such processes being ball milled and 3-roll milling, both of which are well known in the art for use with other materials. Yet an additional process has been found, however, which has been particularly successful In achieving a breaking off of fibers from the bundles. In accordance with this method, the bundled fibers are introduced slowly into a liquid epoxy base. A TEKMAR homogenizer with speeds up to 10,000 rpm is used to mix and to shear the fibers away from the bundle cores. Addition of fibers continues until the epoxy mixture becomes very viscous. More shearing action takes place than crushing or grinding which results in longer fibers. Other similar methods have been tested with solvents, such as water, and instruments which can impart shearing action on the solvents fiber mixtures such as colloidal mills. Individualized fibers have resulted from each of these processes. Figures 12-15 are TEMS of the fiberous material subjected to homogenization as described above to individualize or separate the fibers from the bundles, with the TEMS in Figures 14 and 15 being at a magnification 10 times that of Figures 12 and 13. From an analysis of such TEMS, it has been determined that the lengths of such individualized fibers are substantially in the range of between 10 to 2000 nm. Prior to employing any process for breaking off fibers from the bundl-es, the lengths cannot easily be determined accurately since fiber ends are difficult to find. One problem encountered in seeking to separate fiber bundles into individualized fibers is that, with some processes (e.g., ball milling) for doing so, many individualized fibers may be broken into very short lengths with aspect ratios (e.g., the ratio of fiber length to diameter) of less than 5:1. These shorter aspect ratios have been found detrimental in some applications relating to the fibers' properties as a reinforcing material In plastic matrices and the like. It has been suggested that a preferred aspect ratio for a reinforcing short fiber would be less than 100:1 to avoid difficulties incorporating the fibers into the matrix. A more preferred aspect ratio would be approximately 20:1. However, it has nevertheless been further discovered that with respect to the aspect ratio of individualized fibers produced in accordance with the process herein disclosed, the aspect ratio of such individualized fibers has been found to be substantially within the range of between 5:1 to 40:1. After the individual fibers are removed from the bundle, a solid core 285 may be seen in Figures 12 and 13. This remnant core is further indication that some of the bundles have substantially solid interiors. As aforementioned, it will however be recalled that presence of the cores 285 are generally considered to be atypical. With respect to the chemical properties of the fiberous materials produced in accordance with the processes of the present invention, the material appears to be comprised of substantially two elements: silicon and oxygen. The relative percentages of each have been found to vary from process run to run, although a mixture of both is typical for such material when exposed to air. However, it is believed that the material may be varied in composition from substantially 100X silicon to substantially 100X silicon dioxide. Chemical analysis of various fiber material samples from different process runs conducted under differing methods, including x-ray defraction, wet chemical, and neutron activation tests, have revealed that a typical chemical composition of the aggregate fiber material from a process run prior to any post-formation treatment, is as follows: : Silicon 55-60% Oxygen 38-43X Carbon 1-4% Trace Elements Less Than lX (Nitrogen, Iron, Potassium, Chlorine, Zinc, Manganese, Nickel, Copper, Calcium, Potassium, Sodium.) It is believed that a single fiber of the present invention, whether in individualized or bundled form, may exist either as pure silicon and/or silicon monoxide in crystalline form, as such crystalline silicon and/or sili-con monoxide with a silicon dioxide outer coating, or in the form of non-crystalline, e.g., amorphous silicon dioxide and that an aggregate of such fibers may include fibers of each type. Referring now to 15 288 Figure tS, there may be seen certain individual fibersS2t which clearly show a darker core. The distinct line 289 suggests a core of crystalline material surrounded by an amorphous coating. By the nature of crystalline structure, crystalline material under proper orientation will appear darker than amorphous material of equal thickness in a transmission electron micrograph. With respect to these cores of crystalline material as represented by line 289, it is believed that substantially all of the fibers of the material of the present invention include such cores or veins comprised of a crystalline silicon surrounded by a sheath of amorphous silicon dioxide. It will be appreciated that under electron microscope examination, a crystalline material will appear with varying degrees of intensity dependent upon the crystal orientation with respect to the electron beam. Accordingly, in photomicrograms not all such fibers will appear to have the aforementioned crystalline veins or centers, although, as aforementioned, substantially all such fibers are believed to have these crystalline centers. Also, as aforementioned, it is believed that at least some of the smaller fibers oxidize completely throughout to the core, resulting in a fiber which is substantially 100% silicon dioxide. Moreover, it Is further believed that a portion of the fibers form as substantially 100% silicon, only later oxidizing on the outer surface thereof when exposed to an oxidizing source such as air. It is presently believed that when the fiber material initially appears in the pure elemental silicon form, it has an active surface and thus may easily oxidixe in varying degrees to the coated or pure silicon dioxide form. Alternatively, the fiber material may be initially produced in the form of silicon monoxide which in turn dissociates or forms a displacement reaction into elemental silicon and silicon dioxide. The degree of oxidation is dependent upon the post-formation treatment seen by the material prior to analysis. Such treatment includes the atmosphere and other reaction conditions, and, in particular, whether the material is freshly prepared, very hot from the process, and exposed to atmospheric oxygen. Accordingly, some level of oxygen is typically observed in process samples despite attempts to isolate the initial sample of fiber material from oxygen upon its formation in the reactor apparatus. Moreover, it has been observed that the material appears to combust, e.g., to rapidly oxidize from silicon to the silicon dioxide form without visual physical change other than to a slightly lighter color. Additional physiochemical properties of the fiber material of the present invention have been found to be within the following typical ranges: Carbon Content 2-6S Water Viscosity (10 phr) 120-810 (15 phr) 600-2300 Surface Area (BET), m2/g 13-78 Surface Structure, cc/g 145-15 (Dlbutyl Phthalate) Density, g/cc 2.2-2.4, with 2.25 typical Melting Point Greater than lOOO'C Colors Light to Dark Gray, Dark Green, Yellow, Tan to Brown Resistance at 60 phr 6.3 x 1015 in Rubber, ohms With respect to appearance of the fiberous material, it appears quite flocculent, having a texture of fluffy sawdust, spongy dirt, or a latex rubber-like material. As noted in the preceding description of the reactor apparatus and process, a typical feedstock to produce the subject fiber material is as described in Example 2 hereafter. As further noted, It has been discovered that variations in feedstock of the process produced fiberous material of the present invention with not only the same characteristics but additional and different characteristics from those just described. With respect to yet additional characteristics of the fiber material, it has been observed that such material is inert or stable in air indefinitely up to 500"C when partially oxidized, gaining less than 1% in weight after four hours heating. However, at 10000C or higher, the material becomes substantially all silicon dioxide with the fiberous structure remaining intact. After such oxidizing, it was observed that the material melted in the focused electron beam of the transmission electron microscope, whereas partially oxidized fiber material did not melt. Regarding the theory of the growth mechanism of the subject fiber material, several possible such mechanisms have been postulated. However, one such theory Is the vapor-liquid-solid or "VLS" method of fiber growth. Support for this method is indicated by the numerous fibers having catalyst balls as indicated in the TEMS. In particular, representative such balls on the end of fibers may be seen identified by reference numbers 29fl and 292 in Figures 10, 11, 14, ani 15, respectively. A more detailed discussion of this growth method may be found in the previously cited reference to Milewski, et al, a brief discussion of which follows hereafter. However, it will be understood that the present invention is not intended to be limited in scope to any particular theory of fiber formulation herein advanced. In accordance with the VLS method, It is believed that the fiber grows from a supersaturated liquid solution in a catalyst ball comprised of a liquid alloy. A vapor phase metal or metal oxide (vaporized in chamber 10) is deposited on the ball after evolving to a supersaturated gas phase as a result of rapid, extreme temperature drops In the cooler regions of the reactor, e.g., in PRTZ's 32 and 34. Molecules of feed vapor from the gas phase diffuse In a concentration gradient through the catalyst ball where they are absorbed or deposited into the liquid droplet or ball solution and deposit or condense out at the solid-liquid interface. As this liquid becomes supersaturated with the particular feed material, crystal fiber growth commences by precipitatIon from the supersaturated liquid at the Interface between the liquid and solid crystal. The catalyst ball liquid solution is formed by alloying a proper material with the substrate fiber material. It Is believed that trace impuritfes in the feedstock for the fiberous material assists in formation of the catalyst balls. The balls Initiate fiber growth tn one manner upon condesatfon off the vapor In free space, thereby forming the observed individual fibers. More often however, fiber growth is fnitiated on the surface of a small particle of unvaporized starting feedstock material, giving ri-se- to the observed fiberous bundles. Yet another theory or mechanism of formation of the fiber formed in accordance with the present invention which is believed to be more likely than that aforementioned VLS mechanism fs as follows. In this theory, silicon dioxide is reduced fn the apparatus by carbon or another reductant as desired as, for example, methane gas, to form silicon monoxide and silicon. The silicon condenses out before the silicon monoxide to form minute molten drops of silicon. As the temperature of the gases, including silicon monoxide Is reduced, the silicon monoxide begins to condense out on the surface of the molten silicon particles, with the silicon atoms forming a bond and the oxygen atoms remaining on +he outside of the condensate. As more silicon monoxide molecules bond to this surface, the silicon atoms tend to migrate or displace" to the inside next to the silicon core, inasmuch as this condition is more chemically stable. Concurrently with the formation of the silicon monoxide coating around the silicon particles, silicon monoxide fiber may also grow from the silicon particle. The fiber growth Is at a rate greater than that of the particle due to the relatively more reactive silicon surface at the ed of each fiber. The end may be more reactive due to its composition and molecular or crystalline structure or due to the reaction temperature effect at the tip which becomes the preferred reaction or condensation site relative to other silicon monoxide coated particles. The fiber, accordingly, grows at a higher rate in terms of length relative to diameter due to the more reactive surface at the fiber tip. Once the fiber growth has been completed as, for example, by contacting another particle, the fiber then begins to grow by Increasing fn diameter in like manner to the growth of the original molten silicon spheres. It will thus be appreciated that this growth mechanism differs from that of the VLS mechanism in that fiber growth is in a direction away from the sphere as contrasted with the VLS method, wherein fiber growth is at the interface between the sphere and the fiber. Moreover, in the VLS method, diffusion occurs from a gaseous to a liquid form after which preciptatlon occurs to form the solid whisker, whereas, in the present mechanism the liquid phase is substantially eliminated or occurs only at the tip of the fiber on the growth end. It will be appreciated that, although it Is believed that the mechanism thus described is that by which the fibers of the present Invention are formed, such disclosure is by way of mere explanation of a possible theory of growth and the invention is accordingly not intended to be so limited to this particular method. Examples of Process Runs and Product Analyses The invention will now be illustrated more particularly with reference to the following examples. Example 1. In this series of experiments process variables were discovered which appeared to be significant in the production of the fibers. Twelve process runs employing the apparatus depicted in Figures 1 and 2 were made using a Plackett-Burman experimental design known in the art. Six dependent process variables were tested and their significance to variables such as process yield and fiber material chracteristics determined. Thus, the numbers indicated in Tables 2 and 3 are statistical factor effects based upon minimum significant factor effects at 90% confidence levels. The dependent variables Investigated and their respective ranges were as follows: VARIABLE VARIABLE RANGE Reactor chamber temperature 2100-25000C (3800-45000F) Percent oil in feedstock 0 to 0.7X Nitrogen blanket flow rate 2.5-3.7 m3/min (90-130 scfm for both N2 feeds) X Carbon in feedstock 2X to 5X Feed Particle Size 80-120 mesh with and without 5X of -325 mesh silicon dioxide sand Feed rate 2.3-68 kg/min (5-15 lbs/min) The feedstock was comprised of varying percentages of carbon, oil and sand (except for some runs in which no oil was utilized). The composition of the various materials comprising the feedstock was AS follows: Carbon: The carbon was a type of thermal carbon black from the J. M. Huber Corporation having a designation "TB1000" and the following typical physiochemical properties: Iodine No. 5.0 - 15 BET Surface Area, m2/g 5.0 - 15 Tint vs. IRB#3, % 7-10 Pour Density, lbs/cu. ft. 13 - 18 Discoloration of Toluene, fT 85 - 100 pH 6.5 - 10.0 Volatile Content, X 4.0 - 6.0 Ash Content, % 4.0 - 8.0 Sulfur, X 1.0 - 2.0 Oil - The oil, when present in the feedstock. was a light transformer oil from Texaco having a typical chemical analysis of: Carbon 83.3X Sulfur 0.1% Hydrogen 11.9% Other 4.7X Sand - The sand was a #5 (e.g., 80-120 mesh size) silicon dioxide sand havina a typical chemical analysis of: : S102 99.76% CaO Trace Mg0 Trace AL203 0.096X Fe203 0.019X TiO2 0.012X A typical sieve analysis of this sand was: Mesh Size % Retained 40 Trace 50 0.4% 70 3.7X 100 41.4% 140 38.1X 200 15.1X The feedstock was prepared by mixing the sand, carbon black and oil (when utilized) until the sand particles were uniformly coated and the mixture free flowing. It is preferred that the preceding feedstock be at least 90t sand and more preferably substantially 100X sand flour for most beneficial flow characteristics. This feedstock was then delivered to feed tube 22 at the various indicated feed rates whereby it was evenly dispersed as it free fell downward through core 11, protected by a nitrogen gas blanket 26 introduced through ports 24. After passing through reactor chamber 10, the vaporized material, residual feedstock and inert gas then entered the insulated post-reactor treatment zone 32 which had an approximate temperature profile thermocouple readings of 1400us (2500eF) at the top to 900"C (1600'F) at the bottom. After passing through PRTZ 32, the feedstock and gas then entered the water-cooled post reaction treatment zone or PRTZ 34 having a temperature inside the surface of housing 32 of approximately 90"C. From there, the gas and the majority of the fibers formed by the hereinbefore described process flowed through conduit 46 to separator 48. Separator 48 separated the heavier unreacted solids (primarily S102 sand and a small quantity of fibers) from the gas and from the majority of the fibers thus produced and entrained in the gas. The unreacted solids and a small amount of fibers fell through port 50 to a collection receptacle with the majority of the fibers passing through conduit 52. The fiber and gas mixture was then routed from conduit 52 to a conventional bag filter (not shown) wherein the fiberous material of the present invention was thus separated from the gas. The following Table 1 indicates the various fiber yields for indicated run conditions: TABLE I OFF-GAS REACTOR FEED- FEED- FEED- FEED- % NET GROSS TEMPER- RATE STOCK STOCK TOTAL STOCK CARBON FIBER FIBER ATURE (1b/ (% (% FLOW SAND % MON- % YIELD YIELD RUN# ( F) min) CARBON) OIL) (scfm) TYPE NITROGEN OXIDE HYDROGEN (%) (%) 1 4500 15.4 2 0.7 130 mix 88.7 9.2 1.9 6.5 12.6 2 4500 6.0 5 0.7 130 #5 94.2 4.5 1.2 12.6 14.5 3 3800 14.6 5 0.7 90 #5 92.4 3.6 3.8 0.5 1.1 4 4500 14.1 5 0 90 #5 94.7 3.9 1.3 0.8 1.7 5 4500 13.7 2 0 90 mix 94.1 5.2 0.6 1.0 1.2 6 4500 5.1 2 0 130 #5 99.1 0.7 0 1.5 3.1 7 3800 6.6 2 0.7 90 mix 95.5 2.9 1.5 0.4 0.6 8 3800 5.9 5 0 130 mix 99.4 0.5 0 0.8 0.9 9 3800 12.9 2 0.7 130 #5 96.9 1.6 1.3 0.9 1.6 10 4500 5.1 5 0.7 90 mix 89.6 8.9 1.3 3.4 3.4 11 3800 14.4 5 0 130 mix 99.5 0.3 0 0.1 0.2 12 3800 6.1 2 0 90 #5 99.0 0.9 0 0 0.1 It will be noted that "mix" in the "sand type" column refers to a 95%-5% mixture respectively of &num;5 sand and sand having a -325 mesh. "Gross fiber yield" refers to the percent of feedstock by weight converted to a sand-fiber mixture captured at the bag filter, whereas "net fiber yield" refers to the percent of feedstock by weight converted to apparently substantially pure fiberous material of the present invention (e.g., with almost no visible sand content) and collected in the bag filter, assuming a fiber density of 2,98 lb/cu.ft. Also gas percentages indicated an analysis of the percentages of various gases detected in the gas passing through conduit 52 in which the fibers were entrained. The next Table 2 indicates a statistical analysis of the variance of certain preselected variables such as yield as a function of the aforementioned six dependent variables indicated in Table 1. TABLE 2 PRESELECTED FACTOR EFFECTS FOR VARIOUS DEPENDENT VARIABLES NET NET GROSS ADJUSTED FIBER FIBER FIBER FIBER FIBER-SAND FIBER-SAND VARIABLE YIELD #1 YIELD #2 YIELD YIELD CONTAMINATION CONTAMINATION Reactor Chamber 2.6 3.9 5.3 4.1 27.4 -1.3 Temperature Feed Rate -1.2 -1.5 -0.7 -1.7 4.2 2.1 Feedstock (% Carbon) 1.0 1.3 0.4 1.4 -5.4 0.3 Feedstock (% Oil) 2.3 3.4 4.4 3.6 22.1 -0.8 Nitrogen Blanket Flow 1.4 2.7 4.1 2.8 27.4 0.9 Rate Feedstock (Sand Type) -0.2 -0.7 -0.5 -0.7 -3.7 -1.2 Minimu,m Significant Factor Effect at 90% Confidence Level 1.8 3.2 4.1 3.2 27.3 2.2 A few factors must be noted from the foregoing table. The first and second net fiber yields are based upon assumed fiber densities of 1-.83 and 2.98 lb/cu.ft., respectively. The first gross fiber yield is based on the sand-fiber mixture captured at the bag filter. The second or "adjusted" fiber yield is based, upon substantially pure fiber material recovered (e.g., uncontaminated with sand). It further assumes a fiber density of 2.98 lb/cu.ft. and includes an estimate of fiber recovered in the solids collection receptacle below port 50. The first fiber-sand contamination column refers to total sand recovered in the bag filter divided by the total feed by weight. The second fiber-sand contamination column refers to the sand contaminated fiber density. As previously indicated, the foregoing Table 2 (as well as Table which follows) represents a Plackett-Burman form of experimental analysis wherein for an indicated preselected factor to be statistically significant it must be greater than the corresponding minimum significant factor indicated in its respective column. Accordingly, underlined numbers indicate which factors stand out over background noise containing both experimental error and interactions, if present e.g., the dependent variable listed to the left of the number has been found to have a statistically significant effect on the factor indicated above the number. In like manner, the highly subjective analysis of the fibers produced by the foregoing 12 process runs suggest the following relationships between the same six preselected dependent process variables and the indicated fiber characteristics. TABLE 3 PROPERTIES OF PROCESS OR FIBER SIGNIFICANT VARIABLES AFFECTING PROPERTIES Incresed yield of fiber relative to Increased reactor chamber temperature feedstock Increased percent oil in feedstock Presence of carbon Increased averased fiber diameter Increased reactor chamber temperature Increased nitrogen blanket flow rate Increased range of fiber diameter Increased nitrogen blanket flow rate Increased degree of nesting Decreased feed rate Decreased nitrogen blanket flow rate Decreased percent carbon in feedstock Decreased percent oil in feedstock Increased incidence of fibers with Increased reactor chamber temperature balls on ends Increased nitrogen blanket flow rate In the foregoing, it will be noted that "range of average diameter" is highly subjective and means the difference between the smallest and largest diameter of that group consisting of the majority of the fibers. For example, in a sample having an average diameter ranging from 16 to 24 nm, the range of average diameter would be 8 nm. *Upper average fiber diameter" of the above sample would be 24 nm. The large fiber diameter refers to the largest single fiber found in a particular sample. Moreover, the "degree of nesting" and "incidence of fibers with balled end" refer to subjective determination of incidence of these properties previously described with reference to Figures 7-15, such properties being qualitatively analyzed with reference to transmission photomicrograms (TEMS) of samples such as those of Figures 7-15. From experiments and analyses such as those summarized in the foregoing Tables 1 and 2, It has accordingly been discovered that the following functional relationships appear to exist between the respective preselected process variables, fiber and process properties. In particular, with reference to run &num;2 of Table 1 and the ranges and combinations of variables tested, preferred operating conditions for the process of the invention to maximize fiber yield have been found to be as follows: Feedstock: &num;5 SiO2 sand 94.3X Carbon black 5.0% Light Oil 0.7% Reactor chamber conditions: Temperature, core of 25000C (45000F) reactor chamber 10 Feed rate 2.7 kg/min (6 lb/min) Nitrogen blanket flow rate 4.3 m3/min (120 scfm) Post reaction zone 32 870-1400"C (1600-2600"F) temperature profile Example 2: : It will be recalled that one serious problem with previous attempt two grow whiskers was the reproducibility of the process, e.g., it was difficult to consistently produce significant quantities of the material. The purpose of the following tests was to demonstrate the repeatability of the processes of the present invention whereby the novel whiskers described herein could be repeatedly produced and in relatively large quantities. In these experiments, the hereinbefore described apparatus was operated substantially as described for three successor process runs under the following process variable conditions: Temperature of reactor chamber 10 25000C (45000F) Flow rate of inert blanket gas 4.7 m3/min (120 scfm) (nitrogen) into reactor chamber Peedstock feed rate into feed tube 22 7.3 kg/min (16 Ibs/min) Composition ofefeedstock: 94.3% 85 Sand 5.0% TB-lOOO carbon black 0.7X Oil The fiberous material produced by each process run was then collected, analyzed, and compared, resulting in the following comparison data for the samples: : RUN l RUN 2 RUN 3 Chemical composition XSi 54.9 57.8 56.9 X C 3.9 4.0 3.6 X N 0.3 0.2 0.3 Surface area (BET), m29 37.8 45.2 35.5 Density, g/cc 2.3 2.3 2.2 Surface Structure, cc/g 1.60 1.81 1.79 (Dibutyl Phthalate test) Minor variations in certain physical and chemical properties of the fiberous material samples thus produced were evident. Moreover, the preceeding test revealed that the fiber material of the present invention previously described herein in more detail was uniformly and repeatably produced, with electron microscopy examination of the samples clearly showing the fibers to be of substantially identical appearance and substantially in the bundled form depicted herein in photomicrographs. Alternate Embodiment In general, this invention contemplates production of novel fibers from substantially any silica-based feedstock in the presence of a number of different reductants when elevated to relatively high temperatures and thence rapidly cooled in a gas-phased reactor. However, by manipulation of particular process variables in a manner hereinafter described, particular novel forms of the fiber of the present invention are created as well as distinctive novel characteristics such as substantially Increased yields and the like. With respect to the properties of the fiber material of this form of the invention, the material may be characterized as frequently comprising bundles of fibers typically 3-4 microns in diameter and of a generally tan color, with a consistency of sponge rubber or the like and further having a bulk density of 3-5 lbs./cu.ft. and a specific gravity of about 2.20 gms/cu.cm. Electronic microscopy, as with hereinbefore described forms of the fiber of the present invention, indicates the composite material to be comprised of substantially two types of bundling. The first bundling appears as a nest of fibers having diameters of about 30 nm Intermixed with individual particles of about 45 nm in diameter, the fibers appearing to grow from a terminal particle on the end thereof. The more atypical second form of bundling appears to be comprised substantially of solid spheres or cores of up to 4 microns in diameter covered with finer fibers of 10-20 nm in diameter. Bulk analysis of the fiberous material indicates a composition of 54.87-57.80X silicon, 38.5-41.0% oxygen, 3.57-4.00; carbon, and 0.19-0.33% nitrogen. With respect to make-up of a typical individual fiber, transmission electron microscopy indicates the fibers to typically appear as a filament with a spherical particle at the end, the fiberous filament exhibiting a slight curvature which appears to be random. A radially ribbed core is evidenced running the length of the center of the filament and into the spherical particle which is generally darker than the surrounding material. The fiber typically has a diameter of 30 nm, a core of 16 nm, and a terminal particle diameter of 45 nm. The filament core is believed to be of a cubic crystalline silicon and/or silicon carbide composition, and the surface or sheath of the fiber to be of an amorphous silica, with the core containing about 28-32S of the fiber's volume. Typical BET surface area of the material has been found to be typically about 39 n2/g. Filaments have also been produced having observed diameters of about 9 nm, cores of about 5 nm, with sheaths of about 2 nm in thickness. Accordingly, it will be appreciated that notwithstanding these dimensional variations, the relative ratios of these fiber and core diameters and sheath thicknesses have been found to be substantially constant. In the form of the invention presently being described, it has been found that a preferred form of reductant and feedstock exists. More particularly, with respect to the reductant, hydrocarbon gases have been found as the preferred form of reductant such as methane, offering numerous advantages including the fact that feedstock mixing is not ¯ required such as the mixing of carbon and oil into silica sand inasmuch as no carbon or oil is required. This in turn has been found to result in less feedstock being required per pound of silica. Also with respect to the form of the invention being described, it has been found that a particular form of feedstock has been found desirable, namely a silica source having an extremely fine particle size such as a sand flour or the like. Thus, in Example 3 which follows, sand flour, carbon black, and rosin (Ctg, H29, COOH) in various relative proportions were heated to approximately 200OF, thoroughly mixed, cooled to room temperature, and then ground and screened to a 10-35 mesh. The presence of rosin was thought desirable for enhanced carbon utilization and higher carbon loading and, as indicated from the following data with respect to Example 3, fiber material yield substantially increased from a nominal 12% utilizing the aforementioned sand, carbon black and transformer oil feedstock mix to a range of between about 18.6-35.9%. With respect to the aforementioned beneficial effects of a hydrocarbon reductant, these benefits may be clearly seen with respect to the following typical production runs wherein yields of fiberous material have been substantially increased from the nominal 12% to between 50-60g. From the following two Examples 3 and 4, it will be appreciated as a feature of the invention to either alone or in combination provide for a feedstock source of silica wherein the particle size is reduced as small as practicable (as, for example, with sand flour having a nominal particle size of 45 microns compared to 85 sand with a 150 micron size) and to provide for a reductant in the form of a hydrocarbon gas such as the aforementioned methane. It is believed that these two features alone and in combination exhibit a beneficial functional relation to yield of the desired fiberous material, e.g, yields have been found to increase with increasing feedstock silica particle size such as sand flour and w'th increased usage of gaseous reductants such as methane, strip gas, or the like. Example 3. In this example, feed form effects were tested on yield whrein particle size of the silica source was substantially reduced by employing a fine sand flour. Run A A 1:1 sand flour/rosin mix with 2% carbon black was utilizes, wherein the mix was heated to 200cm, mlxed, cooled to room temperature, and then ground and screened to a 10-35 mesh. A water cooled PRTZ 3 was employed with the following results: REACTOR NITROGEN YIELD TEMPERATURE FLOW RATE RUN OF FIBER ("F) (SCFM) TIME MATERIAL 4500 2.3 5 Minutes 35.9% Run B A 2:1 sand flour/rosin mix with 2% carbon black was utilized and prepared as in Run A. A brick insulated PRTZ 34 was utilized with the following results: REACTOR NITROGEN YIELD TEMPERATURE -FLOW RATE RUN OF FIBER ('F) (SCFM) TIME MATERIAL 4500 2.3 4 Minutes 18.62 The foregoing and other like runs has confirmed a direct inverse functional relation between silica source, particle size and yield wherein for a relatively large sand particle size for example, on the order of 150 microns, yields on the order of 12X were found typi'cal, whereas when particle size was reduced to on the order of 45 microns or less, yield of the desired fiberous material of the present invention typically Increased to within ranges of, for example, about 19-37X. Example 4. In this example, the effects of gaseous reductants on yield were tested wherein a methane gas was utilized. Run A A 1.37 lb/m ZEOSYLe feedstock was used with a methane-laden strip gas at a 15 sc-fm flow rate wherein a water-cooled PRTZ was utilized, with Tt and T2 representing the temperatures at the top and bottom of the PRTZ during the runs. Nitrogen blanket flow rate was 120 mcf with a nitrogen inlet temperature ranging between 67-72-F. REACTOR CORE TIME TEMPERATURE (MINUTES) ('F) T1 ('F) T2 ('F) YIELD 0 4300 1523 1252 56.8% 5 4293 1657 1281 9 4297 1712 1280 15 4202 1758 1295 20 4303 1776 1286 35 4326 1758 1305 41 4318 1809 1307 51 4303 1825 1329 68 4318 1827 1315 80 4290 1821 1331 95 4313 1792 1301 Run B A 1.33 lb/m sand flour was utilized with a methane reductant gas at a 1.5 scfm flow rate. The monitored temperatures were as with Run A, with the nitrogen blanket flow rate at 120 mcf and the nitrogen inlet temperature ranging between 76-80'F. REACTOR CORE TIME TEMPERATURE (MINUTES) ('F) T1 ('F) T2 ('F) YIELD 0 4490 1504 1289 57.3% 10 4492 1931 1342 23 4509 2006 1375 34 4501 2055 1400 42 4497 2063 1401 53 4509 2067 1397 67 4511 2082 1414 76 4511 2088 1430 90 4518 2089 1440 98 4521 2090 1440 106 4518 2087 1441 From the foregoing and other like runs, it has been confirmed that there is a direct and substantial improvement with yield of the desired fiberous material of the present invention with use of a gaseous reactant such as methane both with and without silica feedstocks having reduced particle size such as those employed in Example 3. Several additional aspects of the present invention are to be noted. First, it has been found that a functional relationship exists between yield and "residence time", or the time during whIch the gas and feed material are resident within the heated zone of the reactor, with an optimum such residence time being exhibited for maximizing fiber yield. This residence time may be given by: Residence Time = Hot Volume of Reactor Core / Flow Rate of Material Through Core For a representative typical calculation In which the reactor core hot volume was 0.16 cubic feet, the nitrogen blanket flow rate was 2.3 scfm, and the reactor temperature Is 4500°F, the residence time Is given by: Flow Rate = 2.3 scfm x 1 Minute x (4500 + 460) 'R = 0.35 cu.ft./second 60 seconds (80 + 460) 'R Residence Time = 0.16 cubic feet = 0.45 seconds 0.35 cubic feet/second As hereinbefore noted, a relationship has further been found between yield and temperature differential between the reactor and the PRTZs. More particularly, a more rapid temperature reduction or "quenching" from the relatively hotter core to a cooler PRTZ has been found to increase both yield and BET of the resultant fibers. It is thought that the quenching reduces the quantity of silicon monoxide being further reduced to silicon resulting in premature condensation of silicon particles and thus adversely affecting yield. Accordingly, as aforesaid, with a relatively cooler PRTZ, by means of water cooling, yield was found to be greater than with respect to a relatively hotter brick-insulated PRTZ. Yet an additional functional relationship between process variables and product characteristics has been noted. It has been found that by recycling the fiberous product of the hereindescribed processes, increased yields of, for example, from 12-16X have been noted. It Is thought that this is due to the fact that the recycled fiber material is Summary Table of Physical Properties Range TABLE 4 of Typical Physical Property Instrument Values Value Bulk density as poured 64-80 kg/m 72 kg/m Specific gravity Backman Air 2.1-2.6 g/cc 2.25 g/cc pycnometer Particle size Couller counter 0.3-30 median 3.5 m distribution TA-II 2.8-4.3 s Surface area Huber BET 4-point 30-50 mê/g 3.5 mê/g Quantachroms Monosorb Fiber diameter Philipws 121300 2-50nm 25nm Langth: :Diameter (4D) Brookfield RVT 10-20 14 Viscometer RTVD DBF absorption Brabender 150-200 cc/g 169 cc/100 g Absorptometer Viscosity Brookfield RVT viscometer (i) 10 parts (fiber)/ 200-400 cps 300 cps 100 parts H2O (25 C) (ii) 15 parts (fiber)/ 1400-1700 cps 1600 cps 100 parts H2O (25 C) Fackinf fraction Pf 0.10-0.30 0.27 Einstein Coefficient Brookfield varies with 9.1 viscometer polarity RTVD with UL adaptor pH pH meter - 7.1 Color visual tan to elive light tan CTAB absorption Lake Atmost 50-100 ml/g 75 ml/g cethyltriammonium bronide Type of Typical Element/Component Analysis Instrument Value (%) Total silicon Neutron Activation Triga Mark I 59.5 Nuclear Reactor Total silicon Colorimetric Test - 57.0 Elemental silicon (crystalline) XRD Philips 1729 20.4 Total oxygen Netron Activation - 40.0 Total carbon 6 Elemental Parkin Elmer 3.7 Total nitrogen Analyser 2400 [0.25] H2O Moisture Oven 0.1 Total Sulfur Sulfur Analysis Loco SC132 [0.06] Percent residue Gravimetric 21.0 Percent residue Gravimetric 2.0 with HF/HR03 Percent oxidation Gravimetric Muffle furnace 24.4 thus silicon monoxide-enriched due to the first pass through the process which is, as previously noted, required for fiber formation. Finally, with respect to the novel fiberous material produced in accordance with the invention as hereindescribed, In Table 4 there will be seen a table summarizing the physical properties of a representative sample of the material. Figure 12 Is a representative spectrogram of an unoxidized sample of the fiberous material and Figure 13 is a spectrogram of the sample after having been exposed to an oxidant for approximately 12 hours. It is therefore apparent that the present Invention is one well adapted to obtain all of the advantages and features hereinabove set forth, together with other advantages which will become obvious and apparent from a description -of the invention itself. It will be understood that certain combinations and subcomblnations are of utility and may be employed without reference to other features and subcombinations. Moreover, the foregoing disclosure and description of the invention is only illustrative and explanatory thereof, and the invention admits of variations in the size, shape and composition of the material, as well as in the details of the illustrated construction and process, without departing from the scope and spirit thereof.

Claims: CLAIMS 1. In a high-temperature fluid-wall reactor including a cylindrical-shaped reactor tube having a central axis and formed from a refractory material a reaction zone within said reactor tube for inputting reactants, means for heating said reaction tube to incandescence for emitting radiation radially inward to said reaction zone for maintaining a desired chemical reaction, and an inert gas for forming a protective fluid wall for the inner surface of said reactor tube, the improvement comprising: : said reactor tube material being substantially impervious to gas flow; said reactor tube having the plurality of perforations for permitting flow of said inert gas radially inward through said tube; each of said plurality of perforations including an exit adjacent said inner wall of said reactor tube for directing said inert gas in a jetstream commencing adjacent said exit and directed toward said reaction zone; said plurality of perforations being spaced about said reactor tube such that each of said jetstreams engages one or more other of said jetstreams for forming an integral protective fluid wall while maintaining a radially-directed momentum sufficient to repel said reactants; and the radially directed velocity of each of said jetstreams diminishes within said reactor tube without disturbing fluid flow with-in said reaction zone. 2. The apparatus as defined in Claim 1, wherein each of said plurality of perforations through said reactor tube is formed about an aperture axis passing substantially through said central axis of said reactor tube 3. The apparatus as defined in Claim 1, furthe-r comprising: a first cylindrical-shaped reactor tube portion having perforations spaced substantially throughout the length of said first tube portion and spaced substantially around the perimeter of said first tube portion; a second cylindrical-shaped reactor tube portion spaced downstream of said first tube portion and being substantially unperforated; and said inert gas flow downstream of said first portion being substantially laminar for maintaining said protective fluid wall throughout the length of said second tube portion. 4. The apparatus as defined in Claim 2, wherein each of said perforations through said reactor tube has a generally cylindrical configuration formed about said aperture axis and has a diameter of about .020 inches or greater. 5. The apparatus as defined in Claim 2, wherein said aperture axis of each said perforations is substat- tially perpendicular to said central axis of said reactor tube. 6. The apparatus as defined in Claim 2, wherein said plurality of perforations are located about said reactor tube such that any line on an inner surface of said reactor tube parallel to said central axis of said reactor tube passes through a plurality of said perforations. 7. The apparatus as defined in Claim 6, wherein said plurality of perforations are located on said reactor tube at lattice points of the uniform lattice pattern. 8. The apparatus as defined in Claim 1, wherein said reactor tube material has a thermal conductivi.ty in a radial direction with respect to said central axis of at least 16 BTU/ft.-hr.-0F at 40000F. 9. The apparatus as defined in Claim 3, further comprising: conduit means for passing inert gas to the exterior surface of said first cylindrical tube portion; and barrier means for restricting inert gas flow from said exterior surface of said first cylindrical tube portion to the exterior surface of said second cylindrical tube portion. 10. The apparatus as defined in Claim 4, further comprising: said plurality of perforations each have mean diameters in the range of from .02 inches to .10 inches; and said plurality of perforations are spaced about said reactor tube at centerlinespacings of from .06 inches to .35 inches. 11. The apparatus as defined in Claim 4, further comprising: said plurality of perforations each have mean diameters in the range of from .025 inches to .035 inches; and said plurality of perforations are spaced about said reactor tube at centerline spacings of from .06 inches to .15 inches. 12. A method for forming a fluid wall in a high temperature reactor of the type employing a reaction zone for inputting reactants within a reactor tube and heating said reactor tube to incandescence for emitting radiation radially inward from said-reactbr tube to maintain a desired chemical reaction, the improvement comprising: forming a plurality of perforations through said reactor tube each having a linear perforation axis; passing inert gas inwardly through said plurality of perforations for forming inert gas jetstreams maintaining a radially-directed momentum sufficient to repel said reactants; spacing said plurality of perforations about said reactor tube such that said jetstreams overlap for forming an integral protective fluid wall; and controlling the velocity of said jetstreams such that the radially-directed velocity component of said jetstreams substantially terminates before reaching said reaction zone. 13. A method as defined in Claim 12, wherein each of said plurality of perforations through said reactor tube is directed along said perforation axis passing substantially through a central axis of said reactor tube. 14. A method as defined in Claim 12, further comprising: forming a first portion of said reactor tube having said plurality of said perforations; spacing a second unperforated portion of said reactor tube downstream of said first portion; and controlling the flow rate of said inert gas passing through said perforations for obtaining laminar flow downstream from said first portion of said reactor tube to maintain said fluid wall within said second portion of said reactor tube. 15. A method as defined in Claim 14, further comprising: passing inert gas from outside said reactor into engagement with a chamber at least partially defined by the outer surface of said first portion of said reactor tube; and prohibiting inert gas flow from said outer surface of said first portion of said reactor tube to the outer surface of said second portion of said reactor tube. 16. A method as defined in Claim 13, wherein each of said perforations is formed in a generally cylindrical configuration about said perforation axis; and said perforation axis is substantially perpendicular to said central axis of said reactor tube. 17. A method as defined in Claim 13, further comprising: locating said plurality of perforations about said reactor tube such that any line on the inner surface of said reactor tube parallel to said central axis of said reactor tube passes through a plurality of said perforations. 18. A method as defined in Claim 12, further comprising: forming said plurality of perforations through said reactor tube each having a mean diameter in the range of from .03 inches to .09 inches; and spacing said plurality of perforations about said reactor tube at centerline spacings of from .10 inches to .30 inches. 19. A method as defined in Claim 14, further comprising: positioning said first section of said reactor tube in the vicinity adjacent an inlet feed tube for said reactor; and positioning said second section of said second reactor tube in the vicinity of heating elements for said reactor. 20. A method as defined in Claim 14, further comprising: passing inert gas from outside said reactor into engagement with a chamber at least partially defined by the outer surface of said first section of said reactor tube; and heating said inert gas before being passed to said chamber defined by said outer surface of said first section of said reactor tube. 21. A method as defined in Claim 19, further comprising: providing a third perforated section of said reactor tube downstream from said second unperforated section of said reactor tube; and passing inert gas radially inward through perforations in said third section of said reactor tube for maintaining a protective fluid wall for said third section of said reactor tube. 22. A method for preparing whisker fiber material, comprising: (a) introducing a sllicon-containing feedstock and a gaseous hydrocarbon reductant into a stream of gas; (b) heating said feedstock, said reductant, and said gas to a first temperature sufficient for at least a portion of said feedstock to produce a vapor phase; and (c) cooling said vaporized feedstock, said reductant and said gas to a second temperature sufficient for a portion of said vaporized feedstock to condense as said fiber material within said gas stream. 23. The method of Claim 22, wherein said feedstock is sand flour. 24. The method of Claim 22, wherein said hydrocarbon gas is methane. 25. The method of Claim 22, wherein: said feedstock has an average particle size; and wherein the amount of said fiber material relative to said feedstock defines a yield; and wherein said yield varies inversely with said particle size. 26. The method of Claim 22, wherein: said feedstock, said reductant, and said gas are heated within a reactor to said first temperature; a residence time is functionally related to the time said feedstock, said reductant, and said gas are within said reactor; wherein the amount of said fiber material relative to said feedstock defines a yield; and wherein said residence time is preselected to produce a desired said yield. 27. A method for preparing cobweb whisker material In a reactor having: a high temperature reactor chamber means defining an inner core, and having a feed means for introducing a feedstock containing a form of silicon and a reductant into the top of said core; heating means for heating said core to a first temperature; and means for introducing a blanket of gas between said core and said feedstock; a first post reactor means interconnected to and disposed below said reactor chamber means defining a first post reactor temperature zone internal thereof, said first post reactor means being for maintaining said first post reaction temperature zone for maintaining said first zone at a second temperature; a second post reactor means interconnected to and disposed below said first post reactor means defining a second post reactor treatment zone internal thereof, said second post reactor means being for maintaining said second zone at a third temperature; and recovery means interconnected to said second post reactor means for recovering said material from said second post reactor means; said reactor chamber means, said first and second post reactor means, and said recovery means being further interconnected whereby continuous internal fluid communication is established from said feed means through said reactor chamber means, said first and second post reactor means, and said recovery means; and wherein said method for preparing said whisker material comprises the steps of: : (a) introducing said feedstock into said core; (b) establishing said blanket of gas in said core; (c) heating said core to said first temperature and in an amount sufficient for at least a portion of said feedstock to vaporize; Cd) transferring the contents of said core to sad first zone of said first post reactor means for cooling said contents to said second temperature and in an amount sufficient for at least a portion of said vaporized feedstock to supersaturate; (e) transferring the contents of said first zone to said second zone of said second post reactor means for cooling said contents of said second zone to said third temperature; and (f) transferring the contents of said second zone to said recovery means; (g) recovering from said recovery means said whisker material, and wherein said reductant is a gaseous hydrocarbon. 28. The method of Claim 27, wherein said form of silicon is a sand flour. 29. The method of Claim 27, wherein: said form of silicon has an average particle size; and wherein the amount of said recovered whisker material relative to said feedstock defines a yield; and wherein said yield varies inversely with said particle size. 30. The method of Claim 27, wherein: said recovered whisker material includes fibers defining an average fiber diameter; and wherein said diameter varies directly with said first temperature. 31. A whisker fiber material produced according to the process of: -(a) introducing a feedstock containing a form of silicon and a gaseous reductant into a stream of gas; (b) heating said feedstock and said gas to- a first temperature sufficient for at least a portion of said feedstock to produce a vapor phase; (c) cooling said vaporized feedstock and said gas to a second temperature sufficient for a portion of said vaporized feedstock to condense as said fiber material within said gas stream. 32. The method of Claim 31, wherein said form of silicon is a sand flour. 33. The method of Claim 31, wherein: said form of silicon has an average particle size; and wherein the amount of said recovered whisker material relative to said feedstock defines a yield; and wherein said yield varies inversely with said particle size. 34. The method of Claim 31, wherein: said recovered whisker material includes fibers defining an average fiber diameter; and wherein said diameter varies directly with said first temperature. 35. A cobweb whisker fiber composed of silicon, silicon oxide, or a combination thereof having a diameter within the range of about 2-50 nanometer. 36. A fiber material comprised of a bundle of whisker fibers, each of said fibers being composed substantially of silicon, silicon monoxide, silicon dioxide, or a combination thereof, wherein said bundle has a diameter within the range of about 300-5000 nanometer. 37.. A fiber material comprised substantially of a plurality of bundles of whisker fibers, said fibers being composed of silicon, silicon monoxide, silicon dioxide, or a combination thereof, wherein said fiber material includes fibers composed of a silicon or silicon monoxide core and having a silicon dioxide outer coating, and wherein said fiber material has a surface area within the range of about 10-80 m2/g. 38. A fiber material comprised substantially of a plurality of bundles of whisker fibers, said material having a chemical composition of about 55-60S silicon, 38-43% oxygen, and 1-65 carbon. 39. A method for preparing whisker fiber material, comprising: (a) introducing a silicon-containing feedstock and a gaseous reductant into a stream of inert gas which envelopes said feedstock and said reductant radially outwardly thereof; (b) heating said feedstock, said reductant, and said gas to a first temperature sufficient for at least a portion of said feedstock to produce a vapor phase within the range of about 270-5000"F; and (c) cooling said vaporized feedstock, said reductant, and said gas to a second temperature sufficient for a portion of said vaporized feedstock to condense as said fiber material within said gas stream,.wherein said portion of said feedstock forming said fiber material varies relative to the amount of said feedstock directly in function41 relation to said first temperature. 40. A method for preparing cobweb whisker material in a reactor having: a high temperature reactor chamber means defining an inner core, and having a feed means for introducing a feedstock containing a form of silicon and a gaseous reductant into the top of said core; heating means for heating said core to a first temperature; and means for introducing a blanket of gas between said core and said feedstock;; a first post reactor means interconnected to and disposed below said reactor chamber means defining a first post reactor temperature zone internal thereof, said first post reactor means being for maintaining said first post reaction temperature zone for maintaining said first zone at a second temperature; a second post reactor means interconnected to and disposed below said first post reactor means defining a second post reactor treatment zone internal thereof, said second post reactor means being for maintaining said second zone at a third temperature; and recovery means interconnected to said second post reactor means for recovering said material from said post reactor means; said reactor chamber means, said first and second post reactor means, and said recovery means being further interconnected whereby continuous internal fluid communication is established from said feed means through said reactor chamber means, said first and second post reactor means, and said recovery means; and wherein said method for preparing said whisker material comprises the steps of: : (a) introducing said feedstock into said core; (b) establishing said blanket of gas in said core; (c) heating said core to said first temperature and In an amount sufficient for at least a portion of said feedstock to vaporize; (d) transferring the contents of said core to said first zone of said first post reactor means for cooling said contents to said second temperature and in an amount sufficient for at least a portion of said vaporized feedstock to supersaturate; (e) transferring the contents of said first zone to said second zone of said second post reactor means for cooling said contents of said second zone to said third temperature; (f) transferring the contents of said second zone to said recovery means;and (g) recovering from said recovery means said whisker material and wherein said reductant is gaseous. 41. A cobweb whisker fiber material produced in a reactor having: a high temperature reactor chamber means defining an inner core, and having a feed means for introducing a feedstock containing a form of silicon and a reductant into the top of said core; heating means for heating said core to a first temperature; and means for introducing a blanket of gas between said core and said feedstock; a first post reactor means interconnected to and disposed below said reactor chamber means defining a first post reactor temperature zone internal thereof, said first post reactor means being for maintaining said first post reaction temperature zone for maintaining said first zone at a second temperature; a second post reactor means interconnected to and disposed below said first post reactor means defining a second post reactor treatment zone internal thereof, said second post reactor means being for maintaining said second zone at a third temperature; and recovery means interconnected to said second post reactor means for recovering said material from said second post reactor means; said reactor chamber means, said first and second post reactor means, and said recovery means being further interconnected whereby continuous internal fluid communication is established from said feed means through said reactor chamber means, said first and second post reactor means, and said recovery means; said fiber material being produced according to a process comprising the steps of: : (a) introducing said feedstock into said core; (b) establishing said blanket of gas in said core; (c) heating said core to said first temperature and in an amount sufficient for at least a portion of said feedstock to vaporizes (d) transferring the contents of said core to said first zone of said first post reactor means for cooling said contents to said second temperature and in an amount sufficient for at least a portion of said vaporized feedstock to supersaturate; (e) transferring the contents of said first zone to said second zone of said second post reactor means for cooling said contents of said second zone to said third temperature; (f) transferring the contents of said second zone to said recovery means; and (g) recovering from said recovery means said whisker material, and wherein said reductant is gaseous.

Inventors: SCHRAMM, DALE E.
Applicants: J.M. HUBER CORPORATION
Application year: 1985
Main classification: B01J12
IPC codes: C30B25, B01J12