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WO1998003699A9 - Elements a noyaux transmutes presentant des distributions isotopiques non naturelles obtenues par electrolyse, et methode de production - Google Patents

Elements a noyaux transmutes presentant des distributions isotopiques non naturelles obtenues par electrolyse, et methode de production

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Publication number
WO1998003699A9
WO1998003699A9 PCT/US1997/012309 US9712309W WO9803699A9 WO 1998003699 A9 WO1998003699 A9 WO 1998003699A9 US 9712309 W US9712309 W US 9712309W WO 9803699 A9 WO9803699 A9 WO 9803699A9
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WIPO (PCT)
Prior art keywords
conductive
cell
elements
electrolytic cell
housing
Prior art date
Application number
PCT/US1997/012309
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English (en)
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WO1998003699A2 (fr
WO1998003699A3 (fr
Filing date
Publication date
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Priority to AU46440/97A priority Critical patent/AU4644097A/en
Publication of WO1998003699A2 publication Critical patent/WO1998003699A2/fr
Publication of WO1998003699A3 publication Critical patent/WO1998003699A3/fr
Publication of WO1998003699A9 publication Critical patent/WO1998003699A9/fr

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Definitions

  • the electrolytic cell described therein included an inlet and an outlet facilitating the flow of the liquid electrolyte therethrough.
  • the liquid electrolyte is passed through the electrolytic cell, it is acted upon catalytically by the particular bed of catalytic particles contained within the housing of the electrolytic cell to produce excess heat for use.
  • This invention is directed to a method for producing new elements by low temperature nuclear transmutations during electrolysis in an aqueous media within an electrolytic cell, which transmutations, in part, show the distinct characteristics of isotopes which have shifted in ratios of occurrence from those natural abundance.
  • the electrolytic cell includes a non-conductive housing having an inlet and an outlet and spaced apart first and second conductive grids positioned within the housing.
  • a plurality of preferably cross linked polymer non-metallic cores each having a uniform conductive exterior metallic surface formed of a high hydrogen absorbing material, such as a metallic hydride forming material, form a bed of conductive beads closely packed within the housing in electrical contact with the first grid adjacent the inlet.
  • An electric power source in the system is operably connected across the first and second grid whereby electrical current flows between the grids and within the aqueous media flowing through the cell.
  • Figure 1 is a schematic view of a system and electrolytic cell embodying the present invention.
  • Figure 2 is a section view of the electrolytic cell shown in Figure 1.
  • Figure 3 is processed data from a secondary ion mass spectrometer (SIMS) analysis of the outer bead material of beads utilized in Test Number 3 before test run.
  • SIMS secondary ion mass spectrometer
  • Figure 4 is processed data from a SIMS analysis of the outer bead material of beads utilized in Test Number 3 after test run.
  • Figure 5 is a graph depicting binding energy per nucleon versus atomic mass number.
  • Figures 6a and 6b are graphic depictions of the data presented in Table VIII.
  • Figures 7a and 7b are graphic depictions of total increases elemental masses per microsphere and in the thin outer film, respectively, and corresponding to data presented in Figures 6a and 6b.
  • Figure 8 is a graphic depiction of differences between isotopic percentage concentrations observed after cell operation and those for natural abundance for the reaction product elements shown in Table III.
  • FIG. 10 a system embodying concepts of the invention utilized during testing procedures is shown generally at numeral 10 in Figure 1.
  • This system 10 includes an electrolytic cell shown generally at numeral 12 interconnected at each end with a closed loop electrolyte circulation system.
  • the circulation system includes a constant volume pump 18 which draws a liquid electrolyte 59 from a reservoir 32 and forces the electrolyte 59 in the direction of the arrow into inlet 54 of electrolytic cell 12. After the electrolytic cell 12 is completely filled with the electrolyte 59, the electrolyte then exits an outlet 56, thereafter flows into a gas separator 26 which is provided to separate and recombine hydrogen and oxygen gas from the electrolyte 59.
  • An in-line filter 22 capable of filtering down to 0.8 microns of particle size is provided for filtration of debris within the system.
  • the system 10 also includes a digital flow meter 19 to accurately measure electrolyte flow through the system 10.
  • an in-line heater 21 disposed between the filter 22 and the cell 12. This heater 21 is provided to heat the electrolyte liquid 59 as it flows through the system 10 and the cell 12. Note importantly that the heater 21 may be positioned anywhere in the closed system electrolyte flow path as the heating applied is of a steady state nature rather than only a pre-heating condition of the electrolyte, although positioning of the heater 21 is preferred to be adjacent the inlet
  • the heating of the electrolyte external to the cell 12 is one means for triggering and enhancing the catalytic reaction within the cell 12 to produce a positive temperature differential ( ⁇ T) of the electrolyte as it flows through the cell 12.
  • Shown in Figure 2 is another means preferred for triggering this heat production reaction between the electrolyte 59 and a bed 35 of conductive particles 36 within the cell 12 is by the application of sufficient electric d.c. current across electrodes 15 and 16 as described herebelow.
  • Each of the end members 46 and 48 includes an inlet stopper 54 and an outlet stopper 56, respectively. Each of these stoppers 54 and 56 define an inlet and an outlet passage, respectively into and out of the interior volume, respectively, of the electrolytic cell 12.
  • These end members 46 and 48 also include a fluid chamber 58 and 60, respectively within which are mounted electrodes 15 and 16, respectively, which extend from these chambers 58 and 60 to the exterior of the electrolytic cell 12 for interconnection to a constant current-type d.c. power supply (not shown) having its negative and positive terminals connected as shown. Also positioned within the chambers 58 and 60 are thermocouples 70 and 72 for monitoring the electrolyte temperature at these points of inlet and outlet of the electrolytic cell 12.
  • a plurality of separate, packed conductive beads or particles 36 are positioned to define a bead bed 35 within housing 14 immediately adjacent and against a conductive foraminous or porous grid 38 formed of titanium and positioned transversely across the housing 14 as shown. These conductive beads 36 are described in detail herebelow.
  • a non-conducive foraminous or porous nylon mesh 40 is positioned against the other end of these conductive particles 36 so as to retain them in the position shown.
  • Adjacent the opposite surface of this non-conductive mesh 40 is a plurality of non-conductive spherical beads, or more generally particles, 42 formed of cross-linked polystyrene and having a nominal diameter of about 1.0 mm.
  • a conductive foraminous or porous grid 44 formed of titanium and positioned transversely across the housing 14 as shown.
  • non-conductive beads 42 replaces the non-conductive beads 42 with non-metallic spherical cation ion exchange polymer conductive beads preferably made of cross-linked styrene divinyl benzene having fully pre-sulfonated surfaces which have been ion exchanged with a lithium salt.
  • This preferred non-metallic conductive microbead structure will thus form a "salt bridge" between the anode 44 and the conductive particles 36, the non-conductive mesh 40 having apertures sufficiently large to permit contact between the conductive particles 36 and the conductive non-metallic microbeads.
  • the mesh size of mesh 40 is in the range of 200-500 micrometers. This preferred embodiment thus prevents melting of the sulfonated non-conductive beads 42 while reducing cell resistance during high loading and normal operation.
  • the end of the electrode 15 is in electrical contact at 66 with conductive grid 38, while electrode 16 is in electrical contact at 68 with conductive grid 44 as shown.
  • the preferred formulation for this electrolyte 59 is generally that of a conductive salt in solution with water.
  • the preferred embodiment of water is that of either light water ( 1 H 2 0) or heavy water and, preferably deuterium ( 2 H 2 0).
  • the purity of all of the electrolyte components is of utmost importance.
  • the water ( 1 H 2 0) and the deuterium ( 2 H 2 0) must have a minimum resistance of one megohm with a turbidity of less than 0.2 N.T.U. This turbidity is controlled by the ultra membrane filtration.
  • the preferred salt solution is lithium sulfate (Li 2 S0 4 ) in a 0.5-molar mixture with deionized water and is of chemically pure quality having a resistance of 2 X 10 6 ohms or greater.
  • a lithium sulfate is preferred, other conductive salts chosen from the group containing boron, aluminum, sodium, gallium, and thallium, as well as lithium, may be utilized.
  • the preferred pH or acidity of the electrolyte is 9.0.
  • Whetstone Bridge or ohm meter was utilized prior to the introduction of the electrolyte into the electrolytic cell. This cell resistance, when dry, should be infinitely high. Otherwise, a short between the anode screen and the cathode beads exists and the unit would have to be repacked. When testing with electrolyte present at 0.02 amps, the resistance should be in the range of 100 to 200 ohms per sq. cm of cross section area as measured transverse to the direction of current flow.
  • the beads used in Runs 1 , 2 and 3 also have a copper flash coating formed directly atop the cores.
  • Run 7A used a bead construction having a plated layer of palladium on a sulfonated core built up to 1.0 ⁇ to 1.4 ⁇ , followed by a 0.6 ⁇ plated nickel layer.
  • a sputtering technique that utilizes a vibrator method to suspend beads during sputtering application of surface thin film coatings has been developed and is the subject of a separate U.S. patent application 08/748,682 filed November 13, 1996 and co-pending with this application.
  • This invention was developed and employed to produce the sputtering samples reported in Test Runs 4 through 8 and facilitated the multiple thin films in Test Runs 6 and 7.
  • the advantage of the sputtering technique as facilitated by this improved application apparatus include the ability to achieve thinner layers with better control of uniformity, the ability to achieve a large number of multiple layers, and the capacity to employ a variety of materials.
  • the catalytic beads utilized in Test Run #4 had a combination of nickel atop the styrene core, followed by palladium, followed by an outer nickel layer.
  • Catalytic beads utilized in Test Run #5 had two additional layers, first of palladium, then nickel thereatop as did the catalytic beads utilized in Test Run #6.
  • the catalytic beads In Test Run #7, the catalytic beads only had a single sputtered layer of nickel formed directly atop the styrene non-conductive core.
  • Catalytic particles utilized in Test Run #8 reported in Table II herebelow utilized a palladium layer sputtered directly atop the styrene core, followed by a sputtered layer of nickel.
  • This test electrolytic cell was specially prepared as a "clean cell" sample to insure that virtually no foreign contamination of any sort would interfere with test results.
  • all of the clean cells have high purity aqueous media circulated in contact with only plastic surfaces to eliminate contact with metal, and thus, no metal contamination is possible.
  • the range in diameters of the conductive particles as above described is relatively broad, limited primarily by the ability to plate the cores and the economic factors involved therein. As a guideline however, it has been determined that there exists a preferred range in the ratio between the total surface area of all of the conductive particles collectively within the electrolytic cell and the inner surface area of the non-conductive housing which surrounds the bed of conductive particles.
  • a minimum preferred ratio of the total bead surface area to the inner housing surface area is in the range of 5 to 1 (5:1).
  • an ideal area ratio is 10 to 1 (10:1) and is typically utilized in the experiments reported herebelow. This ratio is thus affected primarily by the size of the conductive particles, the smaller the diameter, the higher the ratio becomes.
  • the testing procedures for cell operation incorporated two stages.
  • the first stage may be viewed as a loading stage during which a relatively low level current
  • the current level between conductive members is then incrementally increased, during which time the electrolyte temperature differential is monitored.
  • the temperature of the electrolyte 59 circulating through the electrolytic cell 12 and system 10 was fully monitored, along with temperature differential between thermocouples 70 and 72 and flow rate of the liquid electrolyte 59.
  • the electrolyte inlet temperature was monitored immediately upstream of stopper 54 to more accurately reflect temperature differential ( ⁇ T).
  • the reacted beads were removed from each cell for thorough testing which included gamma scanning, electron microscopy and mass spectrometry.
  • the top layer of reacted beads next to the anode of each test cell was taken and washed with deionized water.
  • a separate sample of the identical unreacted virgin beads was also washed with deionized water.
  • each of the samples of reacted beads were tested with a Geiger-Mueller scanning for gamma rays with negative results, as was the check for tritium in the liquid medium.
  • a portion of each of the reacted beads was also placed on an x-ray sensitive film for a period of five days with no significant flogging detected.
  • Table III An example of a more thorough analysis of this processed data is shown in Table III herebelow. These results were taken with respect to the palladium/nickel catalytic beads used in the test cell in Run #8 reported hereinabove. Table III shows the isotopic shifts with error bars, while Table IV shows the isotopic shifts overlapping with other elements. The fact that such a large number of elements have a non-natural isotopic distribution indicates that they cannot be attributed to impurities entering the coating. These exact amounts of select elements before and after running were determined by NAA while the isotope shifts are from SIMS measurements.
  • Run No. 8 lasted for 310 hours and employed an entering electrolyte temperature of approximately 60°C. Termination of the run was made prior to any noticeable deterioration of thermal performance. A temperature rise across the cell of less than 0.5°C was obtained throughout the run, representing an output of 0.5 ⁇ 0.4 watts. Calibration corrections due to heat losses and flow-pattern variations prevented a more accurate measurement, but the output always indicated a positive excess heat.
  • the cell employed for the run used all plastic fittings with the exception of the pressure and flow meters and the pump. (To further decrease possible impurity sources, a loop with all plastic components except for the electrodes was developed for subsequent runs. As noted later, this modification did not cause a noticeable change in film products.) Titanium electrodes were used. A filter fitted with 0.8- ⁇ m pore size filter paper was inserted in the loop to collect any fine particles entering the electrolyte, either from film surfaces or from other parts of the system.
  • Characteristics of the 650-A Ni film microspheres used in run #8 are summarized in Table IV.
  • a 650-A-thick Ni film was laid down by sputtering the Ni on to a 1 -mm plastic core.
  • the thickness of the layer was determined by weighing a calibration sample coated under the same conditions as the microspheres in the sputtering unit. Some coating variations, estimated to be ⁇ 30%, can occur among the 1000 microspheres used in the cell, however. Measurements with an Auger electron probe on selected microspheres confirmed the film thickness to be reasonable uniform ( ⁇ 20%).
  • the basis concept comes from the well known binding energy curve (Larmash) shown in Fig 5 which was derived (2nd ed.) from Introduction to Nuclear Engineering, by John R. Larmash, at pg. 29. If a light or heavier element with a lower binding energy per nucleon (BE/N) split into elements with a higher binding energy, the e in binding energy is released as excess energy from the reaction (the Q-value for the reaction). A positive Q-value represents, then, an exothermic (+Q) reaction, while a negative Q-value is associated with an endothermic (-Q) reaction.
  • Well known examples of this are fission, i.e. splitting of heavy elements into lighter ones, giving a positive, Q value and fusion, i.e.
  • the output power depends on differences between two large numbers, making it very sensitive to the transmutations occurring, i.e. to the starting material and the reaction conditions (e.g. loading, temperature, electrolyte, etc.). These factors affect the reaction channels and the balance of + versus - Q-values that result. The channels are also strongly dependent on the bead design and metals, plus the cell operating conditions. For example, in Run #2 of Table I, a multiple 2-layer coating of nickel and palladium was used to increase the excess power up to 4.5 watts vs. the 0.5 watt for Run #8, using a single film of nickel. Two important additional conclusions can be drawn from this example.
  • this reaction In order to create elements with mass numbers lying both above and below the base element A number, this reaction (presumed to be a fusion reaction), must lead to a heavier element of mass A (A>A for the base element) which then breaks up or "fissions" into fragments yielding the elements observed, i.e. representing the process by which transmutation occurs.
  • the heavier element undergoing fission will be termed the "compound nucleus”.
  • This breakup can be understood by analogy to the well- known process for neutron-induced fission. In that case, the compound neutron- uranium nucleus undergoes a binary breakup into two fragments, one light and one heavy mass element.
  • the sum of the mass numbers for the two fragments add up to the mass of the uranium plus neutron (less a small conversion to energy released by ⁇ MC 2 , Einstein's famous relation).
  • the present compound nucleus can be viewed as playing the role of uranium, and the fission breakup viewed in a similar fashion.
  • the output energy can be calculated from the mass difference between the compound nucleus and the fission products.
  • the creation of the compound nucleus from the proton plus base element consumes energy, so the net release is the mass difference between the initial reactants (e.g. proton plus Ni in Run #8) and all of the products. Indeed, that is the basis for the previous energetics calculations in Table VI.
  • the peak yield regions on the "sides" of each minimum point are viewed as the fission fragments that result from the breakup of the compound nucleus.
  • the compound nucleus must lie at an A value of ⁇ 80, 160, 320, 640/ .
  • the mix of products can be varied. For example, if a base element of mass A" with A" > 160 is used, the compound nucleus mass will lie above 160, i.e. 320, 640, . Then the fission of the compound nucleus will lead to an array of product elements with light-heavy pairs having mass sums equaling 320, 640," . This then predicts not only a number of standard elements as products, but some new stable heavy elements not yet identified.
  • time-averaged element production rates are computed in Table VIII and plotted in Figs 6a and 6b in terms of weight fraction of the metal film/s-cm 3 of film and atoms/s-cm 3 of film, respectively. These figures assume that the production rate was constant over the 310 hour run. There is some preliminary indication that the rate is higher at the start, and the time dependence, along with the effect of microsphere location, is now under study.

Abstract

Méthode pour provoquer des transmutations nucléaires à basse température, ces dernières se produisant pendant une électrolyse dans un milieu aqueux, à l'intérieur d'une cellule (12). Les nouveaux éléments obtenus par transmutation pendant le fonctionnement de la cellule ont une masse atomique à la fois plus élevée et plus faible que l'élément d'origine soumis à la transmutation. Un bon nombre de nouveaux éléments présentent également des modifications des abondances isotopiques naturelles. La cellule d'électrolyse (12) comporte un boîtier non conducteur (14) avec une entrée (54) et une sortie (56), ainsi qu'une première et une seconde grille conductrice (38, 44) placées dans le boîtier (14). Une pluralité de noyaux non métalliques, de préférence en polymère réticulé, dont chacun possède une surface extérieure conductrice métallique uniforme formée d'un matériau absorbant l'hydrogène tel qu'un matériau formant un hybride métallique, forment un lit (35) compact de perles conductrices (36) dans le boîtier (14), en contact électrique avec la première grille (38) adjacente à l'entrée (54). Le système (10) comporte une source d'alimentation électrique (15, 16) connectée de manière fonctionnelle à la première et à la seconde grille (38, 44), un courant électrique circulant entre les grilles (38, 44) et dans le milieu aqueux (59) qui traverse la cellule (12) pendant le fonctionnement de cette dernière.
PCT/US1997/012309 1996-07-09 1997-07-09 Elements a noyaux transmutes presentant des distributions isotopiques non naturelles obtenues par electrolyse, et methode de production WO1998003699A2 (fr)

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JP3520396B2 (ja) 1997-07-02 2004-04-19 セイコーエプソン株式会社 アクティブマトリクス基板と表示装置
JP3803342B2 (ja) * 1997-08-21 2006-08-02 セイコーエプソン株式会社 有機半導体膜の形成方法、及びアクティブマトリクス基板の製造方法
DE10032886A1 (de) * 2000-07-06 2002-01-17 Kent O Doering Verfahren und Vorrichtung zum Reduzieren von Radioaktivität
EP1509927A4 (fr) * 2002-05-17 2007-04-04 Oregon State Traitement de materiaux radioactifs avec des noyaux d'isotope d'hydrogene

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BE584834A (fr) * 1958-12-31 1900-01-01
US4316786A (en) * 1980-09-19 1982-02-23 The United States Of America As Represented By The United States Department Of Energy Apparatus for electroplating particles of small dimension
FR2596776B1 (fr) * 1986-04-03 1988-06-03 Atochem Cathode pour electrolyse et un procede de fabrication de ladite cathode
WO1990010935A1 (fr) * 1989-03-13 1990-09-20 The University Of Utah Procede et appareil de production de puissance
WO1990013129A2 (fr) * 1989-04-10 1990-11-01 Massachusetts Institute Of Technology Appareil de fusion
KR950009880B1 (ko) * 1989-10-16 1995-09-01 피. 쟈카랴야 챠코 원소와 에너지 생산방법
JPH05134098A (ja) * 1991-11-15 1993-05-28 Takaaki Matsumoto 水からの有用元素の製造方法
US5411654A (en) * 1993-07-02 1995-05-02 Massachusetts Institute Of Technology Method of maximizing anharmonic oscillations in deuterated alloys
US5318675A (en) * 1993-07-20 1994-06-07 Patterson James A Method for electrolysis of water to form metal hydride
US5580838A (en) * 1995-06-05 1996-12-03 Patterson; James A. Uniformly plated microsphere catalyst
US5494559A (en) * 1995-06-08 1996-02-27 Patterson; James A. System for electrolysis

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