WO1997040211A2

WO1997040211A2 - Electrolytic production of excess heat for transmutation

Info

Publication number: WO1997040211A2
Application number: PCT/US1997/005946
Authority: WO
Inventors: James A. Patterson; George H. Miley
Original assignee: Patterson James A; Miley George H
Priority date: 1996-04-10
Filing date: 1997-04-10
Publication date: 1997-10-30
Also published as: AU2663297A; WO1997040211A8

Abstract

An electrolytic cell (12), system (10) and method for producing excess quantities of heat as a result of low temperature nuclear transmutations which occur during electrolysis in an aqueous media within the cell (12). The electrolytic cell (12) includes a non-conductive housing (14) having an inlet (54) and an outlet (56) and spaced apart first and second conductive grids (38 & 44) positioned within the housing (14). 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 metallic hybride forming material, form a bed (35) of conductive beads (36) closely packed within the housing (14) in electrical contact with the first grid (38) adjacent the inlet (54). An electric power source (15, 16) in the system (10) is operably connected across the first and second grid (38 & 44) whereby electrical current flows between the grids (38 & 44) and within the aqueous media (59) flowing through the cell (12).

Description

SYSTEM, ELECTROLYTIC CELL AND METHOD

FOR PRODUCING EXCESS HEAT AND FOR

TRANSMUTATION BY ELECTROLYSIS

This is a continuation-in-part of provisional U.S. Application Serial No. 60/015,229 filed April 10, 1996.

This invention relates generally to electrolytic cells, and transmutation of elements and compounds and more particularly to an electrolytic cell and system for producing excess heat and for low temperature endothermic and exothermic nuclear transmutations in the presence of an aqueous media. The utilization of palladium coated microspheres or beads as a catalytic agent for the absorption of hydrogen is taught in prior U.S. patents 4,943,355 ('355) and 5,036,031 (O31). In these patents, the utilization of cross linked polymer microspheres forming an inner core and having a coating of palladium and other halide forming metals thereatop exhibit significant improvements in the level of hydrogen absoφtion and the absoφtion of isotopes of hydrogen.

Utilizing these catalytic microspheres led to the invention disclosed in U.S. patents 5,318,675 ('675) and 5,372,688 ('688) which teach an electrolytic cell, system and method for, inter alia, producing excess heat within a liquid electrolyte. More recently, U.S. patent 5,494,559 ('559) discloses an improvement in the layer structure of the catalytic microspheres or beads within an electrolytic cell. The combination of nickel/palladium layers enhance the production of excess heat within the liquid electrolyte.

In each of these prior '675, '688 and '559 U.S. patents, the electrolytic cell described therein included an inlet and an outlet facilitating the flow of the liquid electrolyte therethrough. Thus, as 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 an electrolytic cell, system and method for producing excess quantities of heat as a result of low temperature nuclear transmutations which occur during electrolysis in an aqueous media within the cell. 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. It is therefore an object of this invention to provide an improved electrolytic cell and system for producing excess heat and for transproducing transmutations by electrolysis.

It is yet another object of this invention to provide an improved electrolytic cell, system and method for producing low temperature nuclear transmutations by electrolysis in an aqueous media.

It is still another object of this invention to provide a method of producing both endothermic and exothermic transmutations generated simultaneously by electrolysis.

In accordance with these and other objects which will become apparent hereinafter, the instant invention will now be described with reference to the accompanying drawings.

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.

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. Referring now to the drawings, 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.

Still referring to Figure 1 is 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 54 of the cell 12 for better liquid electrolyte temperature control. 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 (ΔT) 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.

In Figure 2, the details of the electrolytic cell 12 utilized during testing procedures is there shown. A cylindrical glass or nylon non-conductive housing 14, open at each end, includes a moveable non-conductive end member 46 and 48 at each end thereof. These end members 46 and 48 are sealed within the housing 14 by O-rings 62 and 64. The relative spacing between these end members 46 and 48 is controlled by the movement of end plates 50 and 52 thereagainst.

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 5 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 l o 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. However, in the experiments reported herebelow, the inlet temperature of the liquid electrolyte was measured just outside of the cell 12 immediately upstream of stopper 54 to more 15 accurately reflect true temperature differential (ΔT) of the liquid electrolyte 59 while passing through the cell 12. Thus, all exposed surfaces to the liquid media are non- metallic except for the conductive beads and the conductive grid.

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

20 conductive foraminous or porous grid 38 formed of platinum and positioned transversely across the housing 14 as shown. These conductive beads 36 are described in detail herebelow.

Still referring to Figure 2, a non-conducive foraminous or porous nylon mesh 40 is positioned against the other end of these conductive particles 36 so as to retain 25 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. Against the other surface of this layer of non-conductive beads 42 is a conductive foraminous or porous grid 44 formed of platinum and positioned 30 transversely across the housing 14 as shown. Should the liquid electrolyte in the system 10 boil off or otherwise inadvertently be lost, a means of preventing system damage is preferred which 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. By this arrangement, when there is no electrolyte within the electrolytic cell 12, no current will flow between the electrodes 15 and 16.

ELECTROLYTE When the electrolytic cell 12 is filled with a liquid electrolyte 59, electric current will flow between the electrodes 15 and 16. 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 (¹H₂0) or heavy water and, preferably deuterium (²H₂0). The purity of all of the electrolyte components is of utmost importance. The water (¹H₂0) and the deuterium (²H₂0) 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 (Li₂S0₄) in a 0.5-molar mixture with deionized water and is of chemically pure quality having a resistance of 2 X 10^β ohms. In general, although a lithium sulfate is preferred, other conductive salts chosen from the group containing boron, aluminum, gallium, and thallium, as well as lithium, may be utilized. The preferred pH or acidity of the electrolyte is 9.0. CELL RESISTANCE

In preparing the electrolytic cells for testing, the cell resistance utilizing a

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.

CATALYTIC BEAD CONSTRUCTION A total of eight cell operational test runs are reported herebelow in Tables I and

II upon which this application is primarily based. The first test runs, 1, 2, 3 and 8 reported in Table I herebelow included beads designated as Ni-Pd-Ni beads which utilized a porous non-metallic and non-conductive styrene divinyl benzene core having a copper flash coating formed directly thereatop, followed by a nickel layer of uniform 1 μ thickness, a palladium layer of uniform 1 μ thickness and a second or outer nickel layer of uniform 1μ thickness. Run 7A used a bead construction having a plated layer of palladium on a sulfonated core built up to 1.0μ to 1.4μ, followed by a 0.6μ plated nickel layer. These layers were deposited by electroless plating, the details of which are fully described in U.S. Patent No. 5,580,838 issued December 3, 1996.

Catalytic beads utilized in the remaining test runs 4, 5, 6 and 8 were made using the technique of sputtering for the application of very thin, uniform layers atop the same styrene divinyl benzene core. For beads in these later test runs, nickel was sputtered directly atop the styrene core in preparation for direct adhesion of the first layer of sputtered nickel. Sputtering is preferred because coatings are very uniform, thin, and nearer to full density (about 80%). Moreover, sputtered layers load much faster, typically in as little as about ten minutes as opposed to 1 to 3 hours for plated layers.

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. 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. In general, 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.

Table I

Rur i Bead Input Power Total Delta Power Power Total No. Type Before Heat Run Temp. In Out Excess Production (Watts) (Watts) Energy

#1 Ni.Pd.Ni Plated 0.102WH 77 Hrs. 1.0°C 0.034 1.0 77WH, 277KJ

#2 Ni.Pd.Ni Plated 0.168WH 48 Hrs. 4.5°C 0.042 4.5 216WH, 778KJ

#3 Ni.Pd.Ni Plated 0.096WH 429 Hrs. 1.5°C 0.032 1.5 643Wh, 2.3E6J

#4 Ni.Pd.Ni 0.065WH 200 Hrs. 0.9°C 0.026 0.0 180WH, 554KJ Sputtered

#5 Ni,Pd,Ni,Pd,Ni 0.14WH 528 Hrs. 1.8°C 0.056 1.8 970WH, 3.5E6J Sputtered

#6 Ni,Pd,Ni,Pd,Ni 0.064WH 168 Hrs. 2.3°C 0.064 2.2 370WH, 1.3E6J Sputtered #8 Ni 0.072WH 288 Hrs. 1.05°C 0.072 1.0 290WH, 1.0E6J

Sputtered

Table II

Run #7A

Pd.Ni Clean Cell

(Plated)

Duration Bath Power Power Energy In Energy Oi

Day Hours Temp. In Watts Out Watts K Joules K Joule:

Day 1 24 Hrs. 24°C 0.176 .504 15.2 43.5

Day 2 25 Hrs. 50°C 0.156 9.4 13.47 807.8 Day 3 24 Hrs. 24°C 0.04 1.4 3.54 241.9

Day 4 24 Hrs. 24°C 0.024 2.5 2.07 216.0

Day 5 24 Hrs. 24°C 0.022 3.3 1.90 285.1

Day 6 24 Hrs. 24°C 0.54 4.5 4.6 390.5

Day 7 24 Hrs. 24°C 0.034 5.2 2.93 449.2 Day 8 24 Hrs. 24°C 0.034 2.4 2.94 207.3

Day 9 5 Hrs. 52°C 0.06 2.0 1.08 360.0

Total 197 Hrs. 47.73 3001.3

RELATIVE SURFACE AREAS 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). However, 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. CELL OPERATION RESULTS

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

(approx. .05 amps) is introduced across the conductive members, that current facilitated by the presence of the electrolyte 59 as previously described.

LOADING

During the initial loading, electrolysis of the aqueous media within the liquid electrolyte occurs so that the hydrogen active surface of the conductive particles fully absorbs and combines with hydrogen, i.e. becomes "loaded". This loading takes about two hours under a current flow through the cell of about 0.05 amps per two (2) cm³ of particle volume. As the particles load with hydrogen, the resistance of the cell will be seen to increase. The cell's resistance measured at constant temperature should be seen to raise about 10%. It is recommended that the loading should proceed at least until the resistance is no longer increasing. As loading proceeds further, a decrease in resistance will appear. TEST RUN

After hydrogen and/or hydrogen isotope, loading of the hydrogen active material of the conductive beads, 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. Preferably, and more accurately, in lieu of placing the thermocouple 70 as shown in Figure 2, the electrolyte inlet temperature was monitored immediately upstream of stopper 54 to more accurately reflect temperature differential (ΔT).

In general, all tabular results herebelow represent data taken on a steady state basis, input and output temperatures of the liquid electrolyte 59 being taken upstream of stopper 54 and at 72, respectively, voltage (v) and current flow (a) across the electrolytic cell 12 measured between terminals or conductors 15 and 16. The flow rate of the liquid electrolyte 59 (ml/min) and calculated wattage input and wattage output and percent yield are also shown. Wattage input to the cell 12 is calculated as the product of voltage (v) X amps (a), while wattage output is calculated based upon a formula for converting calorific heat to power and watts according to a formula -

Watts Out = Flow Rate (liters per minute) x ΔT x 70. As can be seen from these test results, in all cases, after initial loading of the catalytic particles within the cell, excess energy in the form of heated liquid media was found to be present in very significant quantities. Moreover, each of the test runs reported in Tables I and II produced excess heat over a very extended period of time. INITIAL BEAD ANALYSIS

After each of these test runs, 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.

Equipment used for mass spectral analysis was a Camica 5F (SIMS) Mass

Spectrograph and a Nuclear Activation Analysis System (NAA) developed by the

University of Illinois. For auger cutting into samples, an auger electro spectroscope

(AMS) by Perkin Elmer was utilized. A scanning electron microscope by Hatachi was also used for surface observation.

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. TEMPERATUREENDOTHERMIC

ANDEXOTHERMICTRANSMUTATIONS INBEADS

Results of the mass spectrograph analysis on one sample of unreacted beads sample from Test Run #2 are shown in Figure 3. A corresponding mass spectral analysis of the reacted beads from the same cell from Test Run #2 are shown in Figure 4. Each of these sets of mass spectral analysis process data was taken at the University of Illinois and, as reported in more detail in the paper entitled Nuclear Transmutations in Thin-Film Nickel Coatings Undergoing Electrolysis, by George H. Miley and James A. Patterson presented at the 2nd Intemational Conference on Low Energy Nuclear Reactions, Texas A & M, College Station, Texas.

An example of a more thorough analysis of this processed data is shown in 5 Tables 111 and IV 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 l o cannot be attributed to impurity entering the coating. These exact amounts of select isotopes before and after running were determined by Neutron Activation Analysis. Again, the large increase in element concentration after a run indicates production in the cell as opposed to impurity.

In summary, the test results conducted at the University of Illinois and reported

15 more completely in the above-referenced paper delivered at Texas A & M clearly establish the existence of nuclear reaction products which have occurred at room or low temperature and without any evidence of high energy radioactive emissions.

ELEMENT DEPTH PROFILES

Data from an Auger Electron Scan (AES) profile measurement on a typical microsphere are presented in Table V herebelow for the higher concentration elements. While the isotopes' profile behaviors are hard to interpret quantitatively,

5 several observations can be made. Most profiles peak in the nickel volume or near the film-plastic interface, suggesting an internal source rather than diffusion in from the surface. For example, the key elements Ag and Fe peak near the Ni-plastic interface, (at '650 A corresponding to about 12 min. sputtering time). Cu peaks further out in the film. While this data strongly infers an internal source, amplitude of i o the peaks is too small to draw quantitative conclusions about an internal source versus diffusion inward from the electrolyte. This depth profile data, however, shows that contamination from the surface was impossible.

TABLE V Tabulated atomic % vs. Depth from AES Scan

15

Approximate 0 100 700 2000

Depth (A)

Relative Atomic %

20

C 20.00 _ _ 61.23

Ag 2.68 9.94 11.77 3.07

Fe 7.72 10.02 10.45 5.12

Ni 9.99 12.30 22.28 12.56

25 Cu 4.17 7.64 7.61 5.38

Zn 11.12 10.48 9.22 -

Mg 10.78 13.75 - -

Cr - - 3.66 4.00

30 VERIFICATION OF TRANSMUTATION RESULTS

The Illinois Waste Management and Research Center recently conducted an independent study of the unreacted and reacted bead samples from one test run similar to Test Run #8 reported hereinabove. The report concluded that several anomalous metals were observed in a cell identical to that used in Test Run #8, a

35 clean cell. These anomalous metals were not present in the unreacted bead specimens tested. Further, other elements were in both unreacted and reacted beads, but the concentrations observed in the reacted specimens were, in some cases, orders of magnitude greater than that of the starting material. The report went on to conclude that several elements including Ga, U, W, Zr, Th were present that normal sources of contamination simply cannot account for. A complete copy of this report is attached hereto and made a part hereof as Exhibit A.

ENERGETICS OF TRANSMUTATIONS The energetics of the cell operation can be explained as follows. The array of elements observed in the metal film after a run are attributed to nuclear transformations induced by light ion (e.g. H, D, ...) absorbed in the metal film (e.g. Ni in run # 8). For the metals selected, the ratio of absorbed ions to metal ions can approach unity. According to other studies using flat plate electrodes, a high loading of this type is necessary and this requirement seems reasonable for the present thin film case. Indeed, the loading is observed qualitatively in the experiment by following the voltage change during the initial hour of the run. After the run, a large number of new elements attributed to the transmutation reactions are observed. Knowing the yields of these elements, it is possible to calculate the energy released by the reactions without specifying the detailed reaction channels. This calculation can be illustrated from run # 8 that used Ni films. 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. fusing together of lighter elements to give heavier ones, again with a positive Q value. Thus, fission on Fig 5 proceeds from high mass numbers on the right of the curve to the middle, giving higher BE/N products, while fusion goes from low mass numbers on the left to the center region of the curve, again increasing the BE/N. The case of Run #8 used as an example of the various test runs, where the starting point is Ni (mass no. = 58), is more difficult to analyze since Ni lies near to, but not quite at, the top of the BE/N curve. Thus when the array of products observed occur, some have slightly higher BE/N (giving a positive contribution to the Q-value) while others result in a lower BE/N (negative contribution). Thus a careful accounting of the BE/N for the various products is necessary. Such an accounting is shown in Table VI herebelow.

Table VI Energy - Mass Balance for Ni Run #8

Element Atomic A z BE/atom Afm Fraction Contrib.

Fraction (keV) x BE/Atom BE-BE Ni

(from NAA) (Q)

Al 0.0051 27 13 224951.95 1147.254945 _

Ag 0.0661 107 47 915266.2 60499.09582 +

Cr 0.0594 52 24 456345.1 27106.899 -

Fe 0.1453 56 26 492253.89 71524.49051 -

Ni (reacting) 0.377 58 28 506453.84 190933.1 0 (ref.)

Cu 0.0796 63 29 551381.25 43889.94758 +

V 0.0001 51 23 445840.83 44.5840828- -

Co 0.001 59 27 517308.11 517.308113 +

Zn 0.0204 64 30 559093.59 11405.50913 +

H (reacting) 0.377 1 1 0 0

Total 0.377 216135.0892

Delta BE/atm = sum BE/atm products - Sum BE/atm reactants = 25201 V/atm reacted

Total watts per cell = Delta BE/atm x atms reacted/sec in Run #8 = 0.302 watts

Note: all binding energies are from Brockhaven National Laboratory's Nuclear Data Center

In this table, the eight large yield product elements from NAA analysis are used. The added elements from SIMS will change the analysis, but the trends will remain and that is the point of this example. Their respective BE atom are multiplied by the observed atom fraction in the film after the run; the result is then summed and the Ni BE subtracted to obtain the net energy released (overall Q- value) per atom reacting. Note from the "contributions" column that various of the elements have BE atm lying both above and below Ni. As seen, four elements have a (+) contribution to the BE/atom (i.e. to the Q-value) while four give (-) contributions. The energy released is then converted to an average power output for Run #8 using the run time of 311 hours and the number of atoms in the

Ni film (see Texas AM Paper). A positive output of 0.3 watts is found, in good agreement with the 0.5 watt + 0.5 watt observed in the experiment. This calculation then demonstrates that the observed excess power can be accounted for in a straightforward manner by summing the (+) and (-) Q- values for the various nuclear transmutation reactions involved. The fact that both (+) and (-) Q-value reactions occur in such cells had not been realized prior to this discovery. Clearly, as seen from Table IV, 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. First, other experimenters have had difficulty with reproducibility of excess power (heat) experiments using a variety of "other" cell configurations, typically with flat plate type electrodes. In view of the example above, this is understandable. Just small differences in set up can throw the positive vs. negative Q balance off, causing this non-reproducibility. On the other hand, even when non-measurable excess power is observed, transmutations can occur, allowing the detection of products possible without excess heat. In this sense, transmutation experiments are not so sensitive to conditions and this is viewed as the reason the present experiments (e.g. Runs #8 and #18c) are reasonable reproducible.

A second point is that, recognizing the delicate Q-value balance involved in production of excess power, and knowing the various products obtained from different starting materials as obtained in the present experiments, it becomes possible to tailor bead designs/operating conditions to maximize heat production or to emphasize certain transmutation products. The multi-layer run cited earlier is only one example of applying this knowledge.

While the instant invention has been shown and described herein in what are conceived to be the most practical and preferred embodiments, it is recognized that departures may be made therefrom within the scope of the invention, which is therefore not to be limited to the details disclosed herein, but is to be afforded the full scope of the claims so as to embrace any and all equivalent apparatus and articles.

Claims

CLAIMSWhat is claimed is:

1. A system for producing endothermic and exothermic low temperature nuclear transmutations occurring within an electrolytic cell of said system, comprising: said electrolytic cell including a non-conductive housing and an inlet and an outlet; a plurality of conductive beads each including: a non-conductive core; a uniform thin conductive layer of a metallic material forming a conductive surface over said non-conductive core, said metallic material being a metallic hydride which combines with hydrogen or an isotope of hydrogen during operation of said system; a first conductive porous grid means in electrical communication with said plurality of conductive beads; a second conductive porous grid means electrically spaced from said plurality of conductive beads and which is positioned closer to said outlet than said first conductive grid; means for pumping a liquid electrolyte into said electrolytic cell through said inlet, said electrolyte having a conductive salt in solution with water, said electrolyte exiting from said electrolytic cell through said outlet; means for applying an electric current between said first and second conductive grid means.

2. A system as set forth in Claim 1 , wherein: said metallic hydride is taken from the group consisting of palladium, lanthanum, praseodymium, cerium, titanium, zirconium, vanadium, tantalum, uranium, hafnium, and nickel.

3. A system as set forth in Claim 1 , wherein: said conductive layer is relatively high in density and is formed by sputtering.

4. A system as set forth in Claim 1 , wherein: said exothermic transmutations produce more heat than said endothermic transmutations absorb wherein said system produces excess heat.

5. A system as set forth in Claim 4, wherein: said conductive layer has a uniform thickness in the range of about 500 to 5 1000 angstroms.

6. An electrolytic cell for producing useful amounts of excess heat and for producing low temperature nuclear transmutations within said cell comprising: a non-conductive housing; a plurality of conductive beads each including: 0 a first nickel layer of uniform thickness formed atop a non-conductive core; a palladium layer of uniform thickness formed atop said first nickel layer and having high hydrogen adsorption capabilities; a second nickel layer of uniform thickness formed atop said palladium 5 layer; a first conductive porous grid means in electrical communication with said plurality of conductive beads; a second conductive porous grid means electrically spaced from said plurality of conductive beads and positioned closer to said outlet than o said first conductive grid means.

7. A cell as set forth in Claim 6, wherein each said conductive bead further comprises: a second palladium layer of uniform thickness formed atop said second nickel layer; 5 a third nickel layer of uniform thickness formed atop said second palladium layer.

8. A cell as set forth in Claim 7, wherein: said palladium layers and said nickel layers are formed by sputtering and are of high density and highly uniform.

9. A method for producing useful excess heat and for producing low temperature nuclear transmutations within an aqueous media flowing through an electrolytic cell comprising the steps of:

A. providing said electrolytic cell including: a non-conductive housing and an inlet and an outlet; a first conductive porous grid positioned within said housing adjacent to said inlet; a second conductive porous grid positioned within said housing spaced from said first conductive grid and adjacent to said outlet; a plurality of conductive beads each including: a non-conductive core; a uniform thin conductive layer of a metallic material forming a conductive surface over said non-conductive core, said metallic material being a metallic hydride which combines with hydrogen or an isotope of hydrogen during operation of said cell;

B. circulating said aqueous media through said electrolytic cell;

C. passing an electrical current between said first and second grids when said aqueous media is circulating within said electrolytic cell;

D. removing heat from said aqueous media for use external to and separate from said electrolytic cell after said aqueous media exits said electrolytic cell through said outlet.

10. A method of producing useful excess heat and of transmutation by electrolysis in an aqueous media comprising the steps of:

A. providing an electrolytic cell including: a non-conductive housing and an inlet and an outlet; a first conductive porous grid positioned within said housing adjacent to said inlet; a second conductive porous grid positioned within said housing spaced from said first conductive grid and adjacent to said outlet; a plurality of conductive beads each including: a non-conductive core; a uniform thin conductive layer of a metallic material forming, a conductive surface over said non-conductive core, said metallic material being a metallic hydride which combines with hydrogen or an isotope of hydrogen during operation of said system;

B. circulating said aqueous media through said electrolytic cell;

D. removing heat from said aqueous media for use external to and 0 separate from said electrolytic cell after said aqueous media exits said electrolytic cell through said outlet.

11. A system for low temperature nuclear transmutation by electrolysis in an aqueous media, comprising: an electrolytic cell including a non-conductive housing and an inlet and an 5 outlet; a plurality of conductive beads each including: a non-conductive core; a uniform thin conductive layer of a metallic material forming a conductive surface over said non-conductive core, said metallic 0 material being a metallic hydride which combines with hydrogen or an isotope of hydrogen during operation of said system; first conductive porous grid means in electrical communication with said plurality of conductive beads; a second conductive porous grid means electrically spaced from said 5 plurality of conductive beads and which is positioned closer to said outlet than said first conductive grid means; means for pumping said liquid electrolyte through said electrolytic cell, said liquid electrolyte including a conductive salt in solution with water; means for applying an electric current between said first and second o conductive grid means.

12. A method of low temperature nuclear transmutation to produce excess heat by electrolysis in an aqueous media comprising the steps of:

A. providing an electrolytic cell including: a non-conductive housing and an inlet and an outlet; a first conductive porous grid positioned within said housing adjacent to said inlet; a second conductive porous grid positioned within said housing spaced from said first conductive grid and adjacent to said outlet; a plurality of conductive beads each including: a non-conductive core; a first nickel layer of uniform thickness formed atop a non¬ conductive core; a palladium layer of uniform thickness formed atop said first nickel layer and having high hydrogen adsorption capabilities; a second nickel layer of uniform thickness formed atop said palladium layer;

B. circulating said aqueous media through said electrolytic cell;

C. passing an electrical current between said first and second grids when said aqueous media is circulating within said electrolytic cell.