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Time for the new business plan here,
now that the market has digested the cancellation of the port facility. No cash! Credit crunch strikes again.
kermit: seems like it
I don't think it will be sub-penny by Friday's close.
Chlorides:
"A chemical compound containing chlorine. Most chlorides are salts that are formed either by direct union of chlorine with a metal or by reaction of hydrochloric acid (a water solution of hydrogen chloride) with a metal, a metal oxide, or an inorganic base. Chloride salts include sodium chloride (common salt), potassium chloride, calcium chloride, and ammonium chloride. Most chloride salts are readily soluble in water, but mercurous chloride (calomel) and silver chloride are insoluble, and lead chloride is only slightly soluble. Some chlorides, e.g., antimony chloride and bismuth chloride, decompose in water, forming oxychlorides. Many metal chlorides can be melted without decomposition; two exceptions are the chlorides of gold and platinum. Most metal chlorides conduct electricity when fused or dissolved in water and can be decomposed by electrolysis to chlorine gas and the metal. Chlorine forms compounds with the other halogens and with oxygen; when chlorine is the more electronegative element in the compound, the compound is called a chloride. Thus, compounds with bromine and iodine are bromine chloride, BrCl, and iodine chloride, ICI, but compounds with oxygen or fluorine (which are more electronegative than chlorine) are oxides (e.g., chlorine dioxide, ClO2) or fluorides (e.g., chlorine fluoride, ClF) respectively. Many organic compounds contain chlorine, as is indicated by common names such as carbon tetrachloride, methylene chloride, and methyl chloride. However, in the nomenclature system for organic chemistry adopted by the International Union of Pure and Applied Chemistry (IUPAC), the presence in a compound of chlorine bonded to a carbon atom is indicated by the prefix or infix chloro; thus, carbon tetrachloride is tetrachloromethane, methylene chloride is dichloromethane, and methyl chloride is chloromethane.
Chloride is a salt compound resulting from the combination of the gas chlorine and a metal. Some common chlorides include sodium chloride (NaCl) and magnesium chloride (MgCl2). Chlorine alone as Cl2 is highly toxic, and it is often used as a disinfectant. In combination with a metal such as sodium it becomes essential for life. Small amounts of chlorides are required for normal cell functions in plant and animal life.
Environmental Impact:
Chlorides are not usually harmful to people; however, the sodium part of table salt has been linked to heart and kidney disease. Sodium chloride may impart a salty taste at 250 mg/l; however, calcium or magnesium chloride are not usually detected by taste until levels of 1000 mg/l are reached. Public drinking water standards require chloride levels not to exceed 250 mg/l.
Chlorides may get into surface water from several sources including:
* rocks containing chlorides,
* agricultural runoff,
* wastewater from industries,
* oil well wastes, and
* effluent wastewater from wastewater treatment plants.
Chlorides can corrode metals and affect the taste of food products. Therefore, water that is used in industry or processed for any use has a recommended maximum chloride level. Chlorides can contaminate freshwater streams and lakes. Fish and aquatic communities cannot survive in high levels of chlorides."
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IT SOUNDS LIKE ECCI'S TECHNOLOGY WILL WORK TO REMOVE CHLORIDES- THE PRINCIPLE POLLUTANT IN BARNETT SHALE "FRAC WATER", BUT WHY NOT CONFIRM IT IN A PRESS RELEASE, MR. WARD AND MR. ADAMS????
(END OF RANT)
Here is ECCI's technology:
Sold to ECCI by license on September 11, 2002:
http://sec.edgar-online.com/2003/07/29/0001010549-03-000399/Section13.asp
But what is needed is the revelation of how it works on Barnett Shale "frac water":
US Patent #238546 Electrochemical treatment of effluent water
Patent Drawings: Loading
Inventor: Knieper, et al.
Date Issued: May 29, 2001
Application: 09/284,519
Filed: July 23, 1999
Inventors: Knieper; Louis H. (Houston, TX)
Noyes; Daniel G. (Houston, TX)
Tipton; Gary A. (Houston, TX)
Assignee:
Primary Examiner: Phasge; Arun S.
Assistant Examiner:
Attorney Or Agent: Harrison & Egbert
U.S. Class: 204/269; 204/270; 204/275.1; 205/742; 205/759; 205/760; 205/761
Field Of Search: 205/742; 205/759; 205/760; 205/761; 204/269; 204/270; 204/275.1
International Class:
U.S Patent Documents: 4036726; 4329211
Foreign Patent Documents:
Other References:
Abstract: An apparatus (200) for the treatment of effluent including a chamber (210) having an inlet (212) and an outlet (252), a plurality of plate-type electrodes (211) extending vertically in the chamber (210), and an electrical supply connected to the plurality of plate-type electrodes (211). The plurality of plate-type electrodes (211) define a plurality of channels extending within the chamber (210). Each of the plurality of channels occurs between adjacent electrodes (211). The plurality of electrodes (211) are positioned between the inlet (212) and the outlet (252). The electrical supply delivers electricity of a first polarity to a first set of a plurality of electrodes (211). The electrical supply delivers electricity of an opposite polarity to the second set of electrodes (211).
Claim: What is claimed is:
1. An apparatus for treatment of effluent water comprising:
a chamber having an inlet means and an outlet means;
a plurality of plate-shaped electrodes extending in said chamber, said plurality of plate-shaped electrodes defining a plurality of channels extending within said chamber, each of said plurality of channels occurring between adjacent electrodesof said plurality of plate-shaped electrodes, said plurality of plate-shaped electrodes positioned between said inlet means and said outlet means, each of said first set of said plurality of plate-shaped electrodes comprising a flat plate of conductivematerial extending vertically within said chamber, each of said second set of said plurality of plate-shaped electrodes comprising a corrugated plate of conductive material extending vertically within said chamber; and
electrical means connected to each of said plurality of plate-shaped electrodes, said electrical means for delivering electricity of a first polarity to a first set of said plurality of plate-shaped electrodes, said electrical means fordelivering electricity of an opposite polarity to a second set of said plate-shaped electrodes, said first set being in alternating relationship with said second set such that an electrode of said first set extends between adjacent electrodes of saidsecond set and such that an electrode of said second set extends between adjacent electrodes of said first set, said inlet means for delivering effluent to said plurality of channels, said outlet means for passing treated effluent from said plurality ofchannels.
2. The apparatus of claim 1, said chamber comprising:
an entry chamber having an inlet means affixed thereto;
a treatment section positioned above said entry chamber in fluid communication therewith, said plurality of plate-shaped electrodes extending generally vertically in said treatment section; and
an outlet chamber positioned above said treatment section in fluid communication therewith, said outlet means being connected to said outlet chamber.
3. The apparatus of claim 2, said entry chamber having a solid outlet means formed thereon, said solid outlet means positioned below said inlet means, said solid outlet means for removal of sludges and solids from said entry chamber.
4. The apparatus of claim 3, said entry chamber having a downwardly tapered section extending below said inlet means, said solid outlet means positioned at a bottom of said tapered section.
5. The apparatus of claim 2, said outlet chamber comprising a gas release means positioned thereon, said gas release means for passing a gas from an interior of said outlet chamber.
6. The apparatus of claim 1, each of said second set of said plurality of plate-shaped electrodes comprising a corrugated plate of conductive material extending vertically within said chamber.
7. The apparatus of claim 1, said electrical means comprising:
a power supply having a first lead connected to said first set and a second lead connected to said second set.
8. The apparatus of claim 1, further comprising:
polarity reversal means connected to said first and second leads for periodically reversing the polarity of electricity passing through said first set and said second set.
9. The apparatus of claim 1, each of said first set of said plurality of plate-shaped electrodes being connected to another of said first set by a first conductive strap, each of said second set of said plurality of plate-shaped electrodes beingconnected to another of said second set by a second conductive strap, said first lead electrically connected to said first strap, said second lead electrically connected to said second set.
10. The apparatus of claim 1, said electrical means for passing electricity of constant amperage to said plurality of plate-shaped electrodes.
11. The apparatus of claim 1, said inlet means comprising:
an entry hole formed at a lower end of said chamber;
a conduit connected to said entry hole; and
a pump means connected to said conduit for passing effluent at a constant flow rate to said entry hole.
12. The apparatus of claim 1, said outlet means comprising:
an outlet hole formed at an upper end of said chamber;
a conduit connected to said outlet hole for passing treated effluent from said chamber; and
a coalescence tank connected to said conduit.
13. A method of treating an effluent comprising the steps of:
forming a first set of plate-shaped electrodes, each of said first set being a flat plate of conductive material; and
forming a second set of plate-shaped electrodes, each of said second set being a corrugated plate of conductive material, each plate-shaped electrodes of said second set being sandwiched between adjacent pairs of plate-shaped electrodes of saidfirst set;
passing an effluent between said first set of plate-shaped electrodes and said second set of plate-shaped electrodes;
applying electricity of a first polarity to said first set of plate-shaped electrodes and of an opposite polarity to said second plate-shaped electrodes as the effluent passes therebetween said step of applying electricity comprising:
applying direct-current electricity of an amperage of between 20 and 60 amps and a voltage of between 5 and 30 volts, said amperage being constantly applied; and
reversing the polarities to said first and second sets of plate-shaped electrodes periodically as the effluent passes therebetween; and
moving the effluent from the electrodes to a coalescence tank.
14. The method of claim 13, further comprising the steps of:
coalescing the effluent in the coalescence tank so as to form a discrete layer of immiscible liquid in said tank; and
separating the discrete layer from the effluent.
15. The method of claim 13, further comprising the step of:
pumping the effluent at a constant flow rate of between 20 to 30 gallons per minute into a vertical chamber containing the first plate-shaped electrode and the second plate-shaped electrode, said effluent having a pH of between 4 and 9 and atemperature of between 40.degree. F. and 180.degree. F.
16. The method of claim 13, further comprising the steps of:
forming a chamber having an inlet adjacent a lower end and an outlet adjacent an upper end of said chamber, said chamber extending vertically;
positioning said first plate-shaped electrode and said second plate-shaped electrode between said inlet and said outlet in said chamber; and
passing the effluent vertically upwardly within said chamber such that the effluent passes between said first and second plate-shaped electrodes.
Description: TECHNICAL FIELD
The invention relates to the electrochemical treatment of effluent water to remove suspended solids and dissolved particles and provide discharge water within environmental requirements. The invention includes design of an electrochemical cellsuitable for such treatment.
BACKGROUND ART
A wide variety of chemical and mechanical processes have been developed in an effort to control pollution from effluent streams in various industries. Impurities in the streams include suspended solids and dissolved particles. Both chemical andmechanical methods have been employed to cause the impurities to coalesce to permit removal by filters, centrifuges, separators, and clarifiers. The goal of the processes is to remove sufficient impurities to allow the effluent liquid to be dischargedinto the environment with an acceptable amount of adverse impact.
Efforts to treat water by use of electricity to coalesce and remove impurities have existed for many years. One such effort is disclosed in U.S. Pat. No. 5,271,814 which issued to David M. A. Metzler, on Mar. 19, 1992.
Past efforts to achieve coalescence of contaminants in effluent streams without the use of added chemicals have met with some success, but have also had problems with efficiency, cost, flexibility and disposal of the coalesced materials. Inaddition, many systems require batch processing rather than continuous processing. Accordingly, there is a need for a novel system which can remove impurities from effluent streams and can operate as a continuous process.
SUMMARY OF THE INVENTION
Water with dissolved, suspended, or disbursed contamination is introduced into a treatment cell which contains a plurality of plate-type electrodes forming long narrow channels in a chamber through which the contaminated water must flow. Alternate electrodes may have surface irregularities, such as slight corrugations, running perpendicular to the direction of water flow. Such irregularities disrupt laminar flow of the liquid and permit an electron flux to concentrate along the ridgesnearest the adjacent plates for increased intensity of electron flow. Such irregularities are preferred for treatment of an effluent with high amounts of contamination. The water moves perpendicular to the flow of electricity. Water flow and electronflow (amperage) are kept constant for a given application. Voltage is allowed to fluctuate based on the instantaneous conductivity of the water. This input of energy to the contaminated water causes a number of physical and chemical reactions to takeplace which destabilize the contaminated water and cause the contaminants to change form to aid in their removal from the water.
BRIEF DESCRIPTION OF -THE DRAWINGS
FIG. 1 is a front elevational view of a treatment cell in accordance with the invention.
FIG. 2 is a side elevational view of the treatment cell shown in FIG. 1.
FIG. 3 is an alternative form of the entry chamber shown at the bottom of FIG. 1.
FIG. 4 is a top view of the outlet chamber shown at the top of FIG. 1.
FIG. 5 is a sectional view taken through the treatment chamber of FIG. 1.
FIG. 6 is an exploded view of the electrode plates which fit in the treatment cell of FIG. 1.
FIG. 7 is a side view of treatment cells in accordance with the invention.
FIG. 8 is a top view of the cells shown in FIG. 7.
FIG. 9 is an end view of the cells shown in FIG. 7.
FIG. 10 is a schematic drawing of a process utilizing the electrochemical treatment cells in accordance with the invention.
FIG. 11 is a frontal partially cross-sectional view of an alternative embodiment of the treatment cell in accordance with the present invention.
FIG. 12 is a detailed view of the entry chamber of the alternative embodiment of the present invention.
FIG. 13 is a cross-sectional plan view showing the arrangement of electrodes within the interior of the treatment cell of the alternative embodiment of the present invention.
FIG. 14 is a detailed view of the connection of the outlet chamber and the treatment cell of this alternative embodiment of the present invention.
DETAILED DESCRIPTION OF THE INVENTION
With reference to FIGS. 1 and 2, water with dissolved, suspended, or dispersed contamination is introduced into treatment cell 10 of chamber 11 at a constant flow rate through an entry 12 at the bottom of the chamber 11. Prior to entry, pH ofthe water for treatment may need to be adjusted to attain the desired treating reactions and changes in form. A pH between 4 and 9 is generally preferable although a pH commonly used is about 5. At a pH of about 5, H+ and OH- radicals can be generatedwith relative ease. The temperature of the effluent should also be controlled either before or after treatment to a range between about 40.degree. F. and 180.degree. F. Outside of this temperature range flocculation is more difficult.
The entry 12 may be a pipe, opening, orifice, nozzle, valve, or other device as suits the application of the technology. The contaminated water enters an entry chamber 14 that functions to reduce velocity and to distribute the flow across therectangular cross section of the treatment section 20 of the chamber 11. The dimensions of the entry chamber 14 are critical for its function and limit the flow rate to a minimum of 20 gallons per minute and a maximum of 30 gallons per minute. Thebottom of entry chamber 14 has a taper 16 to an outlet 18 that is operated by an external valve. Solids and sludges separated in the chamber 14 are collected and directed to the external valve for periodic removal by this design. FIG. 1 and FIG. 3 showconfigurations of the tapered section 16. An angle of about 60.degree. has been found suitable for the tapered section 16.
Water conditioned in the entry chamber 14 is caused to flow upward into the treatment section 20 of the chamber 11. This treatment section 20 is about four feet long with internal dimensions of about thirty-two square inches. These dimensionsare proportionalities and cannot be independently altered, but other dimensions can be employed. The surface area of the plates and the flow rate past them must be balanced to achieve the desired amount of destabilization prior to subsequentcoagulation. The treatment section 20 may be either round or rectangular tube constructed of a nonconductive, rigid material such as fiberglass, PVC, or stainless steel with a non-conductive liner or coating. Opposite long sides contain grooves 22 (asshown in FIG. 5) for the length of the section 20 to form an electrode rack. These parallel grooves 22 hold plate-type electrodes 24 and 26 (as shown in FIG. 6) forming long thin channels between the electrodes through which the contaminated water mustflow. With the integral support rack or structure having the opposite surfaces with parallel grooves, electrodes can be readily removed and replaced to facilitate exchange or cleaning. Electrochemical treatment occurs in the long thin channels betweenthe plates. Flow rates through a single cell 10 depend on size but generally are between about 20 and about 30 gallons per minute, preferably 25 gallons per minute, for a cell with a cross-sectional area of 30-60 square inches.
The top inside dimensions of the entry chamber are designed smaller than the width of electrodes 24 and 26 to support the electrodes within the treatment section 20. Other suitable supports could also be used. The entry chamber 14 has aperipheral flange 17 which is held together by bolts 21 to a peripheral flange 19 on the outer bottom surface of the treatment section 20. A gasket may be used to seal between the flanges 17 and 19.
A stable, controlled direct electrical current (DC) is introduced to the treatment section through the electrodes. Flat plate electrodes 24 are physically connected across the top by welding or electrically connecting a strap 27 of similarmaterial across a projection 28 on one end of the row of plates 24. Corrugated plate electrodes 26 are welded or electrically connected across projections 30 on the other side to a similar strap. These straps 27 and 31 are connected to electrical wires32 and 34 and serve as electron flow distribution units to distribute the electrical current to and from the plate electrodes 24 and 26. An extension from each connecting strap 27 and 31 may extend through the external shell of the section to allowoutside dry contact with the electrical power. Alternating electrodes 26 have an irregular surface caused by slight corrugations running perpendicular to the water flow. These corrugations are preferably sinusoidal in shape. These corrugations 36 maybe created by alternately deflecting the plate back and forth to form furrows or ridges. Although the deflections are slight, they achieve two purposes critical to successful treatment. The perpendicular corrugations 26 disrupt laminar flow whichallows for complete contact and treatment. The corrugations 26 also concentrate the electron flux along the ridges for increased intensity of discharge. Electrode plates of opposite polarity are very close together along each corrugation. Theelectrode plates are 5/16" and 13/16" between the centerlines and each plate is 1/8" to 1/4" thick.
Within each chamber formed by the electrodes and cell walls of the treatment section 20, the flow of water moves perpendicular to the flow of electricity in a counter current fashion, i.e., water enters the bottom and electricity enters the top. Water flow and electron flow (amperage) are kept constant for a given application. Voltage is allowed to fluctuate based on the instantaneous conductivity of the water. This input of energy to the contaminated water causes a number of physical andchemical reactions to take place which destabilize the contaminated water. Voltage and current are adjustable to select the best flow for a specific waste stream. Voltages are generally maintained between about 5 and about 30 volts with current flowacross a cell being maintained between about 20 and about 60 amps, assuming cells of a size described above. An individual cell normally contains about 14 to 16 alternating electrodes within an electrode rack about 63/4" across. Voltage and current canbe controlled with conventional electric controllers, such as rheostats and rectifiers.
The current between electrodes should be direct current in one direction, although a square wave voltage may be employed for some applications. The polarity between the electrodes should be reversed periodically, e.g., between one and fiveminutes to avoid electrochemical plating. In general, systems with metal ions in the effluent require faster reversal of polarity to avoid plating. The current should be in one direction as long as possible but shorter than the time for plating to besignificant. Under load, a mercury vapor switch with a minimum life of 3,000,000 cycles is preferred for the current flow involved.
An alternative to switching with mercury vapor switches is with a center tap transformer and a SCR bridge rectifier. One pair of SCR diodes are turned off during a switching cycle. This combined with the center tapped transformer will allowsolid-state switching.
To minimize side lobes and spiking associated with abrupt changes in the current flow, the AC current is ramped down prior to switching and ramped back up after the switching. A second dampening transformer is used to further minimize spiking. The second transformer acts as a surge suppressor by providing a counter flow current during the switching operation.
A blending and equalization chamber 38 is formed by a cap 40 at the top of the cell 10 (as shown in FIG. 4). Cap 40 has a peripheral flange 41 which is held against a peripheral flange 43 around the top of the treatment chamber 20 by bolts 45. A gasket may be used to seal between the flanges 41 and 43. Blending chamber 38 receives water as it leaves the treatment section 20 of the cell 10 in a vertical direction. In this chamber 38, gases from the electrical treatment may be captured andvented from the vertical flow. Gases are derived from carbonates, nitrogenous compounds, halogenated compounds, chlorides, and hydrolysis of the water. Usually these are released in small amounts in this chamber 38. The chamber 38 also serves toequalize pressure within the system and minimize the swelling effect caused by the electrical treatment. A valve 47, such as a check valve, may be located on the cap 40 to allow gases to escape.
Treated and destabilized water is transported through treated water outlet 42 from the chamber 11 to a manifold (not shown) that collects effluent from a plurality of cells and conveys the treated water to a holding tank for coalescence where thedestabilized water is allowed to attain a modified equilibrium. The contaminants coalesce and agglomerate around charged nuclei and create either globules or floc. The imbalance continues to cause reaction and even delayed redox reactions may occur inthe coalescence tank of the system. Through natural mechanisms, globules in the water will continue to coalesce and will form a discrete layer of immiscible liquid that will rise to the top or sink to the bottom based on its density. Flock particlesagglomerate until the charged and imbalanced system has come to equilibrium. The floc sinks or floats based on the density of the contaminate.
As the water leaves the coalescence tank, it has been treated and impurities have been removed. Floating scum and settled sludge will contain impurities which may be removed by conventional means and disposed of appropriately.
The most direct result of the treatment on contaminants is the disruption of the Stern's layer of charges that keep suspended particles apart and dispersed throughout the water. Colloids and minute particles can then attach to each otherreaching a critical mass for separation. In addition, some particles may have an induced static charge that causes them to be attracted to opposite charged particles. Along similar lines, the polar water molecules may be affected by the electric fieldcausing a new alignment that reduces affinity for suspended materials. The new system is effective for both hydrophilic and hydrophobic suspensions.
A second result of the electrical current in the contaminated water is the alteration of the molecules and atoms due to the presence of the electrons. Reduction occurs at the cathode causing some materials to become less soluble or to achieve aneutral valence state. At the anode, oxidation may occur due to the stripping of electrons. In addition, at the anode, metal ions may be released leading to complexing and floc nuclei formation. Certain elements and compounds that exist as relativelystable ionic species may be crated by substitution or stripping in the electronic field (chlorine stripping of chlorinated hydrocarbons).
In addition to the alterations of the redox equilibrium within the treatment cell, hydrolysis is also taking place. Hydrogen, oxygen, and hydroxyl liquids are generated from the breakdown of water molecules at the electrodes. These areavailable to attack the contaminates in the water flow as they are created and swept away from the electrodes. The result is a reduction in COD and BOD values in the treated effluent.
Lastly, the flow of electrons through the contaminated water kills organisms. Bacteria, protista, fungi, spores and parasites are destroyed due to the alteration of the cell membrane function by the presence of an abundance of negative charges. Unstabilized membrane potentials allow the cells to rupture or to desiccate due to osmotic imbalances. The data to date indicates that disinfection has been demonstrated.
The material of construction of the electrodes 24 and 26 is constant in each cell but may vary between cells and from application to application. Electrodes are commonly made from cast iron, mild steel, carbon steel, or hardened aluminum. 401aluminum alloy has been successful. Less typically but for specific treatment purposes, electrodes may be lead, titanium, platinum, graphite, copper, etc. Electrode pairs which have been used successfully include iron and aluminum, lead and aluminum,and titanium and aluminum. Graphite bonded with epoxy may also be used. Electrode materials should be selected depending on the characteristics of a particular waste system.
Additional energy may be introduced to the treatment portion of the cell in the form of ultrasonic oscillations within the medium to be treated. Ultrasound is applied along with the electric current to further degrade atomic and inter-molecularbonds, to increase the efficiency of oxidation resulting from hydrolysis, to keep materials in suspension, to keep cells clean, and to aid in preventing degradation of the electrodes. The power generator may be external to the system but the preferredmethod is to attach a unit to each cell.
FIGS. 7-9 show the system of the present invention in which each of the treatment chambers can be arranged in combination so as to effect the systematic treatment of a large volume of the effluent. System 60 is shown in FIG. 7. System 60includes treatment chamber 62 and treatment chamber 64 supported on a manifold 66. As can be seen, the inlet 68 serves to deliver the untreated effluent into the manifold 66. Feet 70 and 72 extend transversely outwardly from the manifold 66 so as tosupport the system 60 on a floor. The treatment chamber 62 extends vertically upwardly from the manifold 66. A bracket 74 affixes the treatment chamber 62 to an outlet manifold 76. Similarly, a bracket 78 is used so as to support the treatment chamber64 to manifold 76. Outlet pipe 80 serves to pass the treated effluent outwardly of the system 60 to a coalescence tank. It can be seen that the treatment chamber 62 has a blending and equalization chamber 82 positioned thereabove. Similarly, thetreatment chamber 64 has a blending and equalization chamber 84 affixed thereabove. Each of these chambers 82 and 84 will have suitable gas release means formed thereon. Power supply 86 is connected by bracket 88 to the manifold 76. The power supply86 provides the necessary electrical energy to the respective plate-type electrodes within the treatment chambers 62 and 64.
FIG. 8 is a plan view of the system 60 of FIG. 7. As can be seen, the outlet manifold 76 extends centrally between the treatment chamber 62 and an adjacent treatment chamber 88. The chambers 62 and 88 are held by bracket 74 and 90,respectively, to the manifold 76. It can be seen that feet 72 extend outwardly at the base of the system 60. The power supply 86 is connected to the outlet manifold 76 so as to deliver suitable electrical energy.
In FIG. 8, it can also be seen that another pair of treatment chambers 64 and 92 are affixed to the outlet manifold 76 at a location laterally displaced from the treatment chambers 62 and 88. It can be seen that the feet 70 extend outwardly soas to support the chambers 64 and 92 on the ground. The outlet pipe 80 extends from the outlet manifold 76 so as to deliver the treated effluent to the coalescence tank.
FIG. 9 shows an end view of the system 60. In particular, it can be seen that feet 70 serve to support the inlet manifold 66 above the ground. The chambers 64 and 92 are fluidically connected to the inlet manifold 66. A suitable support 94 isused so as to properly position the chambers 64 and 92 in their respective locations relative to the manifold 66 and 76. The power supply 86 is shown as extending rearwardly of the chambers 64 and 92.
In FIG. 9, it can be seen that the bracket 94 serves to secure the treatment chamber 64 to the outlet manifold 76. Similarly, bracket 96 is used to secure the treatment chamber 92 to the outlet manifold 76. Bracket 88 secures the power supply86 to the treatment units.
With reference to FIG. 10, a process for treating contaminated effluent 100 from an industrial plant is illustrated. Effluent 100 passes through valve 102 to a positive displacement air operated pump 104 and into the inlets of two tanks 106 and108 where the effluent 100 is allowed to separate and form a sludge at the bottom of the tanks 106 and 108. Sludge 110 passes from the tanks 106 and 108 to a pump 112 and then is pumped to sludge outlet 114 for appropriate disposal. Contaminated water116 exits the top of the two tanks 106 and 108 and proceeds to positive displacement pump 118 where it is pumped into the appropriate number of electrocoagulation units 120 for treatment. Electrocoagulation units 120 are controlled by theelectrocoagulation unit panel 122 which is further controlled by the electrocoagulation box 124. The electrocoagulation units 120 are illustrated in series, but the units may be used in parallel or in a combination of series and parallel to achieve thedesired results.
Treated water 126 then passes to a holding tank 128 for coalescence and separation after treatment by the electrocoagulation units 120. Sludge 110 from the bottom of tank 128 is directed to positive displacement pump 112 for disposal throughdischarge 114.
Treated water is taken from the holding tank 128 through a suitable filter 130 and then through a positive displacement pump 132 where it is pumped to a discharge 134.
The four positive displacement pumps 104, 112, 118 and 132 are controlled by an air supply 136. The pumps are controlled to provide a continuous process and to balance the system while regulating flow through the electrocoagulation units. Theunits are controlled to balance the input to the electrocoagulation units with the liquid output from the holding tank. The contaminated effluent 100 is matched with the sludge discharge and the treated effluent 134 to provide a continuous balancedsystem. The system could be balanced in other ways but a combination of positive displacement pumps is durable and inexpensive. Filter 130 can be a filter bag canister or other suitable filter such as a belt filter. A plurality of filters may also beemployed to allow for cleaning and removal of filter cake without closing the continuous process. Preferably, the filters should be capable of removing solids 150 microns in size to about 0.01 microns for particular requirements.
FIG. 11 shows an alternative embodiment of the system 200 for the treatment of effluent water. System 200 includes a treatment chamber 210 of a generally cylindrical configuration which extends vertically. A plurality of plate-type electrodes211 are installed on the interior of treatment chamber 210 in the arrangement described herein previously. Inlet chamber 216 is shown as having a tapered section 216 extending downwardly to solids removal opening 218. The solids removal opening 218allows for the removal of solids and sludges from the interior of the treatment chamber 200. In the embodiment shown in FIG. 11, since the chamber 214 and the chamber 210 are of generally cylindrical configuration, a collar 217 is used to secure thetreatment chamber 210 to the entry chamber 216. A neck 219 extends downwardly into collar 217 so that a solid fit can occur therebetween. Inlet opening 212 is formed so as to allow for the introduction of effluent water into the interior of thetreatment chamber 210. The blending and equalization chamber 238 is affixed to the top of the treatment chamber 210. This chamber 238 is secured through the use of peripheral flange 241 which is secured to the flange 243 through the use of bolts 245. A gas vent 250 extends upwardly from the chamber 238. A pipe 252 allows for the passage of treated effluent into the chamber 238.
FIG. 12 shows a detailed view of the entry chamber 214. It can be seen that the tapered section 216 extends downwardly to the solids removal outlet 218. Collar 217 secures the entry chamber 214 to the bottom of the treatment chamber 210. Inparticular, neck 219 extends downwardly into collar 217 so as to assure the proper connection between the entry chamber 214 and the treatment chamber 210.
In FIG. 12, it can be seen that the inlet 212 is connected to a conduit 260 through an elbow 262. Similarly, an internal elbow 264 serves to deliver the effluent water toward the bottom of the entry chamber 214. Since the effluent water isdelivered directly downward into the entry chamber 214, the solids and sludges will have an opportunity to settle within the tapered section 216.
FIG. 13 shows the arrangement of the plate-type electrodes 224 and 226 within the interior of the treatment chamber 210. The treatment chamber includes grooves 222 that are formed into the wall of the cylindrical treatment chamber 210. Each ofthese grooves 222 forms a slot for the removable receipt of the respective plate-type electrodes 224 and 226. Each of the electrodes 224 and 226 extends, in generally parallel relationship, across the interior of the treatment chamber 210. Each of theelectrodes 224 has a projection 228 which extends upwardly therefrom. Each of the electrodes 226 has a projection 230 which extends upwardly therefrom. Each of the projections 228 is connected to a strap 227. Similarly, each of the projections 230 isconnected to a strap 231. Straps 227 and 231 are individually connected to positive and negative leads from the power supply.
FIG. 14 shows a detailed view in the manner in which flange 240 serves to connect the blending and equalization chamber 238 to the treatment chamber 210. As can be seen, projections 230 are in a proper position for connection to the respectivestrap. The respective electrodes 226 and 224 extend in generally parallel relation to each other within the interior of the treatment chamber 210. Bolt 245 extends into flange 240 so as to appropriately secure the flange to the connecting flange 243. A pipe 252 extends upwardly through flange 240 so as to allow for the passage of treated effluent from the interior of the treatment chamber 210.
The apparatus and process of the present invention has made application in a number of different fields. For example, and without limitation, the present invention can be applied to various waste streams including primary pigment waste streams,trona mining waste streams, biological waste sludge streams, milk, ice cream and dairy product waste streams, vegetable and fruit industry waste streams, oxidation of water waste streams, refinery, petrochemical, and rubber waste streams, transport tankwash waste streams, metal plating waste streams and metal recovery processing, meat industry waste streams, cooling tower water treatment, and disinfection of water and waste streams.
The present invention is useful for the treatment, stabilization and reduction of contamination of waste streams resulting from processing primary pigments. The primary pigment waste streams include an abundance of metals that produce brightcolors normally associated with their use (for example titanium in the production of white paints or chrome for yellow). Most of the resultant sludges are equivalent to enriched metal ores having commercial value which may be used or sold as their ownsource material. When treating such primary pigment waste streams, the inlet waste water stream is pH adjusted with alkali to optimize treatment (generally between 7 & 9). The waste water is next held in a primary separation vessel to settle out andremove any precipitation which may occur. The waste water is then passed through the treatment cell of iron construction. Electrolysis within the cell produces hydrogen and oxygen radicals. The hydrogen acts as a protonic acid so as to reduce thevalance states of the contaminates within the solution, complexing the metal to be removed. The oxygen combines with the dissociated complexes so as to stabilize them. The treatment is instantaneous. The waste water is immediately transferred into thenext cell to complete treatment. This cell, of aluminum construction, treats the water in the next phase of treatment to assimilate, precipitate, and remove any remaining compounds within the water stream. Water is held in a separation vessel for 30 to60 minutes to allow floc formation and facilitate separation and collecting of the sludge by-product from the clean water. The clean water can either be final filtered for reuse or discharged. The collected sludge from the process can be captured anddewatered using a conventional filter mechanism, stabilized, or used as a source material for further recycling.
The process and apparatus of the present invention can be used for the treatment stabilization and reduction of contamination of waste streams resulting from mining of trona. Trona which is the silica used in the manufacture of glass. The inletwaste water stream is pH adjusted with acid to optimize treatment (generally between 7 & 10). The waste water is then passed through the treatment cell using iron. Electrolysis within the cell produces hydrogen (H+) and oxygen (O.sub.2). The hydrogenion acts as an acid dissociating compound and affects the valance states of the sulfur and minerals within the solution, dissolving the carbonates and bicarbonates. The oxygen combines with the dissociated carbon forming carbon dioxide (CO.sub.2). Theiron ion, which is introduced into the stream, combines with sulphur to form ferric sulfide (FeS.sub.2). The treatment is instantaneous. The waste water is immediately transferred into the next cell to complete treatment. A cell, of aluminumconstruction, treats the water in the next phase of treatment to assimilate, precipitate, and remove any remaining compounds within the water stream. The aluminum ion combines with the silicon, and oxygen to form aluminum silicate (Al(SiO.sub.3).sup.3). Water is held in a separation vessel for 30 to 60 minutes to allow floc formation and facilitate separation and collecting of the sludge by-product from the clean water. The clean water can either be final filtered for reuse or discharged. Thecollected sludge from the process can be captured and dewatered using a conventional filter mechanism, stabilized and used as a source material for further recycling.
The apparatus and method of the present invention can be used for enhanced dewatering and stabilization of waste sludge streams from activated sludge wastewater treatment plants without the use of polymers while substantially reducing oreliminating harmful coliforms and pathogens. Typical applications include but are not limited to municipal sewer plant waste sludges, septage and its associated sludges, paper and pulp mill waste streams, and landfill leachates. The waste sludge ispassed through the treatment cell. As the waste sludge stream enters the energy field within the cell, four separate processes act upon the waste sludge. First, the current being passed through the sludge overcomes the Stern's forces within the organicmolecules, disrupting the P-orbits. This process shears the long molecules apart, making them very unstable. Second, electrolysis takes place in the cell, liberating free oxygen and hydrogen within unstable medium. The hydrogen forms a positivelycharged, nucleophillic radical, which acts like an acid to further break down complex hydrocarbons while the oxygen serves to oxidize the remaining volatile compounds in the sludge. Third, the electrons flowing through the stream catalyze thecoagulation or cross-linking of the proteins. Fourth, the cell anodes introduce a charged ion (either cationic or anionic) into the waste stream, both attracting and assimilating the newly formed compounds into a large, stable floc. This combination ofprocesses cause any remaining cellular function within the sludge to cease and desist.
The apparatus and process of the present invention substantially stabilizes and reduces contamination (Primarily BOD.sub.5, TSS, COD, and disinfection) of waste streams resulting from the processing of milk, ice cream, and processing of dairyproducts such as cheese, and their by-products. Because no chemicals are added in the treatment processes, most resultant sludges have commercial value and can be used or sold as its own source material. Typical applications include but are not limitedto: milk processing plants, ice cream plants, cheese processing plants, yogurt processing plants. The waste water is passed through the first treatment cell using either iron or titanium as the cell construction to oxidize the volatile organiccontaminant while dissociating the emulsion holding the fats, oils, and grease (known as FOG) in solution. A cell with aluminum plates treats the water in the next phase of treatment. The water is held in a three phase separation vessel for 15 to 30minutes to facilitate separation and collection of the FOG and sludge by-product from the clean water. The clean water can either be final filtered for reuse or discharged. The collected sludge from the separation devices can be captured and dewateredusing a conventional filter mechanism. This by-product is available for use as a source material for other food products.
The apparatus and process of the present invention can be used for substantial stabilization and reduction of contamination (primarily BOD.sub.5, TSS, COD, and disinfection) and of waste streams resulting from the processing of vegetables,fruits, and their by-products. Because no chemicals are added in the treatment processes, most resultant sludges have commercial value and can be used or sold as their own source material. Typical applications include but are not limited to fruitprocessing, vegetable processing, juice processing, sugar cane processing; brewery waste processing. The waste water is first treated using a fine screen to remove large solids such as pulp, beggas, and other fibrous materials. Any alcohol, starches,or other hydrophillic compounds within the waste water are then treated one of two ways. They are either detained within an activated sludge treatment tank (either aerobic or anaerobic) to metabolize the simple sugars into more complex, hydrophobiccompounds or treated with sodium metabisulfide in a mixing tank for 15 minutes to polymerize the simple proteins into complex hydrophobic compounds. The water is then passed through the treatment cell using either iron or titanium as the cell materialto oxidize the volatile organics while dissociating the complex compounds into simple hydrocarbons which are easily treated. A cell with aluminum plates treats the water in the next phase to assimilate, remove, and stabilize the remaining pollutingconstituents within the water streams. Water enters a vessel to facilitate separation and collecting of the sludge by-product from the clean water. The clean water can either be final filtered for reuse or discharged. The collected sludge from theprocess can be captured and dewatered using a conventional filter mechanism and used as a source material for further food products.
The process and apparatus of the present invention can be used for the complete and universal oxidation, treatment and disinfection of water and wastewater streams in a single step without the use of chemicals or biological processes. Typicalapplications include but are not limited to municipal waste water plants, drinking water plants, industrial and chemical waste water plants, food and food processing waste water plants. The water which contains the contaminating material is passedthrough the treatment cell of titanium construction. Within the treatment cell, a sonic transducer device induces ultrasonic acoustical sound at resonant frequency to induce cavitation in the stream. The cavitation destabilizes the molecular structureof the water (into hydrogen and the hydroxyl radicals). In addition, particulants and surface tension are broken down and greatly reduced. These radicals, along with the hydrogen (which acts as a reducing acid dissociating compound) and oxygenliberated by the electrolysis which occurs, serve to combine with the titanium dioxide (formed from the free oxygen and the titanium ion in the stream) to form titanium dioxide, a powerful catalyst for oxidation. This catalyst assists in reactions withthe volatile compounds to completely oxidize them. In addition, surface membranes of the organisms, which are semipermeable membranes that regulate water intake using osmotic forces, are broken apart by the acoustical cavitation and easily oxidized bythe oxygen and hydroxyl present. The intense ion exchange from the high amperage catalyzes the coagulation, or cross-linking, of the volatile compounds allowing large scale floc to form. Because the floc Is completely oxidized, it is extremely stable.
The apparatus and method of the present invention provides substantial stabilization and reduction of contamination of waste streams (primarily metals and sulfur) resulting from refining, rubber, chemical and plastic manufacturing. Typicalapplications include but are not limited to refinery processing, plastic and petrochemical processing, rubber processing and rubber product manufacturing.
The waste water is pH adjusted to optimize removal of the target metals (vanadium requires a pH of 9, while nickel requires a pH of 6) but, generally the resultant pH is between 4 and 10. The waste water is then passed through the treatment cellusing either iron or titanium, reducing the valance states of the metals within the solution, allowing the metals to complex, forming new compounds and oxidizing the volatile complex hydrocarbon compounds while dissociating the emulsion holding theresidual oils and grease (known as TPH) in solution. The water is held in a separation vessel for 15 to 30 minutes to allow the hydrocarbons to separate from the water and be collected and removed. The metal treatment is instantaneous while thecollection of the oils and grease is not. The waste water is therefore transferred into an intermediate separation tank for 30 minutes to allow for the collection and removal of the oils and grease. A cell, of aluminum construction, treats the water inthe next phase of treatment to assimilate, precipitate, and remove the new metal compounds within the water streams. Water is held for 15 to 30 minutes in a separation vessel to allow floc formation and facilitate collecting of the sludge by-productfrom the clean water. The clean water can either be final filtered for reuse or discharged. The collected sludge from the process can be captured and dewatered using a conventional filter mechanism and used as a source material for further metalextraction and recycling or prepared for disposal.
The process and apparatus of the present invention provides substantial treatment, stabilization and reduction of contamination of waste streams resulting from container wash out, primarily in the transport industry. Wash out waste water can beanything which is transported in a container or tank. The ability of the electrocoagulation process to effect universal treatment for the wide variety of contaminants found in this application is unique. The typical applications include but are notlimited to trucks, rail cars, barges, tanker ships, storage tanks. Wash out waste water is not contaminant specific. The inlet waste water is passed through a screening mechanism to remove large particulate matter. The waste water is then pH adjusted(generally between 4 and 9) to optimize treatment. The waste water is then passed through the treatment cell using either lead, iron, or titanium, reducing the valance states of the metals within the solution, allowing the metals to complex, forming newcompounds and oxidizing the volatile complex hydrocarbon compounds while dissociating the emulsion holding the residual fats, oils and greases (known as FOG) in solution. Biological, organic, or food residuals are treated by destabilizing the Stern'sforces affecting the P-orbits while creating an osmotic imbalance, destroying existing micro- organisms. The water is held in a separation vessel for 15 to 30 minutes to allow the FOG to separate from the water and be collected and removed. The metaltreatment is instantaneous while the collection of the oils and grease is not. The waste water is therefore transferred Into an intermediate separation tank for 30 minutes to allow for the collection and removal of the oils and grease. Solvents mayexhibit some destruction and stripping of chlorine, sulfur, or phosphorous. Often solvents are driven off as vapors and may be collected for further processing or disposal. A cell, of aluminum construction, treats the water in the next phase oftreatment to assimilate, precipitate, and remove any remaining compounds within the water stream. Water is held in a separation for 30 to 60 minutes vessel to allow floc formation and facilitate separation and collecting of the sludge by-product fromthe clean water. The clean water can either be final filtered for reuse or discharged. The collected sludge from the process can be captured and dewatered using a conventional filter mechanism and used as a source material for further recycling orprepared for disposal.
The apparatus and method of the present invention provides substantial stabilization and reduction of metal contamination of waste streams resulting from the metal plating, galvanizing, and etching of circuit boards and manufacture of theirassociated electronic components. Most resultant sludges are equivalent to enriched metal ores having commercial value which can be used or sold as their own source material. Typical applications include but are not limited to metal plating, photoprocessing laboratories, metal finishing and processing, galvanizers, and electronics manufacturing. The waste water is pH adjusted to optimize removal of the target metals (chrome requires a pH of 9, while arsenic requires a pH of 4) but, generally theresultant pH is between 4 and 10. The waste water is then passed through the treatment call using either iron or titanium, reducing the valance states of the metals within the solution, allowing the metals to complex, forming new compounds. Thetreatment is instantaneous and the waste water is transferred immediately into the next cell. A cell, of aluminum construction, treats the water in the next phase of treatment to assimilate, precipitate and remove the new metal compounds within thewater stream. Water is held 15 to 30 minutes in a separation vessel to allow floc formation and facilitate separation and collecting of the sludge by-product from the clean water. The clean water can either be final filtered for reuse or discharged. The collected sludge from the process can be captured and dewatered using a conventional filter mechanism and used as a source material for further metal extraction and recycling or treated for disposal. Often the sludge produced by theelectrocoagulation process is so stable that the material will pass the TCLP test without further treatment.
The method and apparatus of the present invention provides substantial stabilization and reduction of contamination (primarily BOD.sub.5, TSS, COD, and disinfection) of waste streams resulting from the slaughter and processing of meats and theirby-products. Because no chemicals are added in the treatment processes, most resultant sludges have commercial value and can be used or sold as their own source material. Typical applications include but are not limited to beef slaughter andprocessing, pork slaughter and processing, poultry slaughter and processing, fish processing, tannery processing. The waste water is fine treated using a fine screen to remove large solids such as paunch manure, blood clots, hair and feathers. Thewaste water is then passed through the treatment call using either iron or titanium as the cell material to oxidize the volatile organics while dissociating the emulsion holding the fats, oils, and grease (known as FOG) in solution. The water is held ina separation vessel for 15 to 30 minutes to allow the FOG to separate from the water and be collected and removed. A cell with aluminum plates treats the water in the next phase of treatment to assimilate, remove, and stabilize the remaining pollutingconstituents within the water stream. Water enters a second vessel to facilitate separation and collecting of the sludge by-product from the clean water. The clean water can either be final filtered for reuse or discharged. Except for the tannerywaste, where chrome is present in the water, the collected sludge from the process can be captured and dewatered using a conventional filter mechanism and used as a source material for further food products.
The process and apparatus of the present invention provides conditioning of recirculating water used within cooling towers to eliminate scale and algae buildup without the use of harmful chemicals, such as chlorine, for elimination of algae orpolymers and water treatment chemicals for elimination of scale (carbonate buildup), substantially reducing or eliminating periodic water blow down or discharge. Typical applications include but are not limited to big cooling towers and little coolingtowers. The cooling water is passed through the treatment cell. The preferred material of construction is copper. As the water stream enters the energy field within the cell, the carbonates and minerals within the water stream are systematicallybroken down into their elemental components by the liberated hydrogen, a proton which forms a nucleophililc radical and acts as an acid. The resultant elements then reform with the liberated oxygen to form carbon dioxide. The copper ion introduced intothe waste stream is particularly toxic to Invertebrate life forms offering a residual in the waste stream to eliminate future growth in the cooling tower system. The remaining elements within the water stream coalesce around the charged ions (from thecopper metallurgy used) being introduced via the flux field generated by the high current flow which both attracts and complexes the newly formed compounds into a matrix of a large stable floc. This floc can be captured using a conventional filtermechanism. Any algae, molds, or bacteria are simultaneously destroyed as previously described.
The present invention provides the elimination of unwanted biological organisms in water and wastewater streams without the use of hazardous chemicals. Typical applications include but are not limited to sewer plant discharges, drinking waterdisinfection, control of snail populations in various treatment processes, control of zebra mussels in water intakes for power plants, boilers and other raw water intakes, hospital and laboratory waste water and swimming pools. The water which containsthe infectious or pathogenic organisms is passed through the treatment cell. The surface membranes of the organisms are semi-permeable membranes which regulate water intake using osmotic forces. The control of this osmotic cellular water balance iswithin the electrical charge of the fats and proteins in the organism surface membrane. The intense ion exchange and high amperage occurring within the treatment cell drives these surface membranes to an imbalanced state by overwhelming the organismselectrical field and charge; depending upon the surface membrane polarization (+or -), the organism is either excessively hydrated (and blows up like a balloon) or, is dehydrated (and shrivels up like a prune). Alternatively, the electron catalyzes thecoagulation, or cross-linking of the proteins causing the cellular function to cease and desist. Different materials of cell construction (such as copper or carbon) can be used to increase or limit residual disinfection properties after the water streamexits the treatment process to achieve the desired results.
Persons in the art will understand that while certain forms of the present invention have been described and illustrated, the invention should not be limited to the specific forms or arrangement of parts described and shown. Numerous aspects ofthe treatment cell and process which have been described and illustrated are intended to be exemplary and the exemplary particulars are not intended to limit the range of design and use.
* * * * *
I thought we would know by last Friday,
know if this company is "the real deal" or just another Pinksheet scam. Now they have done something dramatic and let the "cat out of the bag" to boot. They really should have put the truth on the table last week to make this new authorized share number more palatable. This is horrible news without an explanation of how it relates to something stockholder friendly. Merger? Buy-out? Hell, Microsoft only has 9.1 billion shares outstanding. HOW MANY SHARES DOES LITTLE ECCI HAVE OUTSTANDING?
Royce Ward (his real name) has closed the sale of his "Regency Energy" company to CTI, and he has millions in hand to make ECCI a real player if it has a real viable technology. He does not personally need to dilute this stock. EC-Water Pure units need to work on Chloride removal. ECCI needs to demonstrate to current and future stockholders that it is excellent at chloride removal from frac water. Otherwise, all is lost!
I want to see an honest and very significant press release in the next two days, preferably tomorrow. I want to know how the 500% authorized share increase is going to be contained and used for stockholder value- not share value destruction. PLEASE SHOW YOUR HAND ECOLOCLEAN INDUSTRIES! IT IS MAKE OR BREAK TIME.
Pure Biofuels is due for news,
Lima plant for real? Show time.
NanoViricides, Inc. Signs Rabies Agreement with CDC for Expanded Research
Monday August 4, 7:00 am ET
Study to Evaluate Usage Strategy for further Development towards Drug Approval
WEST HAVEN, Conn.--(BUSINESS WIRE)--NanoViricides, Inc. (OTC BB: NNVC.OB), (the “Company”) said that it has signed a Materials Cooperative Research and Development Agreement (MCRADA) with the United States Centers for Disease Control and Prevention (CDC) in Atlanta, Georgia for rabies treatment study. The study, to be performed in collaboration with the CDC Rabies Program, is scheduled to begin soon.
“This study will expand on two successful animal studies of RabiCide™-I performed previously by the government of Vietnam,” said Eugene Seymour, MD, MPH, CEO of the Company, adding that “In those prior studies we achieved a 25% to 30% survival rate in animals that had already developed rabies. We believe this strong survival rate is a historical first achievement for any post-infection rabies treatment.”
“Collaborating with CDC in designing and conducting these studies is an important step forward,” said Anil R. Diwan, PhD, President of the Company, adding, “If the current studies are successful, we anticipate that this will be instrumental in helping our anti-rabies nanoviricide towards drug approval and widespread use across the world.”
The Company has previously reported that Yale Research Professor Thomas Lentz, a leading expert in antiviral therapeutics based on virus-cell binding, has joined the Scientific Advisory Board. Prof. Lentz studied the binding of rabies virus to various cell receptors and has performed pioneering research in this field. The Company believes that it has put together a strong team to tackle rabies.
Up 57.14% on the open this morning,
quick, print your portfolio balance to look at over the weekend.
(Things change fast around here. Uoops, now it is down 14%. Can you imagine what will happen when we get some REAL news?)
Tomorrow some positive news?
That Barnett Shale pilot project should be in place by now. 90 days and counting?
Cugar32- the chart is mildly interesting:
only in that volume has risen substantially in the recent month:
http://bigcharts.marketwatch.com/advchart/frames/frames.asp?symb=nubv&time=8&freq=1
Substantial volume increases without price increase can be a sign of accumulation- the move before the move.
What is the share structure? This sounds BAD:
http://investorshub.advfn.com/boards/read_msg.aspx?message_id=31119908
Ben- I have not spent more than 2 minutes
researching it and own no shares- short or long.
tmcc- agreed.
I'm holding for the long run under present circumstances. The future looks good and the company will not respond to my feeble prodding. So sitting on my hands and waiting for the first 10 bagger is the only recourse. Over 20 million long and strong.
If CEO Santini owns 1.5 billion shares,
how many FFGO outstanding shares are there? "Buy low, sell lower" is not my idea of a winning hand.
FFGO down 33.3% too.../eom
No news, no volume
time is running out....
July 15, 2008 TRRC granted DEVON authorization for another pilot project to treat and re-use fracture flow-back fluids and produced water from Barnett Shale. See next to last paragraph below for verification. I wonder who all will be working that new pilot project?
WATER USE IN THE BARNETT SHALE
Updated - 7/30/08
Hydraulic Fracturing
The Newark East, Barnett Shale, Field is one of the most active drilling targets in the past decade. The initial development of the field was centered in southeast Wise County. Activity has expanded to the north in Montague County, to the east in Denton County and to the south in Tarrant County and now is present in 16 counties in North Texas.
The success of the Barnett Shale is in large part a result of the use of stimulation technology. While the volume of gas–in-place is large in the Barnett Shale (estimated to be over 27 trillion cubic feet), recovery of the gas is difficult because of the low permeability of the shale. The Barnett Shale must be stimulated – treated to increase permeability – in order for the field to be economic.
In order to be able to produce gas at volumes that are economical, reservoirs with low permeability must be treated. One method of treatment to increase permeability is fracture treatment or “fracing,” which increases the available surface area by creating fractures that are “propped up” or held open by the propping agents in the frac fluid.
Hydraulic fracturing is used in the Barnett Shale. Hydraulic fracturing consists of pumping into the formation very large volumes of fresh water that generally has been treated with a friction reducer, biocides, scale inhibitor, and surfactants, and contains sand as the propping agent. The water treating fluid maximizes the horizontal length of the fracture while minimizing the vertical fracture height. The fractures, which are held open by the sand, result in increased surface area, which further results in increases in the desorption of the gas from the shale and increases in the mobility of the gas. The result is more efficient recovery of a larger volume of the gas-in-place.
In 1997, the first slick water frac (or light sand frac) was performed and found to be very successful in stimulating the Barnett Shale. Slick water fracing of a vertical well completion can use over 1.2 million gallons (28,000 barrels) of water, while the fracturing of a horizontal well completion can use over 3.5 million gallons (over 83,000 barrels) of water. In addition, the wells may be re-fractured multiple times after producing for several years.
Water Use Estimates
Increasing water use due to growing population, drought, and Barnett Shale development has heightened concerns about water availability in North-Central Texas. In January of 2007, the Texas Water Development Board (TWDB) published a study of a 19-county area in North Texas that includes the Barnett Shale development area. This report, “Northern Trinity/Woodbine Aquifer Groundwater Availability Model, Assessment of Groundwater Use in the Northern Trinity Aquifer Due to Urban Growth and Barnett Shale Development,” includes estimates of water used in Barnett Shale development. This report can be found at http://www.twdb.state.tx.us/home/index.asp.
The TWDB report states that approximately 89% of the total water supply for the region for all purposes (municipal, agricultural, electric power generation, industrial, and mining) is provided by surface water sources, while groundwater is used for the remainder of the total demand (about 140,000 acre-feet per year1). The amount of water from all sources that is used for Barnett Shale development has been a relatively small (less than 1 percent), although growing, percentage of the total water use from all sources and for all purposes in the counties with Barnett Shale development.
The TWDB report estimates that, out of the total water used in 2005 for Barnett Shale development, approximately 60 percent was groundwater from the Trinity and Woodbine Aquifers. The report further estimates that groundwater used for Barnett Shale development accounted for approximately 3 percent of all groundwater used in the entire study area in 2005. However, the ratio of groundwater to surface water used in specific areas varies greatly. For example, groundwater provides as much as 85 percent of the total water supply for Cooke County. In general, groundwater provides for a greater percent of total supply in rural counties and a smaller proportion of total use in more urban counties. Therefore, increased groundwater use for any purpose will have a greater impact on rural areas in the study area.
The TWDB report makes predictions of future water needs for all purposes, including Barnett Shale development. The low estimate for Barnett Shale development predicts a decrease of about 2,000 acre-feet by the year 2025 and the high estimate predicts an increase from an estimated 7,200 acre-feet in 2005 to about 10,000 to 25,000 acre-feet per year by 2025, which corresponds to a estimated potential increase in groundwater used from 3% in 2005 to 7 to 13 percent in 2025. As with the development of any estimate of future conditions, the TWDB and its contractors used educated assumptions to develop reasonable low and high estimates in light of the unpredictability of the natural gas market, which would drive future drilling activity in the area.
Recycling
Recognizing the concerns with water use in the area, over the past few years several companies have applied for, and the Commission has approved, pilot projects in the Barnett Shale to reduce the amount of fresh water used in Barnett Shale development activities.
* Fountain Quail Water Management of Jacksboro uses a recycling process that allows reuse of approximately 80% of the returned fracture fluid used in the Barnett Shale play. This recycling process involves on-site distilling units that apply heat to separate brine from water used to fracture gas formations. When water injected to fracture formations returns to the surface, it becomes unusable due to its high salt content. Under this project, instead of hauling unusable return fracture fluid to a disposal well, the fracture flow-back fluid is stored in tanks on location and piped into treatment equipment. Natural gas produced on location is used to fire the distilling units that in turn boil the returned fracture fluid and produce fresh distilled water. The distilled water can then be used to fracture treat another Barnett Shale well. On October 30, 2006, the Commissioners authorized Fountain Quail on a permanent basis to treat fracture flow-back fluid. As of April 26, 2008, Fountain Quail has processed over 5.7 million barrels of returned fracture fluid to recover over 4.5 million barrels of reusable water.
* DTE Gas Resources, Inc. was granted authority on April 18, 2006 to conduct a pilot project. They are authorized to perform a pilot project to store, handle, treat and re‑use frac flow‑back water at two Barnett Shale gas well drill sites in Tarrant and/or Jack Counties. The frac flowback water must be treated with onsite separation and filtration. On November 13, 2007, DTE Gas Resources has reported that they ceased the pilot project to store, handle, treat and re-use flow-back water from Barnett Shale gas wells. DTE reported that the project was found non-viable economically.
* Devon Energy Production Company, LP was granted authorization effective January 15, 2007, to perform a pilot project to store, handle, treat and reuse fracture flow back fluid from five to ten Barnett Shale gas well drill sites. The fracture flow back water must be treated with on site separation and filtration. On October 22, 2007, Devon reported that the EMS Water Treatment System pilot project has ended. Devon has indicated that fracture flow-back fluid was brought into the system for treatment; however, no recycled water was used to frac. On July 15, 2008, Commissioners approved of Devon's request for authorization for another pilot project to treat and re-use fracture flow-back fluids and produced water from Barnett Shale.(Emphasis added)
* Burlington Resources and Stroud Energy were authorized in 2003 and 2005, respectively, that they may reuse flowback water from fracs in the Barnett shale without a permit for use in future fracs or drilling new wells.
http://www.rrc.state.tx.us/divisions/og/wateruse_barnettshale.html
Hey p_ta- you know the cause of volume,
big volume increases. ECCI needs a leak of big news (GOOD OR BAD) or a press release that is not PURE BS.
Your charts are great.
I'm speculating on 7:00 a.m. ET
tomorrow for some over due news about this company's latest accomplishments. Also, it would be only "sporting" of them to publish the current share structure. I estimate the O/S to be approaching 400 million shares. Call it 355 Million outstanding shares, as a guess. Time to stop all the guessing! I WANT THE TRUTH!
ECCI chart from penny_TA:
Looks like there is life after all. Premature? Volume needs to increase to incubate:
http://stockcharts.com/c-sc/sc?s=ECCI&p=D&yr=0&mn=4&dy=0&i=p51332099101&a=146371304&r=9297
Another 7:00 a.m. passes with no news,
ECCI likes 7:00 a.m. press releases. And there has been none for weeks and weeks. I do not need news for news sake. But the long delays undermine the "sense of immediacy" expressly presented in recent press releases about big developments. So not only is the content disappointing, the timing sucks too: 7:00 a.m PR's cause gaps in the price chart- gaps that chartists and experienced traders expect to be filled by retracements in price. Go ahead, prove me wrong. Make my day!
They could use "all that oil" as a personal lubricant.
Another 7:00 a.m. passes with no news,
ECCI likes 7:00 a.m. press releases. And there was none today or yesterday or tomorrow. I do not need news for news sake. But the long delays undermine the "sense of immediacy" expressly presented in past press releases about big developments. So not only is the content disappointing, the timing sucks too: 7:00 a.m PR's cause gaps in the price chart- gaps that chartists and experienced traders expect to be filled by retracements in price. All in all, this is a bush league operation so far. Go ahead, prove me wrong. Make my day!
BK- stockholders RIP
vampires win again. American greed just like sub-prime/bankers greed. And the good guys end up paying the bill again while the irresponsible bloodsuckers walk away with bonus money in their pockets.
http://biz.yahoo.com/e/080729/ncey.ob8-k.html
I respect that position,
but may I ask you this: to you only moderate on I-Hub boards of stocks that you like? ;))
So janice, what stocks do you like,
now that we know that you are an excellent financial critic? I don't mind selling on good advice, but I love to buy stocks on excellent advice. tia
CR
CleanTech Biofuels to Begin Producing Renewable Electricity
Monday July 28, 4:05 pm ET
ST. LOUIS, MO--(MARKET WIRE)--Jul 28, 2008 -- CleanTech Biofuels, Inc. (OTC BB:CLTH.OB - News) intends to use its proprietary technology at a commercial site in Chicago, Illinois to produce cellulosic biomass as solid fuel for the production of electricity. Beginning commercial production of biomass for electricity will allow CleanTech to develop significant revenue more quickly than originally anticipated.
Tests on the feasibility of using the biomass from CleanTech's processes for electricity production indicated that the energy value (or Btu value) is approximately 75 percent that of coal. Testing also indicates that the biomass has substantially less pollutants in emissions from combustion than other refuse derived fuels and coal.
CleanTech believes that this approach will dramatically lower the cost of its first commercial ethanol plant. By using the infrastructure it constructs for electricity production to support cellulosic ethanol production at the same site in the future, CleanTech believes that it will be able to incrementally increase the amount of MSW processed at the site daily to support both operations.
"We look at the application of biomass co-fired with coal as the low hanging fruit that can be done commercially right now," said Ed Hennessey, CleanTech CEO. "Coal prices have increased dramatically in recent years and that has increased the value of the energy content in our biomass." Hennessey further added, "We are looking to develop a plant in Chicago using the biomass as solid fuel to produce electricity with traditional debt and bond financing to fund a significant part of the development costs. When our cellulosic ethanol conversion technology is ready for commercial implementation, we hope to use the infrastructure at the existing plant to add a cellulosic conversion plant to the same site."
It's Time for ECCI Management to Respond:
There have been some valid criticisms lodged against ECCI and its management in the last month. Many folks have seen losses in excess of 85% over the last 18 months. Many are hoping for an "exit plan" on any modest price appreciation of ECCI stock.
What is needed (to stop this bloody bounce along the jagged bottom of share price) is some verifiable transparency of water purification contracts in Texas that will yield "enormous" revenue/profit for ECCI. Then old folks may abandon their "exit plans" and new folks will start thinking about "entry plans" for investments in ECCI stock.
If there are deals on the Barnett Shale, reveal them. If there are test results needed in advance of signing such contracts, reveal the laboratory test results. Indicate how many machines are on the Barnett Shale and how many more are coming. If there are deals in South Texas for the newly announced plant, reveal them. If there are test results needed in advance of signing such contracts, reveal the laboratory test results. Indicate how many machines are in South Texas below Crystal City and how many more are coming.
http://www.rrc.state.tx.us/divisions/og/wateruse_barnettshale.html
And one last thing, reveal the current SHARE STRUCTURE in an SEC filing with EDGAR, so the stock market can evaluate the ECCI business revelations. No one can force management to respond, but management cannot force anyone to buy its stock. It can force folks to sell its stock.
http://www.pinksheets.com/pink/quote/quote.jsp?symbol=ecci#getFilings
Old SEC Filings
Form Type Received Period Ending Size Report
REGDEX Apr 25, 2008 1.5 KB
15-12G May 4, 2007 3.9 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
4 Mar 2, 2007 Feb 26, 2007 5.7 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
8-K Mar 2, 2007 Feb 26, 2007 11.9 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
8-K Mar 2, 2007 Dec 29, 2006 16.5 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
5/A Feb 28, 2007 Dec 31, 2006 5.2 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
5 Feb 14, 2007 Dec 31, 2006 3.8 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
8-K Jan 19, 2007 Jan 16, 2007 6.3 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
NT 10-Q Nov 14, 2006 Sep 30, 2006 6.9 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
10QSB Aug 14, 2006 Jun 30, 2006 65.8 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
CaliFla- you are spot on:
This stock is a con job and ECCI is going nowhere. Jay Ewing is just a fictional character;
http://www.bledsoecapitalgroup.com/sitebuildercontent/sitebuilderfiles/energyarticle.pdf
http://www.barnettshalenews.com/documents/EwingPres.pdf
ROFLMAO
CaliFla: How are your Real Estate investments doing in 2008?
13- let's just call it rank speculation.
By this time next week we will know,
Jay Ewing of DEVON ENERGY knows already.
But he is not telling anyone the ECCI water test results.
Good luck to all ECCI longs- and even ESPH longs!
Never use a market sell order,
use a limit order, no matter how low. Market orders are always filled lower in a panic sell off than most limit orders that you could accept or imagine (i.e. .01).
NCEY: R.I.P.
Those poor folk never knew what hit them. They are still wondering on the NECY board:
http://biz.yahoo.com/e/080724/ncey.ob8-k.html
No news again?
Long week!
Time for ECCI Management to Respond:
There have been some valid criticisms lodged against ECCI and its management in the last month. Many folks have seen losses in excess of 85% over the last 18 months. Many are hoping for an "exit plan" on any modest price appreciation of ECCI stock.
What is needed (to stop this bloody bounce along the jagged bottom of share price) is some verifiable transparency of water purification contracts in Texas that will yield "enormous" revenue/profit for ECCI. Then folks may abandon their "exit plans" and start thinking about "entry plans" for investments in ECCI stock.
If there are deals on the Barnett Shale, reveal them. If there are test results needed in advance of signing such contracts, reveal the laboratory test results. Indicate how many machines are on the Barnett Shale and how many more are coming. If there are deals in South Texas for the newly announced plant, reveal them. If there are test results needed in advance of signing such contracts, reveal the laboratory test results. Indicate how many machines are in South Texas below Crystal City and how many more are coming.
http://www.rrc.state.tx.us/divisions/og/wateruse_barnettshale.html
And one last thing, reveal the current SHARE STRUCTURE in an SEC filing with EDGAR, so the stock market can evaluate the ECCI business revelations. No one can force management to respond, but management cannot force anyone to buy its stock. It can force folks to sell its stock.
http://www.pinksheets.com/pink/quote/quote.jsp?symbol=ecci#getFilings
SEC Filings
Form Type Received Period Ending Size Report
REGDEX Apr 25, 2008 1.5 KB
15-12G May 4, 2007 3.9 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
4 Mar 2, 2007 Feb 26, 2007 5.7 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
8-K Mar 2, 2007 Feb 26, 2007 11.9 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
8-K Mar 2, 2007 Dec 29, 2006 16.5 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
5/A Feb 28, 2007 Dec 31, 2006 5.2 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
5 Feb 14, 2007 Dec 31, 2006 3.8 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
8-K Jan 19, 2007 Jan 16, 2007 6.3 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
NT 10-Q Nov 14, 2006 Sep 30, 2006 6.9 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
10QSB Aug 14, 2006 Jun 30, 2006 65.8 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
Only if Pure Biofuels is under capitalized
would I think it is a scam. I'm looking into that issue. I'm also sending someone to the Lima port. Why would you think it is a scam?
Tomorrow is a good day to clear the air,
a very good day indeed.
Salmon Creek was a little fishy,
ECCI is getting a more sophisticated Public Relations outfit for handling of the BIG developments that are in the wings. Have not all the I-Hub reviews of the ECCI PR contacts been negative posts. Think positive, folks. The glass is "half full" of very clean water.
DEVON ENERGY Slide Show plus other links:
You need PowerPoint software on your computer.
http://www.fwbusinesspress.com/barnettshale/files/feb29th/8.pps
JUST CLICK ON SCREEN TO TURN THE PAGE!
Also: http://www.bledsoecapitalgroup.com/sitebuildercontent/sitebuilderfiles/energyarticle.pdf
Insane in the Membrane = too expensive:
http://www.geopurewt.com/index.htm
Chart of what needs to be removed from Barnett Shale frac water:
http://www.geopurewt.com/barnett_shale.htm
Chart on NNVC:
It is in a bull channel:
http://investorshub.advfn.com/boards/read_msg.aspx?message_id=30832464
Time for ECCI Management to Respond:
There have been some valid criticisms lodged against ECCI and its management in the last month. Many folks have seen losses in excess of 85% over the last 18 months. Many are hoping for an "exit plan" on any modest price appreciation of ECCI stock.
What is needed (to stop this bloody bounce along the jagged bottom of share price) is some verifiable transparency of water purification contracts in Texas that will yield "enormous" revenue/profit for ECCI. Then folks may abandon their "exit plans" and start thinking about "entry plans" for investments in ECCI stock.
If there are deals on the Barnett Shale, reveal them. If there are test results needed in advance of signing such contracts, reveal the laboratory test results. Indicate how many machines are on the Barnett Shale and how many more are coming. If there are deals in South Texas for the newly announced plant, reveal them. If there are test results needed in advance of signing such contracts, reveal the laboratory test results. Indicate how many machines are in South Texas below Crystal City and how many more are coming.
http://www.rrc.state.tx.us/divisions/og/wateruse_barnettshale.html
And one last thing, reveal the current SHARE STRUCTURE in an SEC filing with EDGAR, so the stock market can evaluate the ECCI business revelations. No one can force management to respond, but management cannot force anyone to buy its stock. It can force folks to sell its stock.
http://www.pinksheets.com/pink/quote/quote.jsp?symbol=ecci#getFilings
SEC Filings
Form Type Received Period Ending Size Report
REGDEX Apr 25, 2008 1.5 KB
15-12G May 4, 2007 3.9 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
4 Mar 2, 2007 Feb 26, 2007 5.7 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
8-K Mar 2, 2007 Feb 26, 2007 11.9 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
8-K Mar 2, 2007 Dec 29, 2006 16.5 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
5/A Feb 28, 2007 Dec 31, 2006 5.2 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
5 Feb 14, 2007 Dec 31, 2006 3.8 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
8-K Jan 19, 2007 Jan 16, 2007 6.3 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
NT 10-Q Nov 14, 2006 Sep 30, 2006 6.9 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS
10QSB Aug 14, 2006 Jun 30, 2006 65.8 KB [PDF] PDF [RTF] RTF [HTML] HTML [Excel] XLS