PROCESS AND ASSEMBLY FOR REMOVING A DISSOLVED OR SUSPENDED CONTAMINANT FROM A POLAR LIQUID AS A SOLID SUBSTANCE

Abstract: Solid and/or dissolved contaminants are separated from a polar liquid such as water by providing in the contaminated, acidic liquid medium a galvanically charged particulate dis­ persion of defined size, concentration, density and free sur­ face energy, and then flowing such loaded medium through successive oxidation and treatment zones of an electrically insulated apparatus at a rate defined by dimensionless para­ meters such as Reynolds numbers, etc., so as to prevent phase separation. Gaseous oxygen adheres to particle sur­ faces and oxidation is further promoted by bringing medium to pH 2.0 to 2.5 as with sulfur dioxide gas, plus exposure to action of heavy-metal ions such as ferrous/ferric. After air blowing, medium is neutralized and brought to pH 10-11 with continuous aeration of suspended flocculant, then treated with soda ash and optionally additional particulate (recycled sludge), and the contaminant matter then allowed to precipi­ tate with concurrent galvanic grounding of the medium. The dispersed particulate matter may be inert and deliberately added (e.g., shredded cellulose) or it may be produced in situ by fractionation of component debris as in sewage-refuse; when possible, as in the latter case, the particle itself is subse­ quently oxidized. In either event, dual end products are pot­ able water and sterile sludge. Dissolved salts such as sodium chloride are simultaneously removed from medium as com­ ponent of sludge; applicable to remove toxic components from cooling water systems, recover traces of precious met­ als, etc., from slurry or run-off liquid, brackish water, indus­ trial waste, etc. Suitable treating apparatus is also provided.

Description: GALVANIC FLOW SYSTBT FOP JOINT PARTICULATE RECOVERY AND LIQUID PURIFICATION The demand for water purification does not arise solely from the need for treating sewage or noxious industrial waste, nor is it necessarily directed merely toward obtaining potable water for humans and animals. Recent environment control regulations have restrained the discard of water such as that which through ordinary industrial use has appreciably increased its content of dissolved solids (which are generally inorganic or mineral compounds) as well as inhibiting discard of such liquid which has accumulated or concentrated particular toxic components. For example, the body of water which is circulated as a coolant in many industrial or chemical plants, is then returned to a heat exchanger where part of it is evaporated in order to reduce the temperature of the remainder, which remainder is then recirculated. This evaporation step itself would increase the concentration of contained solids merely bo reducing the volume of liquid. However, in its travel, the liquid picks up deposits or sediment from the plumbing system, and in addition, in order to minimize corrosion, foaming and scale formation (such as resulting from '#ard water"), various inhibitory additives are mixed into the circulating stream. These obviously contribute further to the dissolved solid content and after the latter has built up to the maximum allowable for continued circulation, it becomes necessary to discard part of the fluid mixture and replace it with fresh water (and new additives). However, this heavily loaded discard has now become an illegal pollutant when released into flowing streams or ocean. The problem is to purify it before release; and hopefully if such purification process is sufficiently successful or complete, the water may be reused indefinitely and need not be released at all. A particular contaminant in such cooling water system is chromium which is a component of many anti-corrosive or biocide additives. Thus hexavalant chromium is a toxic substance not releasable to the environment. other toxic components of common cooling water additives are cyanides and phosphates, which must be detoxified before release. Phrification of polluted water for purposes of reuse, whether starting with agriculture/municipal sewage or with industrial waste, has been concerned primarily with recovery of potable water, only after the initial separation and disposal of solid components in an inert state, this being considered a necessary and preliminary step for any subsequent treatment. The solids may have then been utilized to a small extent as plant support base or land fill,but such product is not a primary purpose for effecting the separation and for the most part the undifferentiated sludge is simply separated in bulk and discarded in the manner most convenient. purification of the aqueous phase then takes place (if at all) as a successive, rather than concurrent, procedure. -However, it will be realized that the aqueous run-off from many and probably most watertreating procedures (even if only involving flushing) carries a quantity of solid and potentially-solid ingredients having tangible economic value if such could only be recovered in concentrated form without great expense. Further, treatment of such masses of contaminated water in the past has been primarily on a batch basis, large bodies of water being treated with acid or other reagent in a "settling basin" or even in successive chambers and then allowed to stand for atprolonged period until spot checks show that the supernatent was clarified. In brief, it has not been realized that by careful regulation of the parameters of a flowing stream containing charged particles, separation/purification of an impure aqueous medium could be effected in a fraction of the previous time, and also that the controls could be shifted so as to maximize the withdrawal of specific contaminants which it was desired to concentrate in the solid state. Some substances it may be desired to destroy - - as microorganisms, herbicides, pesticides and inorganic toxins - - or to recover, such as flitrogeneous compounds or precious metals. Accordingly, the control parameters of such flow treatment can now be accommodated to a particular feed stock and with a view as to how it is wished to dispose of specific contaminants. It has long been known to purify waste water by oxidizing it in the joint presence of iron plus sulfur dioxide or an oxidizing acid. The impurity is then removed by flocculating the iron in alkaline media. However, to the extent that this process has been used, bulk solids necessarily were first removed as by filtration, and as to the remaining filtrate, past treatment does not remove dissolved impurities (such as inorganic salts typified by Nail) or substances incapable of oxidation (such as metal particles): each of these classes may include such undesirable toxins as arsenic, mercury, cadmium, lead, selenium or boron. It has now been found that this dual oxidation/precipitation step can be incorporated into a composite treating process whereby essentially any flowable, polar liquid medium containing (finely fractionated) waste/refuse, as well as soluble salts and non-oxidizable impurities, can have all non-gaseous impurities removed as solids, leaving a sterile, pure, oxygen-containing liquid (e.g. potable water, which is also capable of supporting fish and other marine life). The precipated material is also sterile and if desired can be further fractionated to recover substances of economic value, such as precious metals or fertilizer-enriched sludge. In brief, in a primary reaction vessel or multi-unit apparatus, all of which is electrically insulated, there is provided (in the absence of any externally imposed electric current) a self-generated galvanic cell formed by "soluble" or free electrons resulting from acidic oxidation of a contained heavy metal capable of alkaline flocculation, such as iron and/or aluminum, as well as by free electrons produced by disassociation of water (or other polar media) by introduction of sulfur dioxide. A minimum suspension of minute particles (as hereafter defined) is also deliberately provided, either by addition or by fractionation of bulk solids initially present. Such dispersed particles (preferably constituting all of the solid material present except for the electron-produciTt metal) inherently possess random movement in the liquid medium (which movement is the Van der Waals effect resulting from an internally generated spin of an unsymmetrical molecule). In conjunction with the moving electrons, this results in a distribution of charge to other particles and adhesion between charged microparticles and minute gas bubbles, which ultimately results in complete oxidation of all oxidizable material present. This necessary cross-distribution or random mixing of electrons with both charged and uncharged particles in the insulated cell may be accentuated by bubbling gaseous oxygen (air) and/or sulfur dioxide through the liquid, as well as by agitation of the body of liquid as by means of pump or stirrer. Electrical insulation of each reaction vessel is necessary in order to keep such charge (maintained by pH regulation) from grounding through a conductive reaction vessel or flow conduit. Under the step-wise oxidizing conditions and imposed galvanic flow pattern, metallic ions agglutinate with particulate matter and are replaced in the aqueous medium by other cations, i.e. hydrogen ions, at the same time maintaining the selected concentration of acidity. Among oths reactions, part of such hydrogen ions couple with available nitrogen to form NH4 Such ammonium ion then couples with ferrous ion to form (green) ferrous ammonium ion. Successive chemical reaction steps can be effected by batch procedure, as long as sufficient agitation is provided to keep the ingredients from settling out prior to the ultimate and desired flocculation. However, it is usually desirable to effect the process as a continuous flow, particularly when a continuing supply of feed stock is available, as from a municipal sewage collection stream or similar industrial/agriculture waste flow. Accordingly both the liquid medium and an associated gas stream are moved to and through successive treating zones or chambers. The body of reactant gas (which should include oxygen) is channelled to contactingly overlie or flow through the liquid medium as the case may be. Accordingly, by relating the size and shape of the reaction vessels and connecting conduits, a series of dimensionless parameters has been obtained for both the liquid and gas streams, by use of which controlled flow rates the material being treated is moved in a substantially continuous but step-wise pattern of reaction which prevents phase-separation while enabling or promoting electron distribution until complete oxidation is effected. The final chemical-treatment step is then accomplished by alkylation of the medium with avoidance of potential phase-separation during a preliminary digestion period followed by electrical grounding of the medium concurrent with joint precipitation Xlocculation of the metallic ions and the coagulated impurities. In addition, such grounding of the medium, which may be effectuated by grounding the insulated reaction vessel containing it, produces a noticeably more firmly-packed precipitate than would otherwise result. When the composite impurity is composed of both (a) cellulosic material (e.g., food residues, waste paper orcartons, etc.) and (b) suspended minerals or metals and/or soluble salts (e.g. brackish water) the final alkaline flocculation tends to segregate "a" and 'b2' into successive layers with the 'M" material being precipitated first or underneath the "a" material. The procedure can thus be used to concentrate small quantities of precious metals from slurries and the like; in the event that "a" material is not already mixed with it, the minimum charged particulate matter is added as described. Separation of all potentially-solidcomponents from such aSDwiE galvanic cell, by grounding and cessation of movement or agitation, in addition to removing in the flocculate such impurities as might previously be expected from the chemical reaction alone, now also draws soluble salts such as sodium chloride out of solution as well as precipitating suspended non-oxidizable particles. The only requirements for participating substances are that the liquid be a polar liquid, and the solid or potentially-solid substance be capable of the Van der Waals effect. In addition to water, other polar liquids are alcohols, acids, bases and other substances which ionize or conduct an electric current. The dispersed particulate matter should constitute a minimum of about 0.1% w. and have a particle density of about 1.05 to about 2.0 and a size of about 30 to about 225 microns with free surface energy of about 100 2 to about 500 ergs/cm In this connection it will be realized that the smaller the particle size, the greater the relative surface area and the greater the forces of surface attraction (relative to weight), so that the relative influence of gravity on the particle is correspondingly deminished. Thus the specific surface energy of a given solid can multiply more than 8000 times in going from approximately two inch diameter to one micron. Its unit surface energy at the same time increases more than 6oo#. Accordingly, the greater the fractionation (maceration) of the bulk material into small particles the greater effect the increased surface energy will have on reaction and flow properties. This factor is the same of course whether the material constitutes matter which (in addition to its carrier function) is to be oxidized, or whether it is particulate matter added merely for its function of carrying a charge in the flowing galvanic stream. However it will be apparent also that such fractionated particles, possessing Brownian movement and increased unit surface energy, have a strong tendency to coalesce if brought together; that is, they become a non-free-flowing mass rather than acting as independent discrete particles. Such potential coagulation is prevented by (1) pump action,mechanical agitation, and passage of gas currents through the liquid, each applied at a particular critical location, and (2) by moving the galvanic flow stream at a varied and deliberate rate in accordance with Reynolds Numbers and other dimensionless parameters selected to prevent phase separation. Thus when later such suspended particles (galvanically charged) are finally directed to settle out, in cooperation with a flocculating ion, cancellation or grounding of the galvanic charge tremendously reinforces this final (desired) phase separation. Thus one particularly notable and totally unexpected result from this flowing galvanic cell and from the Van der Waals surface effect exhibited by the particulate dispersion, is that by the present process soluble salts (in particular Nacl or other alkali metal halides) present in the liquid, also leave their state of solution and enter into the separating flocculate. Such desalinification may be explained in part by continuation of the suspended flocculate in an oxygen-saturated medium until the reduced flocculating ion (ferrous) is itself completely oxidized (to ferric ion). To restate the present process: flowable contaminants of a liquid may be either or both soluble and solid (the latter being held suspended by a moving stream). They may or may not be in a condition of lower valence or be subject to having toxicity destroyed by oxidation, but in any event the flow is exposed to a strong oxidizing treatmezt(initially in a strongly acidic environment which is then shifted to a highly alkaline environment) in a moving ionic exchange medium which characteristic is furnished by a combination of Van der Waals surface action of particulate matter and by galvanic charge imposed on such particles; one result of this is that gas bubbles (of air and sulfur dioxide) surface-adhere to and react with oxidizable particles and are replenished by inert particles (carriers) transferring similar bubbles to them. The flow is moved through successive treating units at rates of flow determined by dimensionless numbers such as Reynolds, Schmidt Numbers, Peclet Numbers, Lehman Reaction Numbers, Weber Numbers, Stanten Numbers and certain bed contact numbers. After alkaline treatment and continued gaseous oxidation, the nonliquid components are flocculated and separated as a sterile solid sludge. The latter may then be digested and/or fractionated to concentrate and retrieve particular ingredients of value, by use of known methods. Whereas in the past it was only dimly appreciated that the 502 iron oxidative reaction required the presence of free electrons (apparently transferring between ions), it is now realized that it is highly desirable to provide such a "galvanic exchange" condition throughout the whole procedure and particularly in conjunction with (a) turbulence or agitation, and (b) the intimate presence of gaseous oxygen continuing through successive steps until the flocculating ion itself is oxidized. As already noted, the galvanic charge imposed on the particulate matter by the added electrolytes (acid and basic reagents) promotes or accentuates the surface adhesion of gas to particle, and enables the interchange of electrons. Such a reacting state is then maintained, and phase separation prevented, by movement at a tailored flow rate. Typical surface-adsorbent particulate matter may be either oxidizable or non-oxidizable and includes cellulosic or other organic matter as well as inorganic compounds such as metallic oxides (alumina, magnesium oxide or calcium oxide) and especially compounds of atoms which have a Van der Waals packing radii of about 1.9 or less. Additional examples of particulate matter include infursorial earth, diatomaceous earth, bentonite, and siliceous matter such as free-flowing sand and silicones. The invention will be described further, by way of example, with reference to the accompanying drawings, in which : Figures 1, 2, 3 show in semi-schematic representation, a process and apparatus embodying the present invention, with the various flow connections being horizontally alignable when the three sheets are placed side by side in this order. Figure 4 is a horizontal sectional view taken on line 4 - 4 through the soda ash treatment unit of Figure 1. Figure 5 is a vertical sectional view on line 5 - 5 of the homogenizer tank of Figure 2. Figure 6 is an enlarged fragmentary detail of an end outlet segment of an air delivery conduit of tanks 70 and 72. In the illustrated apparatus, a flowable feed stock such as raw sewage is introduced through an inlet conduit 10 into a wet well or fragmentation chamber 12 where a chopper pump 14 reduces the solid matter to the required particle size (30 to 250 microns). Liquid level in this chamber is regulated by an automatic control unit 16 which opens and closes a pinch valve 17 in the line. From the wet well the particulate dispersion is moved to a primary or marshalling tank 18 through a conduit 19 as regulated by a liquid level control 20. In the absence of any or sufficient solid matter in the feedstock, the required particulate matter, which may be any inert material which will hold a galvanic charge (e.g. shredded cellulose) is added to the wet well from a supply hopper 22 by a conduit 23. The comminuted feed stock is ultimately withdrawn from the primary tank 18 through conduit 24 at a rate determined by a suction pump 25 and conveyed to a pulsation damper tank 27. A controlled quantity of exhaust gas is released from the top of the closed tank 18 through a wet charcoal filter unit 26 and vented (odourless) to the atmosphere. Within the primary tank 18 is a submerged transfer pump 28 which is operated to maintain a continuous flow of fluid and suspended particles. Turbulence within tank 18 is contributed in part by the presence of internal baffles 29 and by continuous bubbles of a (recycled) gas mixture from conduit 30 which enter through perforations in the piping adjacent the flooring 31 of the tank. To the extent that the liquid medium is clear enough, it is visually discernible that small gas bubbles here adhere to the surface of the moving solid particles within the liquid, and their gaseous oxygen content (derived initially from air) plus SO pretreats or conditions oxidizable particles for subsequent oxidation. In the case of highly oxidizable matter such as fecal debris, a residence time in the preliminary chamber 18 on the order of about one and a half to about two hours is indicated. From the pulsation dampener tank 27, the flow, at the rate controlled by mass flow meter 21, is moved through conduit 34 to a mixer tank 35 where it is intermingled with a gaseous mixture of sulfur dioxide and air, introduced by drop lines 37 from an overhead gas mixing chamber 36. Recycled gas is introduced to the mixer chamber 36 through the line 38 coming from a compressor 40 which receives exhaust gas through line 42, passing through a silencer unit 43. Both the gas mixer 36 and the flow mixer tank 35 are at times supplied with liquid sulfur dioxide through line 45 from a supply tank 46 (which may be heated), in response to a pH meter 44 which maintains the tank 35 within the pH range of about 2.0 to about 2.5. Alternately or concurrently sulfur dioxide gas is supplied to the gas mixer 36 from supply source 47 through conduit 48, controlled by pH meter 44 and/or the mass flow meter 21. In tank 35, Peclet Numbers will range between 9 and 25. Lehman Reaction Numbers of the blow tubes 37 vary from 3.5 to 8; for eductors 25 to 30. Exhaust gas from the tower39 is continuously introduced into the iron reaction chamber 50 as a stream of bubbles through conduit 49, while at the same time the liquid flow containing a controlled amount of free gas bubbles is passed through an outfall conduit 52 and introduced through line 53 into the reaction chamber 50 below the porous bed. It is very important that gas inlet valve 49 be partially closed and thus used to mix its flow with the fluid flowing through the line 53. The gas mixture which is passed jointly through the scrap iron bed (which furnishes both ferrous and ferric ions to the medium) and through the liquid flow stream, should contain a mixture of both nitrogen and oxygen (i.e. air). Vaporous mixture from the stack 51 of the iron chamber is passed through the conduit 54 which separates the non-gaseous components (i.e. liquid droplets) and returns them to the mixer tank 35 of the main flow by way of conduit 57 or into the discharge from tanks 70 or 72; the gaseous portion is recycled through the compressor 40 by the line 57. Liquid outflow from the reaction tank 50 has a pH of about 3.0 to about 3.5 and is passed through conduit 60 to a blow tank 62 where air from a reservoir 63, by conduit 64 and manifold 65 is passed upward through the liquid so as to separate it and to again provide a fluid system saturated with dissolved oxygen. The flow is generally red from ferrous ions. Gaseous take-off from stack 61 by conduit 66, and gases from tanks 70 and 72 by lines 67, 68 are returned by line 30 to primary tank 18. From the blow tank, liquid outflow is conveyed to the lower level of the neutralizer tank by conduit 69. A conduit 74 connects a mixing throat 75 of the outflow conduit 69 to a caustic supply tank 76, and a conduit 78 connects a lime slurry source 79 and circulating pump 80 to the mixing throat 75, the alkali flow to the neutralizer 70 being controlled by a pH meter 77. Instead of gradually neutralizing the acidic flow and progressively bringing it to the required alkalinity of about pH 11, it has been found advantageous to introduce through the throat 75 at one time, substantially the whole quantity of alkali required to achieve the final p11 for that immediate volume of flow with which it is mixed. The air reservoir 63 initiates a plurality of air delivery lines 83 to the neutralizer tank 70 and a similar series 88 to the homogenizer tank 72, which individual lines are disposed to emit a bubbling shearing air stream from individual sparger or wedge-aperture nozzles at their distal ends, thus agitnting the churning or foaming mass of liquid and charged particles at the same time that they supply oxygen and nitrogen. Consequently, the emerging outflow through conduits 71 and 73 is oxygen-saturated and the adsorbed gas on the particulate surface aitinues to be reactive. The flow of air through the several lines 83, 88 is controlled by individual (manual) valves or orifice plates so that it can be adjusted to the "step by step" progression of the increasingly viscous flow and thus continually prevent agglomeration and sedimentation. A residence time of about 15 to 17 minutes in each tank is typical; total about 30 to 40 minutes at about 60 - 800F. The air reservoir 63 is supplied by conduit 59 from an air compressor 89 connected to a silencer 91. The compressor processes fresh air and in some instances may pass it through an ozonizer 98, such as the non-sparking, low voltage, AC, face-separated insulated-plate type described in U.S. Patent No. 3,948,774. However, the basic procedure is sufficiently effective in most cases without the additional oxidation provided by ozone. As seen particularly in Figure 2, 5 and 6 the several air lines 83, 88, each angularly dispose their terminal segment 100 transversely within the tank 70 or 72. It is formed with a closed end 101 and a blow outlet mouth 102 is cut wedge-shaped into the hemi-cylinder which is oriented downward when disposed in the tank at a transverse angle to the longitudinal vertical plane of the chamber. Such positioning of the outlet minimizes the possibility of liquid backflow and consequent solid deposition or encrustation therein. Successive segments 100 are mounted crisscross or at different angles so that their outlet mouths are angularly staggered relative to the longitudinal axis of the tank. Functionally, the flow-aligned tanks 70, 72 can be considered to provide the same continuing and accelerating reaction process in tandem structural units, that is, supporting completion of the neutralization process while keeping in suspension the forming flocculate in the increasingly viscous flowstream so as to restrain phase separation. When it is desired to maximise removal of hardness components and silica, the outflow conduit 73 from the homogenizer tank 72 receives a soda ash increment from a supply tank 99 through line 84 and then passes through a heating zone or unit 85 where the flow is raised to a temperature of about 900 to about l200F before introduction to the treatment tank 82 where it is agitated by a motor driven agitator or marine type impeller 85. Location of four intermediate-length upstanding baffles 87 in the tank enables or directs the liquid suspension to circulate in closed paths of generally vertical ellipses between adjacent baffles. From the treatment tank 82, a conduit 90 carries the flow to a flocculation chamber 92 which may have inclined walls and/or corrugated floor segments separated by upstanding baffles which form a convoluted pathway for descending sediment and liquid. Individual floor segments are movable by pneumatic actuators 93 driven by air lines 94. Each unit of the apparatus has been electrically insulated from the ground and from successive (adjacent) units, being connected together by plastic conduits, the chambers preferably being formed of non-conductive material (concrete or wood) and in any event lined with corrosionresistant layer such as plastic or glass fibre. The flowstream or liquid medium may now be grounded by closing a switch 95 connected to an electrode 96 which is exposed to (i.e. inserted within) the fluid of the chamber 92. Consequent discharge of the galvanic charge carried by the particulate matter (which should now be oxidized to the extent possible), and cessation of agitation and flow, initiates a relatively rapid precipitation of the potentially solid components from the liquid medium. Residence time in the flocculation chamber is on the order of about 30 to about 90 minutes. Dismally the sludge, dark red-black from ferric ion, falls into a screw conveyor 97 which passes it through a screen classifier (not shown) and returns the liquid component to the system, The liquid of the flocculation chamber 92 passes over an air-locked weir 104 into a decanted water tank 106 where a submerged pump 107 moves it through conduit 108 to woven strainer units 109, 110, which remove collcds, and thence to an upper inlet of a packed tower 112 where it percolates down through raschig-like rings countercurrent to a stream of (possibly ozonized) air and is then introduced through the conduit 115 to a holding tank 116. Air from the top of the tower is conveyed by line 114 to the decanted water tank 106. Liquid outflow from the tower 112 passes through conduit 115 to a holding and aeration tank 116, which latter may be connected by a line 117 to a source of chlorine for optional use in particular circumstances (e.g. when required by local ordinance). A compressor 120 with silencer 121 delivers fresh air through conduit 122 to the aeration tank 116 through lines 123, 124 and to a filtered water tank 125 through lines 126, 127, 128. A gas take-off line 129 connects the filtered water tank 125 with a charcoal-filter exhaust unit 130. The latter is also connected by gas line 131 to the aeration tank 116. The tank 125 has a submerged pump 132 which moves liquid through conduit 133 to an ultimate polishing or holding tank 134. The aeration tank 116 is connected by pump 135 and liquid conduit 136 to dual or alternate activated-charcoal filter tanks 137, 138, having drain lines 139, 140 , which are joined to conduit 144 which terminates in the holding tank 125. A backwash line 142 collects fluid from filter tank 134 and delivers it to the decanted water tank 106. A return line 146 connects the backflush outlets of the two filter tanks 137, 138 to the decanted water tank 106. pump 132 in tank 125 provides product water or water for backwash through line 133 to filters 137, 138 and to product filter tank 134. A backwash line 146 connects the filter tank to the primary tank 18. The solids collected in the bottom of the flocculation tank 92 may contain toxins (which have not-been detoxified by oxidation). Such can be metals such as mercury, arsenic, boron, lead, iron, gold or silver, as well as some biocides. Nonoxidative pyrolysis may be used to remove organic materials such as petro-chemicals. Precipitates such as carbonates and sulfates are decomposed and removed as carbon dioxide and sulfur dioxide. Nitrogen is removed as an inert gas. The metals may be volatised and recondensed or removed in a carbon matrix and then calcined/ roasted in the presence of oxygen to prepare a composite of various metallic oxides. The noble metals are recovered as a combined metal concentrate. The particular procedure for any flowstresm will be adapted of course to the specific components shown by analysis to be present and which it is desired to recover. F1#W PATTERN: Reynolds Number EMI14.1 For example, the iron reaction chamber 50 has the characteristics - Diameter Liquid Liquid masç Air Mass Npe Mass flow feet velocity- flow-lb/ft Air flow-lb/ft2/hr e Ratio ft./sec. liquid/air 1.5 0.0143 1763 210 967 8.395 2.0 0.0121 1984 230 1452 8.626 2.5 0.0124 2540 210 2320 12.095 2.75 0.0116 2600 210 2613 12.381 3.00 0.0118 2645 252 2900 10.496 A critical factor for such sewage or waste water treatment in the presence of particulate matter and sulfite/sulfate ion or hydroxyl ion is defined as Shape Factor EMI14.2 wherein Y = particulate concentration factor. DA = nominal air lift Disengaging Area HFA = waste fluid hydraulic flow area An operative SF range is from about 9.5 to about 11.3; optimum 10+0.5 EXAMPLE: Municipal sewage with the bulk solids reduced in size to the designated particulate diameter was flowed through a processing assembly such as here illustrated, the initial acidity made pH 1.5 to 2.5 by introduction of liquid and/or gaseous sulfur dioxide. The liquid flow was then moved through the serpentine flow pattern of tank 35 (shape factor 9-10) at NRe of about 5000 to about 10,000 when in contact with the gaseous flow and about 7000 to about 18,000 when not in contact with the gaseous flow; the gas mixture of SO and air was moved at about Npe 400 to about 500. After about 7-1/2 - 15 minutes residence in the iron reaction chamber 50, the flow was passed through the airflow tank 62 and thence to the neutralizer tank 70 where the p11 was increased from about 8.5 to about 10.0 during a period of about 15 minutes; it continued through the homogenizing tank 72 for about 15 minutes while the pH increased to a maximum of about 11. When the operation is particularly directed to removal of calcium and magnesium ions ("hardness" components) and also to reduce the concentration of silica, 15- ps of the sludge removed from the screens (subsequent to flocculation) is returned to the homogenizer tank to augment the particulate concentration and increase interfacial surface area, thus - Type In Liquid System Particulate Particle size Density Amount Interfacial Surface Dia.microns mg./cm go nitre area, cm2 nitre Solution born 30-225 192-1500 0.3-0.9 660-13000 Fiocculants 1004350 300-3500 0.04-0.3 25-4500 Precipita#s200-700 250-500 0.07-0.09 14-135 Additives & BR< soda ash 75-250 320-1700 0.10-16 40-4800 Recycle sludge 30-700 192-3500 0.01-4.8 250-3360 Additives of such size include fly ash, carbon black and infusorial earth. The flow is then moved through an agitation and heating zone 82 at NRe of about 30,000 to about 40,000 with addition of soda ash. Alternate to use of mechanical propellors, complete agitation with blown air may be achieved when there is 1.5 - 3.0 CFM/minute/ft2 of cross section area. Finally, the fluid flow is moved at Npe of about 2000 to about 3700 for about 30 to about 90 minutes through the flocculat- ion tank or sedimentation zone 92. In retrospect, the addition of particulate matter by the present process may be distinguished from various incidental additions of particles to liquids in the past in that the latter were (a) for removal of dispersed colloids by adding charged particles in order to agglomerate the two substances, or (b) for removing a solute by addition of a substance which decreases the solubility of one or more of the dissolved components. Neither of these treatments contemplates (or obtains) a continuing reaction (oxidation) between the dispersed particles and a gaseous component adhered to the added particles, and/or the interplay of free electrons in such environment, which electrons take part in the desired continuing reaction. Nor do they contemplate deliberately maintaining such dispersion and preventing agglomeration during a necessary {multi-step) reaction period; nor final precipitation by introduction of a flocculating ion. In brief, the provision and utilization of an insulated flowing body of polar liquid constituting a galvanic or ionic exchange module (cell) the contents of which is continually manipulated both to prevent phase separation (precipitation) and to effect a desired chemical reaction (ultimately resulting in joint liquid purification and separation of solids) seems to have been entirely overlooked or unappreciated. The necessary polar solvent such as water, contrasts with non-polar solvents such as mineral oil, paraffine, kerosene, etc., which are not suitable because of being incapable of transmitting an electric current. It should be appreciated that the intended and necessary result from applying the dimensionless flow parameters related herein, is that (1) sedimentation and agglomeration are prevented, and (2) at their active surface area, the dispersed particles maintain the intermolecular attraction, often referred to as the Van der Waals effect, which attracts to and causes to adhere thereto clusters of moving air molecules (bubbles). The result is not only the progressive oxidation of the flowing particles, but also subsequently the electrical and interatomic field force which is thus continued, appears responsible for "drawing out" of solution the dissolved electrolytes of both positive and negative charge, such as the halide (chlorine) ions and alkali metal (sodium) ions which finally are separated from the medium as one component of the flocculate. In addition to the Reynolds Number which relates the fluid density and velocity with the container configuration, the following parameters should be taken into account - The heat transfer and energy retaining properties of the flowing fluid are defined by the Peclet Number = DV,o Cp/k or EMI16.1 Cp = specific heat; 6 = surface tension k = thermal conductivity. The peclet Number for tanks 70 and 72 is in the range of 12 to 32, and gas escape velocity at the surface is 0.18 to 0.24 ft./sec. The Schmidt Number relates viscosity, density and container diameter (hydraulic diameter in an awkwardly shaped vessel) NSc = A / r DV. The Stanton Number relates the coefficient of heat transfer (h) to the specific heat, velocity and density. NSt = h/C V p p The Stanton Number for the liquid flow gas mixing tank 35 is 35.50 to 36.20; for the neutralizer and homogenizer tanks 70, 72 the Stanton Number is 28.60 to 10,160. The Weber Number relates the shape of the container (length of flow path L), the density, the velocity, and surface tension. N We = L# V76 gc. Contact Number Nc = Uê/#êg) 1/3 (NRe) 1/2(NSc) 1/2 The iron tank 50 has an operable range Schmidt Number 4 x 10 7 to 1.3 x 10-6; the contact number is 228 to 446. Reaction gases (air, sulfur dioxide, nitrogen or ozone) can be introduced into the stream of particulate-laden fluid by eduction, sparge lines, or blow-shear tube. Each of these operates within a precise Lehman Reaction Number and Weber Number range. The dimensionless Lehman Reaction Number relates the System Shape Factor and the mass flows of fluid and gases. System LRN Weber Eductor system 25-30 1.0-1.7 Sparge Lines 3.4-4.4 0.92-1.98 Blow-Shear Tube 6.7-7.7 0.98-1.85 The terminal velocity of spherical and non-spherical droplets of particles settling in the vapour space will vary from 0.4 to 30 ft./sec. Particles up to 85 microns will be entrained and are removed prior to gas flow to the iron tank 50. flow conditions within the heater tank 85 are defined by a Reynolds Number of 30,000 to 40,000 and a Grashof-Prandtl Number product within the range of 25,600 to 230,000 on the waterparticulate matter side. The Grashof Number = (L3 t 2 ( 1# T) where L equals length of reaction chamber; f = density; g =32. 2 ft/ sec.2; /2¯viscosity; b = coefficient of thermal expansion; T = temperature. The Prendtl Number EMI17.1 where C is specific heat; * is viscosity; K is thermal p conductivity. In removing hardness components, the heater tank is operated at a temperature of 105 F # 5 F, the fluid leaving the tank between 100 F and 110 F. Introduction of additional particulate matter by line 103 into the line 73 (effluent from the homogenizer tank 72) as noted earlier, provides 30; to more surface area in the final stages of magnesium conversion to magnesium carbonate and then to magnesium hydroxide (a solid). Magnesium oxide and magnesium hydroxide also promote silica removal. The reintroduced sludge at this point, composed of mechanically formed particulate matter, flocculants and precipitates, is very effective in assiting the soda ash in final removal of silica and magnesium. The electrical charge on the particulate matter also increases the rapidity and effectiveness of silica removal. Magnesium and calcium chlorides, sulfates and nitrates are converted to solid magnesium hydroxide and calcium carbonate. Since Ca and Mg exist in hard water primarily as chloride, bicarbonate and sulfates, they are removed by the present process. The way the present system handle hexavalent chromium and cyanides is of particular interest. As the recirculating gas stream of oxygen, nitrogen and sulfur dioxide contacts the particulate matter and soluble salts, the sulfite ion reacts with any metallic ions present. Hexavalent chromium is reduced to tribalent chromium in about 15 minutes at pH 2.0 to 2.5. As a reductant, the sulfur dioxide consumes oxygen but the latter is continually being replaced. In the iron reaction tank, ferrous sulfate is produced, which also acts as a hexavalent chromium reductant. This insures complete conversion to trivalent chromium. As the latter flows into the neutralization tank (with an initial pH of 8.0 to 8.2) its coupling with hydroxyl ion results in a light and voluminous precipitate which is continually mixed with the ferrous hydroxide that is changing to ferric hydroxide (a heavier precipitate). In a total residence time of about 30 minutes in tanks 70 and 72, this reaction goes to completion -- the precipitate continuing to be suspended as a result of air drive "churning" which maintains an oxygen-saturated medium - the pH eventually reaching about 10.5to 10.8 or 11. Discharge conduit 73 delivers a finely dispersed, charged particle that agglomerates rapidly in the region of the flocculation/sedimentation zone 92. When cyanides are present it is necessary to oxidize them to cyanate and thence to free carbon dioxide and nitrogen gas (both of which could be vented freely). If cyanide ion were oxidized in acidic medium, cyanide gas would result and require special handling precautions. Alternately, if cyanide is oxidized to cyanate in highly basic medium, it requires an extended reaction period. However, in the presence of the great amount of reactive oxygen carried by the particulate dispersion, cyanide can be oxidized to cyanate at pH 8.5 in approximately 5 minutes (in tank 70). If then this cyanate is exposed (i.e. returned by line 105) to oxygen and ferrous ion of the iron tank, an iron cyanate complex is formed. After passage through the blow tank 62, the flow reenters the neutralization tank 70 where hydroxyl ions react with the cyanate complex forming carbon dioxide and nitrogen. At the same time ferric sulfate is hydrolysed to ferric hydroxide; Fe(S04)3 + 6H = 2Fe (OH)3 + 3H2 S04 Upon grounding of the fluid, the ferric hydroxide separates as platelets which are as large as a quarter-inch across, dark red to black and firmly compacted in comparison with the fine, greyish, amorphous precipitate formed by ferrous hydroxide. Waste water treatment by the present system produced the foflowing- WATER PRIOR to % reduction of Initial con- Sludge concentate: TREATMENT centration found in Product specrographic Water prior to filtration analysis pH 5.1 . pH 7.2 2 pH 8.2;sp-gr,1.O94 Al 430. 0 mgll 0. 5 mg/l 99. 9% 33. 700 % by wt. Ca 616.0 536.0 13. 0 1.080 Mg 145.8 53.5 63.3 3.230 Boron 105.0 16.6 84.2 .190 Cu .009 Iron 700. 0 70. 0 90. 0 6. 670 Silicon 1.660 Titanium .640 Mn 1.3 .20 84.6 1.030 Sodium 13750. 1550. 0 88. 7 48. 230 Potassium 240. 14. 5 94. 0 2.810 99. 249,% Ammonia 5. 85 96. 6 Total hardness (asCaCo3) 2140.0 1560.0 27. 2 Fluoride 113.0 6.25 94.5 Chloride 1240. 152.0 87.8 Sulfate 32000 4050.0 87. 4 Phosphate .2 .2 Total Organic Carbon (TOC) 16. 0 18.0 mu/l Free Carbon Dioxide (as CO2) 20. 0 5. 0 Total Dissolved Solids 62338. 7598. 87.8 Total Solids 69514 7652 89.0 Suspended Solids 7176 54.0 99.25 Chemical Oxygen Demand 765. 0 38.3 95. 00 Volatile Solids 1599 464. 71. Dissolved Oxygen 0 4.5 Surfactants 2. 0 .6 70. Turbidity 18500 JTU 35.0 JTU 99.8 units Specific conductance @ 25 C. 45000 micromhos/ cm 7600 29.100 The unexpected usefulness of the present (water)treating process in killing and agglomerating viral and other monocellular life forms may be attributed to the cumulative effect or concurrence of a number of individual factors, at least some of which have a unique effect even alone. These factors are - (1) The broad band shift from extreme low to extreme high pH (i.e. 1.5 to 11), as well as residence at each end of the spectrum, effects the range of organisms of which individual groups may be resistant to acidic or basic media only, but not to extremes of both pH. (2) In this connection, the rapidity (e.g. 15 to 30 ;minutes) as well as the range or strength of the shift of pH appears important. kn organism could better acclimate or survive slow or mild change. (3) Residence time during which the whole medium or environment is undergoing treatment at each end of the flow-process, comprising gaseous inter-change, continued suspension/agitation, oxidation and ion exchange, is significant. (4) Relative density and composition of particulate matter in the flow-medium, compared to the volume of water being treated is an important parameter. (Total area particles cam2/1. = 130 to 13,280.) (5) The additional effect (attraction to living or newly dead cells) contributed by the galvanic charge which is carried by the particles is effective. In this connection, it is preferred to obtain the initial low adicity (plus galvanic charge) by introduction of sulfur dioxide, rather than by addition of formed acid, since the SO produces hydrogen ions and shifting electrons by disassociation of water. (6) Detergent action results from sulfonation of fat and oil components of the medium and especially from such ingredients which may form part of the viral/bacterium capsule/membrane. Protenaceous components of the membrane may also conjugate; subsequent salting out of the organic salts then exposes the cell contents to caustic attack or saponification. (7) Under these critical conditions, lime is particularly effective against some viruses. (8) Rapidity and completeness of flocculation is important, e.g. 5 to 7 minutes after grounding, in comparison with a minimum of 25 to 35 minutes or more which might be required in "merely clarifying murky water by flocculating with A1 or Fe ions. (9) The total kill is achieved without recourse to chlorine or other toxic agent, and without need to modify the treatment so as to target it at a specific organism first determined to be present. Such process can be used to '%arve6t" pestilential life forms for identification and study; by extracting samples from successive process steps, the susceptibility of the cell to each step is learned.

Claims: CLAIMS 1. A process for removing from a polar liquid as a solid substance, a dispersed soluble or suspended contaminant, of which any suspended particles thereof are characterised by Van der Waals effect and which contaminant is capable of solid existence at ambient operating temperature and pressure, characterised in that said process comprises (a) dispersing in said liquid a minimum of about 0.1%o w. random-moving particulate matter, which may either be added or be formed by fractionation of said contaminant when the latter is initially present in bulk, which dispersed particles thereof have a density of about 1.05 to about 2.0 and a size.of about 30 to about 225 microns with free surface energy of about 100 to about 500 ergs/cm2, and also reducing any additional solid matter present to such particle size, (b) providing an oxidation medium for such of the contaminant and added particles as may be capable of oxidation, by making such liquid acidic, intimately dispersing gaseous oxygen therein, and providing a supply of free electrons as by acidic dissociation of the polar liquid and by oxidation in situ of a heavy metal provided therein, which metal is characterised by the capacity of subsequently forming a flocculant precipitate in alkaline media, whereby a galvanic charge is imparted to the moving particles by random distribution and attachment of the electrons thereto, (c) maintaining said charge on the moving particles and restraining coagulation and phase separation of particles and soluble contaminants during successive oxidative reaction periods by agitation effected at least in part by flowing the liquid and its contents through electrically-insulated and flow-connected reaction vessels in intimate mixture with gaseous oxygen and at a variable flow rate defined by dimensionless parameters derived from the internal size and shape of the respective vessels and their connecting conduits,. (d) making said liquid alkaline, subsequently ceasing agitation and electrically grounding the alkaline liquid, whereby flocculating ions of the heavy metal provided therein, mutually precipitate the charged particles, the metal ions and soluble contaminants, thus yielding an oxygen-containing supernatent pure liquid. 2. A process as claimed in claim 1, in which said oxidation medium of (b) comprises sulfite and sulfurous ions and is made pH of about 2 to about 2.5, and said heavy metal comprises iron. 3. A process as claimed in claim 1 or 2, in which the liquid of (d) is made pH of about 10 to about 11. 4. A process as claimed in claim 1, 2 or 3, in which said polar liquid is predominantly water. 5. A process as claimed in any preceding claim, in which: (i) said flowable polar liquid comprises sewage/refuse containing bulk solids which are substantially reduced to the particle size of (a); (ii) an inorganic salt is a soluble contaminant of the polar liquid and is substantially removed therefrom in the precipitate of (d); (iii) the suspended contaminant comprises fecal matter which is reduced to the particle size of (a) in situ; (iv) sodium chloride is a soluble contaminant of the polar liquid which is water; (v) the soluble contaminant comprises hexavalent chromium or cyanide ion. 6. A process as claimed in claim 1, 2 or 5, in which said dimensionless parameters are selected from a group comprising Reynolds Numbers, Peclet Numbers, Lehman Reaction Numbers, Shape Factors, Schmidt Numbers, Contact Numbers, Weber Numbers, Grashaf-prandtl Numbers, and Stanton Numbers. 7. A process as claimed in claim 2, in which said contaminant comprises hexavalent chromium and said process includes the steps of reducing hexavalent chromium to trivalent chromium by reaction with sulfite and ferrous ions in the presence of ferrous sulfate at pH about 2.0 to about 2.5, then converting trivalent chromium to chromium hydroxide at pR about 10,5 to about 11.0, and jointly precipitating same in admixture with ferric hydroxide, 8. A process as claimed in claim 5, in which said contaminant comprises soluble cyanide and said process includes the steps of oxidizing the cyanide to cyanate at about PR 8.5 in said particulate carrying liquid, which liquid is substantially saturated with gaseous oxygen, then forming an iron cyanate complex by reaction of the cyanate with ferrous ion, then making the 1 iquid alkaline and converting the complex to carbon dioxide and nitrogen by reaction with hydroxyl ion. 9. A process as claimed in claim 1, in which prior to the flocculation of the charged particles and contaminants, there is reintroduced to said liquid about 15Só to about 3N,' of flocculated sludge plus soda ash, and the resultant mixture is heated at about 1000F to about ALOOF with agitation, and then flocculated as recited in (d), thereby increasing the removal of silica, magnesium and calcium from the liquid. 10. A process as claimed in claim 1 or 9 in which the heated liquid flow is moved through a zone adapted additionally to receive and intermingle therewith soda ash and recycled sludge, said flow being moved in accordance with the dimensionless parameters, Reynolds Number 30,000 to 40,000 and Grashof Prandtl Number product 25,600 to 230,000. 11. A process according to claim 1 or 2, in which (i) said oxidation medium of "b" is moved through a zone wherein said heavy metal produces free electrons, at a Reynolds Number of about 967 to 2900, a Shape Factor of 9.5 to 11.3, a Schmidt Number of 4 x 10-7 to 1.3 x 10-6, and a Contact Number of 228 to 446; (ii) said polar liquid is moved through a zone wherein gas is mixed therewith in accordance with the dimensionless parameters; Peclet Number 9 to 25, Shape Factor 9 to 10, a Reynolds Number of 400 to 500 for gas flow, 5000 to 10,000 with gas contact and 7000 to 18,000 without gas contact, a Lehman Reaction Number of 3.5 to 8 for blow tubes carrying gas into said zone, and a Stanton Number of 35.50 to 36.20; ; (iii) the alkalation of "d" is effected in a zone of liquid flow which is agitated by air moved countercurrent there through, said liquid being moved at a Peclet Number of t2 to 32 and the air being introduced therein by sparge lines having a Lehman Reaction Number of 3.4 to 4.4 or by blow shear tubes having a Lehman Reaction Number of 6.7 to 7.7, and B Stanton Number of 28.60 to 10,160; (iv) the flocculation and precipitation of "d" is effected in a zone wherein the flow is moved at a Reynolds Number of 2000 to 3700. 12. An assembly for purification of contaminated liquid including liquid flow control means, characterised in the following sequentially connected units; (a) liquid container means including associated means for selectively macerating solid components of a thus-contaminated liquid, and gas de#very/aeration means for passing gas into intimate admixture with said contaminated liquid and macerated components, (b) acidic treatment means, flow connected to said container means, and including means for regulation of pH by selective introduction of acidic and gaseous oxidizing reagents to the contaminated liquid, (c) container and reactant means, flow connected to said last treatment means, and comprising a source of soluble heavy metal ions adapted to mingle with the liquid flow stream, and means for subsequently aerating the liquid flow by passing gaseous oxygen therethrough; (d) neutralization means, flow connected to said last aerating means, and including proximate means for introducing alkaline reagent into the liquid flow, and a plurality of successively distal means for intimately mixing gaseous oxygen into the alkaline flow stream in amount adapted to restrain precipitation of contaminants by agitation thereof; ; (e) means for flocculating separable contaminant components of the alkaline flow stream, substantially concurrent with electrical grounding of said stream, and switch means for electrically grounding said alkaline flow stream, each of said units starting with (b) being electrically insulated from ground support, and said flocculating means (e) being electrically insulated from the preceding flow connected unit, whereby a galvanic charge may be imparted to solid particles of the liquid flow by pH regulation and electrons of said soluble heavy metal ions and such charge maintained until discharged by the switch means. 13. An assembly as claimed in claim 12, which includes between units (d) and (e), means for simultaneously heating and agitating the alkaline flow stream while continually restraining precipitation. 14. An assembly according to claim 12, in which unit (d) comprises an elongated chamber and said oxygen mixing means which is located distal to the alkaline introducing means, comprises successive downstream gas delivery conduits individually having ejection nozzles transversely disposed within the flow stream at successive staggered angular displacement from the longitudinal axis of the chamber, which conduits have individual flow control means whereby the gas inflow therethrough may be adjusted to changing turbidity of the flow stream immediately adjacent each nozzle. 15. Potable water derived from contaminated liquid or potable water and an aggregation of minute metallic particles individually derived from a liquid suspension containing said particles whenever obtained by the process or apparatus claimed in any of the preceding claims.

Inventors: ALEXANDER, JOHN A., LINDMAN, WILLIAM EDWARD
Applicants: ALEXANDER, JOHN A., LINDMAN, WILLIAM EDWARD
Application year: 1978
Main classification: C02F1
IPC codes: C02F1, C02F9