Method of insolubilizing demineralizer and cooling tower blowdown wastes
United States Patent 1191 Dulin et al.  
 1 1 METHOD OF INSOLUBILIZING DEMINERALIZER AND COOLING TOWER BLOWDOWN WASTES [75] lnventors: Jacques M. Dulin, Libertyville, 111.;  
 Edward C. Rosar, Lakewood, Colo; Harvey S. Rosenberg, Columbus; Joseph M. Genco, Gahanna, both of Ohio Primary E.ruminer-Allan Lieberman Attorney, Agent, or Firm-Jacques M. Dulin, Esq.  
 [57] ABSTRACT Process for insolubilizing water soluble sodium sulfur oxide wastes resulting from backwash of process feedwater demineralizers and cooling tower blowdown wastes. The sodium sulfur oxide wastes, typically sodium sulfate and sulfite, are reacted in solution with ferric ions and sulfuric acid to produce an insoluble, basic hydrous or anhydrous sodium hydroxy ferric sulfate or sulfite compounds of the type QvFe (SO,1-),, (OH)z&#39;nHzO, wherein Q is NH, or Na, v is 1,2, 4 or 5, w is selected from 1, 2, 4 or 6, x is 3 and/or 4, y is 2,4,5 or 7,zis 1,2, 3, 6, or 12, andn isOor 3. The principal insoluble compounds include Natrojarosite. Metasideronatrite, Sideronatrite, Depegite which is a mixture of Sideronatn&#39;te, Rosarite and lriite, and mixtures thereof. The reaction takes place at an acid pH in a temperature ranging from about 50-300F and may occur in single or multistage reactors. Air and/or bacterial activation at a pH of less than about 5.5 may be employed. The end-product basic, sodium hydroxy ferric sulfate and sulfite compounds are substantially water insoluble, having a sol ubility of less than the standard calcium sulfate, and may be disposed of by simple landfill without the water pollution hazards inherent with landfilling of wet or dry sodium sulfitc or sulfate wastes.  
 22 Claims, 5 Drawing Figures A w /8 Mar/g r 0 29/ 9 f 30 4 x MAKE up 6 75227 557 s U 4 RAW WATER J //V 0L 81L IZ T/O/V ma: rmwr L 1 9 5 L 110 f 2/ END 3/ pmooucrs A DISPOSAL 29 NUCL EAR 0!? c FOSS/L FUt&#39;L POWER .5771 wow sew/1a.: 23 DIP/F7 R gga gin j EVA/P 36 z 2 67/962122 g/va 27 26 33 32 22 W T r 0/1. Y r V 7 WASTE V EM co m xei 7&#39; W sip M To? f #9133 RFC E mow/as TE 38 W504 (/52: arm/ma: r r sums:  
 BfiS/N METHOD OF INSOLUBILIZING DEMINERALIZER AND COOLING TOWER BLOWDOWN WASTES RELATED CASE This application is related to our co-pending application, Ser. No. 353,508, filed Apr. 23, 1973 and titled PROCESS FOR INSOLUBILIZING POTENTIALLY WATER POLLUTABLE WASTES FROM SODIUM OR AMMONIUM TYPE SULFUR DIOXIDE AIR POLLUTION CONTROL SYSTEMS now abandoned in favor of continuation-in-part application Ser. No. 4| L367, filed Oct. 31, 1973. The disclosure of that application is hereby incorporated by reference.  
 FIELD The invention relates to insolubilizing wastes from the treatment of water for biological, agricultural, chemical or process use such as demineralizer treatment of boiler feedwater, and wastes resulting from blowdown of cooling towers. More specifically, this application relates to reducing the solubility of sodium sulfite and sulfate wastes by a factor of l&#34; to l0 to produce a solid product which may be simply disposed of by landfilling without posing serious water pollution problems. The end-products may be characterized as basic, insoluble ammonium or sodium hydroxy ferric sulfate and sulfite compounds which may be in an anhydrous or a hydrated state. The typical source sodium sulfate or sulfite wastes may be demineralizer wastes from boiler feedwater prepared for nuclear or fossil fired fuel power plants and the blowdown sludge from nuclear or fossil fired fuel power plants.  
 BACKGROUND As the emphasis on cleaning up water pollution sources increases. sodium sulfate and sulfite compounds have been recognized as posing difficult problems for disposal. The sodium sulfate and sulfite compounds are normally highly soluble in water, on the order of 200 grams per liter at normal, ambient conditions. The sodium salinity represents serious problems from the point of view of agricultural use, and excess sodium in river waters such as the Colorado River violate international treaties if permitted to exceed stated limits. There are currently proposals for cleanup of such rivers which cleanup represents a national investment in excess of $500 million.  
  Further, in many agricultural or industrial processes water must be treated, i.e., demineralized, prior to use because ambient water sources are already too dirty and introduce cations and anions which interfere with physical or chemical processes. For example, boiler feedwater must be demineralized because contents of sodium, sulfate, chloride. silica and other anions and cations lead to boiler tube failure, scaling and the like. Thus, lake and river feedwaters are normally treated today by a series of anion and cation exchange beds to thoroughly demineralize the water and prepare it as a feedwater for boiler, condenser, and makeup feedstock water. These resins are periodically backflushed, i.e., recycled, and the backwash wastes can contain l525,000 ppm sodium sulfate. These exceed current limits proposed for sodium sulfate effluents into natural streams.  
  Another area of need is in connection with cooling towers for various types of commercial and industrial processes. For example, commercial air conditioning cooling involves packed or hyperbolic type cooling towers in which a certain percentage of the water is recycled. A slipstream or blowdown stream is removed from the cycling waters as it gets more concentrated due to the recycle of the water through the cooling tower. This problem is highly aggravated where very large cooling towers are used in connection with fossil fuel fired or nuclear power plants. For example, a nuclear station generating approximately 2,000 megawatts may have a cooling tower involving a circulating water system employing 1.096 million gallons per minute and makeup water on the order of 56,000 gallons per minute. Approximately 36,220 gallons per minute are lost by evaporation or drift. For every 4,500 gallons per minute of the water passing through softeners, a blowdown sludge or magma in the amount of approximately 3.4 tons per hour of percent solids containing approximately 8,400 parts per million sodium sulfate is removed. This is 15 tons of magma per megawatt per year;  
  As the nations power needs increase, and thermal pollution codes require an increasing number of cooling towers to be used in connection with power or industrial plants and environmental air conditioning, the amount of this waste sludge material will increase.  
  In a sense, the thermal pollution problem and the cleanup of already dirty water streams to the purity required for industrial processing, has generated still another pollution problem: a water pollution problem. This problem is not solved by merely drying the sludge materials because disposal of the dry materials are still prone to leaching and finding their way back into the ambient groundwater unless their solubility is substantially reduced.  
  Therefore, there is a real need for a process for reducing the solubility of sodium sulfite and sulfate wastes from concentration of these compounds in industrial power and processing operations, and which results in a material which can be readily landfilled without posing the potential water pollution currently posed by such wastes.  
 THE INVENTION OBJECTS It is among the objects of this invention to provide a process for reducing the solubility of sodium sulfite and sulfate wastes.  
  It is another object of this invention to provide a process for reducing the solubility of sodium sulfite and sulfate wastes resulting from industrial water preparation operations and power plant cooling tower blowdown.  
  It is another object of this invention to produce a double salt or co-precipitate of ferric sulfate and sodium sulfite and sulfate wastes which end-products are reduced in solubility more than one-hundred fold from the starting sodium sulfate or sulfite materials.  
  It is another object of this invention to provide a simple process at relatively mild conditions which results in a relatively insoluble end-product which can be easily landfilled and which does not pose the problems of a water-retaining sludge material. 0  
  Still other and further objects of the invention will be evident from the description which follows.  
 sented by SUMMARY Sodium sulfite or sulfate-containing solutions, derived from demineralizer or blowdown wastes are reacted abiotically or biotically in a single or multi-stage reaction with ferric sulfate solutions, derived in turn from an iron-containing source in a sulfuric acidcontaining liquid at a temperature between about 50-300F at an acid pH to produce sodium hydroxy ferric sulfite or sulfate products which may be anhydrous or hydrated. These end-products are generally crystalline, water insoluble (as compared to calcium sulfate), and may be easily dewatered and dried, and I thereafter landfilled, without posing severe water pollution problems.  
  The sodium sulfate or sulfite-containing solution is passed into a single or multi-stage reaction tank which is generally maintained in the temperature range of from about 50300F at an acid pH, generally below about 5.5 and preferably in the range of below about 3.5. A ferric sulfate or a ferrous sulfate material or solution may be charged into the reactor. The reaction may occur in the presence of air and/or bacterial activation as optional conditions. In the alternative, elemental iron in the form of high iron content groundwater, scrap iron, steel furnace dust, iron-containing fly ash, iron wastes from local municipal incinerators, iron-containing slag, iron pyrites from coal washings, mine waters containing iron, or industrial process wastes containing iron may be used as a source of iron (Fe). ferric ion, or ferrous ion. In addition, a source of sulfuric acid, alone or in combination with the iron charge, is introduced to the reactor. Typical sources of the sulfuric acid include sulfuric acid from other pollution control processes such as are employed in smelter operations. industrial waste waters containing sulfuric acid, mine waters such as black water, or sulfuric acid from a side stream of the flue gases of fossil fuel burning power plants or boilers. If sulfuric acid is employed, it may be of an extremely crude type of relatively low concentration. Pickle liquors or pyrite or gob dump leachate are good sources of ferrous/ferric ion and sulfuric acid values.  
  The reaction is maintained in a tank for a time sufficient to produce the sodium hydroxy ferric sulfite or sulfate insoluble products which precipitate at the bottom of the tank, typically in IQ minutes to 3 days and preferably 30 minutes to 24 hours. The tank may be perated at a variety of pressures, subor superatmospheric. but ambient atmospheric pressure is preferred. Air may be bubbled through the reactor in order to promote the conversion of elemental iron to ferric ion. and/or to promote bacterial activation of the reactions.  
  The reaction tank may be operated abiotically, or optionally can be charged with one or more bacterium of the type which oxides sulfur and iron. For example, one or more iron bacterium of the genus Thiobacillus (ferrooxidans, rhiouxidans, cuncretivorous, neopolitanus, or lhioparous), Ferribacillus ferromidans, or an acidtolerant filamentous iron bacterium of the genus Metallogenium may be employed. Bacteria other than those mentioned may also be employed.  
  Generically, the compounds produced in accordance with the instant process may be described as hydrous (hydrated) or anhydrous, insoluble basic hydroxy ferric sulfites and sulfates, or mixed sulfates which are reprethe formula Q,.Fe,,.(SO,),,(OH),.nH O,  
 wherein v 0-5, w 0-6, .t 3 and/or 4, y l-5, z O-l2, and n 0-20. Q is NH or Na.  
  An analysis of the end-products shows that they may be generally classified as insoluble, as compared to the standard in the industry, calcium sulfate: 2.3 g/l at RT. CaSO, has been taken as the standard in view of the fact that it is an end-product sought to be produced by air pollution control processes involving contact in a liquid system of lime or limestone with flue gases containing S0,. Calcium has been the material of choice, in spite of severe problems internal to the scrubbers, because of the relative insolubility of the end-product calcium sulfate. The end-products of this invention are [0 to I00 times less soluble generally than the calcium sulfate. This is a reduction in solubility of approximately 10 to 10 times as compared to the starting sodium sulfite/sulfate waste materials.  
  The end-product may be a mixed precipitate, the components of which vary depending on the pH of the reaction tank or tanks. For example, Sideronatrite Na Fe(SO,) OH.3H O and Metasideronatrite Na,Fe SO ),(OH) .3H O may be produced at a pH of below about 2.0, while Natrojarosite NaFe (SO,) (OI-l may be produced at a pH below about 4. Depegite Na -,Fe,(- SO (SO (OH) .3H O, Rosarite Na Fe(SO OH.3- H 0, and lriite NaFe (SO (OH) may be produced at a pH between about 2.2 5.5. Depegite appears to be an empirical compound&#34; containing Sideronatrite, and Rosarite and lriite, which are sulfite analogs of Sideronatrite and Natrojarosite.  
  The presence of other metal cations such as copper, lead, silver, zinc and the like naturally present in these waste waters do not interfere. Indeed, such metallic ions can be scavenged by co-precipitating with the above sodium compounds, as for example Argentojarosite AgFe (SO,) (OH) Beaverite Pb(Cu,Fe,Al),-, (SO,) (OH) Plumbojarosite PbFe (SO,),(OH), and the sulfite analogs.  
 FIGURES The detailed description which follows has reference to the drawings in which like parts have like numbers and wherein:  
  FIG. 1 is an overall schematic flowsheet of the application of the invention to a power plant which produces both demineralizer and blowdown wastes;  
  FIG. 2 is a schematic flowsheet of the raw water treatment portion of the station water use operation shown in FIG. 1;  
  FIG. 3 is a schematic flowsheet of the makeup water treatment system and chemical effluents portion of the station water use flow diagram shown in FIG. 1;  
  FIG. 4 is a schematic flowsheet of the cooling tower portion of the station water use operation shown in FIG. I;  
  FIG. 5 is a schematic of the insolubilization reaction tank portion of the process.  
 DETAILED DESCRIPTION The detailed description of the embodiments of this invention are by way of illustration and not by way of limitation of the present process.  
  Referring to FIG. I, an industrial or power plant 1 employs service water from river 2 via service water intake line 3. As shown in these figures, the plant is a power station, more particularly a nuclear or fossil fuel station. As shown particularly in the figures, reference will be made to a nuclear power station, but it should be understood that other power stations or industrial plants employing demineralizing water treatment systems and/or cooling tower systems are encompassed within the scope of this invention. It should also be understood that the water source need not be river 2, but may be a lake, well water, reservoir water, or ocean.  
  The raw service water drawn in through intake line 3 is passed through a raw water treatment plant 4 which is shown in more detail in FIG. 2. The water is filtered, passed through cation exchange resins, degasified, and stored before being distributed to domestic water system 5 and as feedstock for the makeup water treatment system 6 set forth in FIG. 3. Filter backwash wastes are passed via line 7 to discharge basin 8.  
  Approximately three-fifths of the raw water treated in plant 4 is directed via line 6 to the makeup water treatment system 9, which is described in more detail with respect to FIG. 3. Discharge from acid regeneration of strong cation exchangers in system 9 are recycled via lines 10 and II back to raw water treatment system 4 wherein they are used to regenerate the weak cation exchange resins. The resultant discharge is directed via line 12 to neutralization tank 13. In makeup system 9, the processed raw water feed in line 6 is treated sequentially in strong acid cation exchangers, weak base anion exchangers. strong base anion exchangers and mixed bed demineralizers, as will be explained in detail below, prior to storage and distribution via line 14 to the main condenser, line l5 for miscellaneous demineralized water requirements (laboratory. regeneration. auxiliarly processing, etc. and line 16 to the auxiliary boiler. Discharge 17 from the strong and weak base anion exchangers, and discharge 18 from the mixed bed demineralizers are distributed to the neutralization tank 13. The various discharges 12, I7 and 18 tend to neutralize themselves in tank 13 and the effluent is discharged via line 19 to the insolubilization system described in more detail below with respect to FIG. 5. In the alternative. acid discharges from lines l2, l7 and I8 may be passed directly to reactor tank 98 (see FIG. 5).  
  The prepared water in lines 5, l4, l5 and 16 are uti lized in the plant I in a conventional manner. This aspect of the prepared water use is not part of this invention. In producing product 21, here power, the plant 1 produces excess heat which is dissipated by a circulating water system 22, 23 and cooling tower system 24, which is described in detail below with respect to FIG. 4. Service water discharge 25 may be used as makeup for the cooling tower requirements. The cooling tower operates to evaporate water 26 in cooling and some is lost as mist or drift 27. Direct use of river water 1 via line 28 may also be employed as cooling tower main or makeup water source. The cooling tower evaporative system also discharges a sodium sulfate-rich (l025,000 ppm) blowdown magma of approximately 90 percent solids which is directed via line 29 to the insolubilization system 20. The magma 29 and sodium sulfaterich neutralization tank effluent 19 may be directed separately to the insolubilization system 20, or via line 291 combined as a single sodium sulfate-rich feed stream 30 to the insolubilization 20.  
  Clarified stream 31 exiting from the insolubilization is fed to discharge basin 8. Sanitary wastes from the station facilities are treated in sewage treatment plant 33 with treated effluent 34 being sent to discharge basin 8. Non-radioactive wastes 35 from the administrative building plant, warehouse and shop are treated to separate oily wastes in separator 36 with effluent 37 to discharge basin 8. These treatments are conventional and do not form a part of this invention. Likewise, in the case ofa nuclear station, low activity radioactive waste is conventionally treated with ion exchange resins 38, and the decontaminated effluent 381 is directed to discharge basin 8, bypassing the insolubilization operation 20 (shown in dashed lines in FIG. I). This radioactive waste, and high activity radioactive waste may be treated by conventional processes for disposal and does not form a part of this invention. Runoff waters 39 from storm and roof drains are discharged to the ambient water source 2, as is the flow 40 from dis charge basin 8.  
  Turning from this overview of the water sources and discharges from a station in normal full power operation to the detailed treatment steps, FIG. 2 shows a conventional raw water treatment system 4. Raw water 3 is distributed to two upflow filter units 41, 42 to re move solids, and the backwashed solids wastes 7 are directed to the discharge basin 8 (FIG. 1). The filtered water 43 is transferred to clearwell tank 44, and then is pumped by transfer pumps 45, 46 through weak acid cation exchangers 47, 48 and degasifier 49 where excess C0 115, is removed. Pumps 50, 5] transfer the treated water to storage tank 52. For regeneration of exchange resins 47, 48, the spent acid regenerant used to regenerate the strong acid cation resins in the makeup water system 9 (FIGS. I and 3) is introduced via lines 10 and 1] to the weak acid cation exchangers 47, 48 during the regeneration cycle. The spent regenerant is combined in line I2 and transferred to the neutralization tank I3 (FIG. 3).  
  Turning now to FIG. 3, the makeup water feed stream 6 from the raw water treatment system 4 (FIG. 2) is divided in lines 53, 54 to pass through strong acid cation exchangers 55, 56, and then through weak base anion exchangers 57, 58 via lines 59, 60. After treatment in the weak base anion exchangers 57, 58 the treated water is passed via lines 61, 62 through strong base anion exchangers 63, 64, transferred to mixed bed demineralizers 65, 66 via lines 67, 68 and combined and collected via line 69 in demineralized water storage tank 70 and condenser water storage tank 71. As described above. the demineralized water in tank 71 is fed via line 14 to the main condenser, and both auxiliary boiler water and miscellaneous demineralized water requirements are withdrawn via lines 16 and I5, respectively, from storage tank 70,  
  The regeneration cycle of the exchange resins and demineralizer beds is as follows. Acid regenerant 7] is fed through the strong acid cation exchange resins in beds 55 and 56 via lines 72 and 73, with the partially spent acid and effluent in lines 10 and It being used as the regenerant for the cation exchange resins 47, 48 (in FIG. 2 Caustic regenerant 74 is passed via lines 75, 76 first through the strong base anion exchange resins in beds 63, 64 and the partially spent caustic in lines 77, 78 is then used as the regenerant for the weak base anion exchange resins in beds 57, 58. The spent regenerant containing exchanged ions in lines 79, 80 are combined in line 17 and sent to the neutralization tank 13. Acid and caustic regenerant 81 is passed via lines 82, 83 to mixed beds 65, 66, with the waste effluent withdrawn via lines 84, 85, combined in line 18 and sent to neutralization tank 13.  
  The chemical discharge in neutralization tank 13, representing the combined effluent of excess spent regenerants and released ions in lines l2, l7 and 18 would have the following typical composition shown in Table I.  
 This is treated in the insolubilization tank 20 described in more detail below. It should be understood that the above values depend on the type of raw water source 2. and only the effluent 12 from the cation exchangers and/or the effluent from the anion exchangers 17 need be treated. Typical ranges are shown in Table II with both weights and ppm represented as equivalent to CaCO per day (per regeneration):  
 purity makeup water for the turbine side of the steam generator.  
  Quality requisites for the makeup water include specific conductivity less than 1.0 micromho/cm and a silica content no greater than 0.01 ppm. The specific pretreatment and ion-exchange system used to achieve these requirements varies with the quality of the raw water. With respect to deionization of the clarified raw water, a combination of multipleand mixed-bed resins usually provides the required quality with operating economy. The following resins may be used in sequence: Duolite (Diamond Shamrock Chemical Co.) C-ZO A-IOZD (or A-30B), C-20 A-lOlD, mixed bed of C-20 and A-l0lD, or equivalent. The first pair removes the bulk of the ionic impurities and the second pair polishes the first pair effluent to a high degree while the final mixed bed eliminates traces of ionic impurities. Regenerant economy is enhanced by utilizing excess caustic soda from regenerating the A-lOlD of the mixed bed to assist in regenerating the anionexchange resins of the preceding pairs. If the source water contains appreciable amounts of organic matter, the deionization train may be preceded by a bed of absorbent resin (such as Duolite 5-37) to minimize organic fouling of subsequent strong base anion exchang ers in the train.  
  A full flow condensate purification ion-exchange system can be used to remove dissolved and suspended impurities which may result from condenser leaks or from corrosion/erosion of equipment. These impurities tend to concentrate in the reactor loop. Their removal These represent reasonable ranges of extremes represented by ambient water supplies. The Na SO component is by far the greatest pollutant in the waste streams as seen from Tables I and II. In Table ll, the ppm N21 SO, can be approximated by multiplying the Na or SO,&#34; ppm (reported above as equivalent CaCO by 1.5.  
  lon-exchange resins are useful in the operation of nuclear reactors to produce makeup water of the requisite high purity, to control coolant activity levels, to minimize corrosion. and to remove or reduce the radioactivity present in a variety of low-level radioactive wastes. The makeup deionization system treats the clarified raw feed water to produce high-purity water for the core coolant. This system purifies the raw feedwater to supply high-quality reactor coolant makeup for either the boron-shimmed or non-shimmed pressurized or boiling water nuclear water reactors. The current trend is toward the use of the borated shim for pressurized reactors. The system also furnishes highserves to control radioactive content in the coolant and prevent crud deposition on core surfaces which reduces heat transfer and interferes with coolant circula-&#39; tion in the reactor.  
  A condensate ion-exchange unit also serves to remove minute quantities of silica which may escape from the makeup deionizer. It thus provides insurance against build-up in the turbine loop and consequent scaling of turbine blades and heat-exchange surfaces.  
  A mixed bed of Duolites ES-26 and ES-l09 may be used for high flow-rate condensate polishing. This is a combination of macroporous cation exchanger and gelular anion exchanger. The Duolite ES-26 can be operated in the hydrogen form or the ammonium form, as needed for pH control. The Duolite ES-l09 is used in its hydroxide form. The optimum screen analyses and chemical characteristics of these resins allow effective simultaneous filtration and deionization at flow rates up to gpm/sq.ft.  
 Termination of the exchange resin runs are usually based on increased pressure drop due to crud&#34; removal rather than on conductivity breakthrough. Regeneration is usually conducted externally, i.e.. the resins are transferred to separate regeneration vessels wherein they are &#34;scrubbed&#34; and chemically regenerated, and then returned to the exchanger vessels.  
  Turning now to FIG. 4. hot water from the plant in line 22 is piped to cooling tower 24 of the station for evaporative cooling and return via line 23. In its cooling operation. a portion of the water is lost via evaporation 26 and drift (mist) 27. As the water is evaporated the concentration of soluble and insoluble solids increases, for example. as shown in Table III:  
 TABLE III Average Daily Concentration Increase in Cooling Tower Blowdown Dissolved Solids Therefore. a slipstream portion 86 of the recycling water must be continuously removed and purified before return to the circulating water system 22. 23. As needed, makeup water is supplied to the tower from the service water discharge 25, or direct from the ambient water source via line 28.  
  The slipstream 86 is passed through softeners containing ion exchange resins for removal of hard water ions. and results in a softened blowdown stream 89 and an insoluble softener sludge 88 which may be landfilled by conventionaltechniques. In a circulating water system 22, 23 of 1.096.000 gpm, the blowdown stream will amount to about 4.490 ppm (.457r) and is at approximately 90F. Of this, 3,140 gpm (70%) is recycled via lines 90 and 91 to the cooling tower inlet line 22. The 30% balance of [.350 gpm (679.000 lbs/hr) of the blowdown liquor in line 92 is then passed through a multi-stage flash evaporator 93 having an evaporation ratio of about 8.0 where the temperature is raised to 230F from the 90F inlet temperature. Approximately 2/3. or 900 gpm (450,000 lbs/hr) of water is evaporated off. recondensed and the purified condensate returned to the cooling tower inlet stream 22 via lines 94 and 9l. The concentrated bottom liquor third 95 in the amount of 450 gpm (230.000 lbs/hr) is then passed to evaporator crystallizer 96 where 439 gpm (224,450 lbs/hr) of water are evaporated. recondensed and the purified condensate water returned to the cooling tower inlet 22 via lines 97 and 91. The residual magma or cooling tower blowdown sludge in line 29 amounts except for water content. as the line 89 liquor composition )2 Turning to FIG. 5. the sodium sulfate-containing waste solutions l2, 18. I9 and 29 are delivered individually or mixed together via lines 291. 30 and 30] to insolubilization system 20. which comprises reaction 0 tank 98, underflow line 99, filter 100. and recycle line to 6,790 lbs/hr solids and 755 lbs of water (90% solids.  
 [0% water) of the following composition (taken by sample from line 89 prior to concentration in line 29&#39;. line 29 magma has substantially the same composition,  
  The reaction tank is maintained at 50300F at a pH below about 5.5. and a source of iron and sulfuric acid is added. as shown by line 102. The iron may be elemental Fe. ferrous ion Fe. or ferric ion Fe in solution. or supplied as a salt. preferably Fe (SO The sulfuric acid may be crude waste acid or any other source. The iron and acid may be added separately or together. A convenient source of waste acid and iron is acid mine water. pyrites dump leach water. or steel pickling liquor, all of which contain suitable concentrations of ferrous or ferric iron and sulfuric or sulfurous acid. Further details ofthe acid and iron sources are incorporated by reference from our co-pending application. Ser. No. 353.508. filed Apr. 22. 1973.  
  Where the sulfate wastes in line 30 are too dilute. an evaporator or evaporator crystallizer 103 may be used to increase the concentration of sodium sulfate in line 301. and condensate removed by line I04. This condensate may be used as the filter rinse water source 105. The feed in lines 29 and 301 is preferred to be highly concentrated or dry. so that by control of water input via line I01. the ionic concentration in the reactor 98 may be controlled.  
  The iron is preferred to be in the ferric ion form when delivered to the reactor tank 98. Where, however, the iron is available primarily or only as Fe or ferrous ion. the process contemplates both abiotic iron oxidation and biotic oxidation with one or more bacteria of the genus Thiobacillus (ferrooxidans. rln&#39;ooxidans. concretivorons. neopolimnus. or rlu&#39;oparus). the genus Ferribacillus (such as ferroaridans). and acid-tolerant filamentous iron bacterium of the genus Metallogenium. The abiotic ferrous iron oxidation is directly dependent on the pH above 4.5. indirectly pH dependent between 3.5 and 4.5 and is relatively constant below at pH of 3.5. In general. abiotic ferrous iron oxidation is slower at a lower pH. For example, abiotic oxidation is approximately 8.200 times slower at a pH of 3.5 than at a pH of 5.5.  
  In the mesoacidic pH range of about 3.5 to 6.5. the Metallogenium bacterium and its heterotrophs are particularly suitable for iron or pyrite oxidation and degradation. As a result of the activity of the Metallogenium on the iron and sulfur present in the solution, the pH drops into the 3-4.0 range. The Metallogenium grows in multi-branching colonies of interweaving ferric ironencrusted stalks having a diameter of 0.1 to 0.4 microns. The stalks are characterized as not having a conventional cell body. The upper tolerance of the Metallogenium is approximately 150 micrograms per liter of ferrous iron produced as a result of the oxidation of elemental iron.  
  As the pH decreases and ferrous ion concentration increases, the activity of the Metallogenium bacterium is self limiting, and conditions become more nearly conducive for activity of the Thiobacillus ferrooxidans which has an optimal activity below a pH of 3.5. The latter bacterium completes the ferrous to ferric ion oxidation and brings the pH down to around the l.5 to 2.5 range. Where required, a source of carbon dioxide and nitrogen, typically in the form of ammonium, may be supplied to the bacterium medium to support growth. The resulting biotically-produced ferric ion solution, rich in sulfuric acid, may then be provided to the reaction tank 98 as above described in detail.  
  The preferred conditions are a pH below about 3.54.0 with a pH below 2.5 being particularly preferred. The temperature is preferably in the range of l-200F at atmospheric pressure, with l-l80F being particularly preferred.  
  Waste heat from steam, or water in line 22, may be used via line [06 to maintain the reaction temperature. At these conditions, the predominant precipitate will be Sideronatrite, and where ammonium is present, Ammoniojarosite. As the pH drops into the l .5 range in reactor 98, the predominant precipitate will be Sideronatrite. As the pH drops still further to the range of 0, Ferrinatrite will precipitate. The Ferrinatrite precipitate is generally water soluble. but on standing in moist air can convert to Sideronatrite. Thus where the pH gets down below the preferred 1.0 range and Ferrinatrite is formed, the underflow may be washed in water or let stand damp to either remove the Ferrinatrite or convert it to Sideronatrite insoluble precipitate.  
  The preferred pH range for the production of Natrojarosite or Ammoniojarosite is in the range of 1.8 to 2.5, 1.5 to 2.0 for Sideronatrite, and 0 l.0 for Ferrinatrite. The ferric ion for all these compounds preferably should be present in a concentration on the order of about 4 grams per liter or above. Excess alkalinity and oxygen should be avoided, since these conditions promote oxidation of iron to iron hydroxide compounds such as Fe(OH) Fe(OH) or FeOOH, which reduce ferrous and ferric ion availability without bringing down sodium and sulfate ions. Further, such hydroxides are gelatinous precipitates which are difficult to separate, dewater or dry.  
  An important aspect of this invention is the ability to operate at moderately acidic pHs and at low ferric ion concentrations, thereby reducing iron and acid requirements, while pulling down high quantities of sodium and sulfate ions. Operation at moderately acid, oxygenated conditions is made difficult by the relatively easy formation of Fe(OH) Fe(OH) and FeOOH at such conditions. While these hydroxides are insoluble, the point is not to remove Fe from the solution, but to use Fe to insolubilize the Na SO This is aggravated by the fact that it would be easier and cheaper to operate at higher pHs, since less acid would be required, yet the ferrous/ferric hydroxides production is more rapid and complete at such pH values.  
  The insoluble precipitates of this invention may be selectively produced in the ferrous/ferric hydroxides pH range to the substantial exclusion of such hydroxides by starting the Sideronatrite, Natrojarosite, Ammoniojarosite, etc., precipitation at high Fe, Na, 80, concentrations and low pH to suppress ferrous/ferric hydroxides precipitation. This is followed by gradually permitting the pH to rise and the ferric ion concentration to fall. The Sideronatrite, and NHJNajarosites precipitation may thus be extended with good yields into the pH regions where typically one would expect ferrous/ferric hydroxide precipitation to predominate, yet only a minor proportion of those hydroxides form. [n the alternative, a low ferric ion concentration, low pH, solution may be seeded with Sideronatrite or NHJNa-jarosite crystals, and thereafter the pH adjusted to the higher range without substantial yield interference by the Fe /Fe hydroxides.  
  AS a source of both sulfuric acid and ferric ion, pyrites leachate is particularly suitable since the instant process provides for disposal of the pyrites leachate which otherwise would pose a pollution problem. At present, a typical coal containing from 2-6 percent sulfur may have removed therefrom by washing at the mine or at the power plant approximately 0.5 percent sulfur in the form of pyritic sulfur. The resulting iron pyrite material is ordinarily disposed of in a mine dump. Over a period of time, however, the iron pyrites may be abiotically or bacterially oxidized to form ferrous and ferric ion, and dilute sulfuric acid from the sulfur contained therein. The resulting mine waste water is a pollutant.  
  Indeed, both the sulfuric acid and iron content required for the present process can be provided from waste mine water since it typically contains a dilute sulfuric acid and ferrous or ferric ion content. For example, mine waters ordinarily contain about 300 milligrams per liter total iron content and may have a pH below about 5.5, typically on the order of 2.0 to 4.0. Where necessary, these mine waters may be concentrated before charging to reactor tank 98.  
  ln the alternative, an otherwise pre-prepared concentrated solution of ferric sulfate, ferric ion, and/or sulfuric acid is provided through line 102. A typical source of the pre-prepared concentrated solution in line 102 would be a waste pickle liquor from steel manufacture. For example, a typical pickle liquor has a composition 87.1% by weight H O, 4.6% free H,SO,, and 8.3% FeSO, (30.6 g/l) having a pH of about 0.1.  
  For fossil-fuel fired power plant or smelter, a convenient source of heat and sulfuric acid is to provide a sparger tube 109, to which is provided a slipstream of flue gas at 200650F. This gas also contains CO and S0,. The CO, can provide the bacterial CO requirements. Alternately, C0 115 from degasser 49 (see FIG. 2) can be sparged in tank 98 as shown in FIG. 5. The S0, in contact with the water forms sulfurous and sulfuric acid supplying those requirements to the insolubilization system. The sparger bubbles also afford an optional stirring action. Condensate may be withdrawn from the reactor via line 108 and optionally supplied to filter 100 as rinse water 105. Where hydrogen is produced, it may be withdrawn via line 107. Nonnally, in the case of a preprepared concentrated ferric and/or sulfuric acid solution with the reaction occurring abiotically, hydrogen tends not to be produced.  
  By comparing the overall reactions for the production of Natrojarosite:  
 they may include Metasideronatrite, Ferrinatrite, Depegite, Ammoniojarosite, Rosarite, and lriite or a mixed precipitate, and/or other metal-containing ana- Nmmjnome Recicled logs of hydrated or anhydrous basic sodium or ammoniwith the overall reactions for the production of Sideroum-containing metallic sulfates or sulfites such as natrite: Plumbojarosite, Argentojarosite, Beaverite, Alunite,  
  Natroalunite. and the like, depending on the sulfate 2F 2H so 7F so H wastes heavy metals content, or the content of such 4.) e&#34; e 54 ZFCSO E 6 lhofljaFeisona+ H2O m metals in any of the other reactants, be they fly ash. ash or) Feflsofl h tank waste water, black water, leachate. pickle liquor 2Na,SO +8l-l,O- 2Na,Fe(SO OH.3H O+H O+H,SO, R Td or h ]ik s &#39;t &#39;dnmm me c It should be understood the heavy metals content can it can be seen that the overall can factor (the ratio of F P i g i z Ti p ffi gg elemental iron required to sodium ion removed), the [5 me 0 S n e or pa a on an recovery of valuable heavy metals or heavy metalacid balance (the amount of sulfuric acid produced bearin b roducts minus the amount required), the acid factor (the ratio Th g y P. t m t l r h d f of sulfuric acid required to elemental iron required), e preclp&#39; a e eavy e a 0 9 y foxy ernc sulfates of sulfites are removed via line 99 as an unand the Iron factor (the ratio of elemental ll&#39;Ol&#39;l required d erflow and filtered to remove excess entralned liquor to sodium sulfate disposed of). are each better for Sld- 2 100 b H trite than for Natrojarosite ln Natrojarosite the m separau. IS separator may 6 a screen t 3 wh as for Side} namte the factor is metal fabric or fibrous filter, a vacuum filter, or, prefercan or ls ere O ably. a centrifuge. The precipitate cake is rinsed in one (Ii Will] the lower the factor number the better the opor more stages by input of water 105 and the expressed eratron. Likewise. only two moles of mild are needed m water, wash water, or decantate is recycled to the reac- P f sdemnalme 9 tion tank 98 via line IOLThe moist or dried filtrate 110 moles required in the production of Natro aroslte. is disposed of as by conventional and fill Likewise the acid factor in Sideronatrite is L0 whereas To prevent buildmp of acidity or sodium ion Concem the factor fonNatrojaroslte IS 3 .0. The iron factor of ration. a Slipstream 111 may be passed thmugh Snip Natrojaroslte IS 6 whereas for Sideronatrite the factor able ion exchange resins l1 2 and the clarified water is only 1. Both the acid factor and iron factor (twice the returned m rinse ms or via line 31 to discharge basin can factor) 3&#39;? a f for how much f mater&#39;al m 8. Regenerant 113 is cycled through the resin in conterms of Sulfur&#34;! acid and Scrap are f q l F &#34;F ventional manner, and the spent regenerant back wash the sodium sulfate and thereby the msolubilrze it. The wastes 114 may be combimd in neutralizanon tank 13 lower these fac10r$- thefheaper&#39;me Prom?)s temls to P with wastes l2, l7, 18 or recycled directly, alone or depending f l l y of i and Sulfurlc F with wastes l9 and 29, to the reaction tank 98. This syssources offsfmmg this the dlfficulty tem polishes excess water in the insolubilization sysp S&#39;deronatme at more acid P but this tem. The resin may be a cation exchange resin alone or Can be amellolmed as mined y cPncemmtlon and P with an iron filter, in the hydrogen form for pick up of Control ssedmg during pmcessmgsodium. Mixed beds may be used for pH control to sub- The pyrite oxidatlon. or two stage pyrite degradat on. stantially ambient ground water neutral range values which occurs in the pyrites or pyrites-iron scrap dump H6 8 may be represented y equations 7, and 9 as fOllOWS! The solubility at room temperature of the end prod- Pyrite Oxidation: uct Sideronatrite is 0.16g/liter based on the iron analysis and 0.55 g/l based on sodium analysis. The solubility -2 4 7) fes+7l2oi+lilaol Fe +2H 5 of the end product Natro aroslte IS 002 g/l based on Pymc Degradauon&#39; the iron analysis and 0.37 g/l based on sodium. The iron 8) FeH+%O+H+ Fe+d+vlH2o anal sis is considered more reliable because of the dif- +8H o l5Fe* +SO +l6H y 9) FeSl&#39;MFe 2 4 ficulty of washing entrained sodium 10!) from the prelt should be understood that while the precipitates 5O cipitate. These compare favorably to the following remay be predominantly Natrojarosite or Sideronatrite. ported solubilities:  
 Table V Relative Solubilities Component Solubility 8r Conditions Anhydrous Nil- S0;  
  The following specific examples show insolubllization of blowdown magma and demineralizer system wastes respectively.  
 EXAMPLE I A solution having the composition of blowdown magma sludge 29 (FIG. 4) as set forth in Table IV is prepared by dissolving the following in 500 mIH O:  
 Table VI Component Amount (gramsl SiO 0.3 CaCl 0.55 MgC|-,.6H.,O 0.96 NaCl l5.5 Na SO, 84.3 CuCl: Ulll ZnCl Otll To 100 ml of this solution is added 50 ml of 0.125 molar Fe l S0,), The pH was 2.35 and required no adjustment with additional sulfuric acid. The solution was heated to l40F and maintained for about 25 hours (an additional &amp; hour was estimated as required for heat up). A red-brown precipitate formed which was washed twice with distilled water. The wash water was clear, indicating an insoluble precipitate. Upon analysis the precipitate contained Natrojarosite and Goethite, (FeOOH). as identified above.  
 EXAMPLE 2 EXAMPLE 3 As a second working example, the effluent from cation or anion exchangers, such as in lines 12 and 17 of FIG. 3, (see Table II) may be treated to produce Natrojarosite, Metasideronatrite, Sideronatrite or mixed precipitates under acidic conditions (pH 2.5) with addition of Fe,(SO,) and/or sulfuric acid ferric solution in the l20-l80F range as in Examples l or 2.  
  It should be understood that various modifications within the scope of this invention can be made by one of ordinary skill in the art without departing from the spirit thereof. We therefore wish our invention to be defined by the scope of the appended claims as broadly as the prior art will permit, and in view of this specification if need be.  
 We claim:  
  I. A water pollution control process for reducing the water solubility of sodium and ammonium sulfur oxide wastes comprising the steps of:  
 a. reacting a sulfur oxide anion selected from a sulfate, a sulfite and mixtures thereof, and a sodium or ammonium cation, with a source containing iron values selected from Fe&#34;, Fe&#34;, Fe and mixtures thereof,  
 b. said sulfur oxide anion being a waste produced in a process of demineralizing water,  
 5 c. maintaining said reaction at a pH below about 5.5 and at a temperature in the range of about 50-30()F for a time sufficient to form a compound sclected from:  
 where Q is NH, or Na, v is selected from I, 2, 4, or 5,  
 w is selected from 1, 2, 3, 4 or 6, .t&#39; is selected from 3 and/or 4, y is selected from 2, 4 or 5, z is selected from 1, 2, 3, 6 or 12, n is selected from 0 or 3, and mixtures thereof, and  
 d. said compound exhibiting solubility, measured with respect to ferric ion, of less than about 2.3 g/l at 0C.  
 20 2. A water pollution control process as in claim 1 wherein said water demineralization process is selected from demineralizing feed or waste waters used in, or produced by, industrial or power plant operations.  
 3. A water pollution control process as in claim 2 wherein the pH is maintained below about 3.5 and the temperature in the range of from about l20-200F.  
  4. A water pollution control process as in claim 3 wherein the pH is maintained below about 2.5.  
 5. A water pollution control process as in claim 1 wherein said iron source is an aqueous solution containing iron ions selected from ferrous ions, ferric ions,  
 and mixtures thereof.  
  6. A water pollution control process as in claim 5 wherein the pH is maintained below about 2.5.  
  7. A water pollution control process as in claim 3 wherein said water demineralization process is a process for demineralizing cooling tower water to produce a blowdown magma rich in sodium and sulfur oxide val- 4U ues.  
  8. A water pollution control process as in claim 3 wherein said water demineralization process waste is selected from wastes from processes for demineralizing raw water, make-up water, boiler feed water. condenser water. and coolant water.  
  9. A water pollution control process as in claim 1 wherein said iron-containing source iron is in an elemental or combined state.  
 10. A water pollution control process as in claim 9 which includes the step of oxidizing said iron to the ferrous state, ferric state or mixtures thereof.  
  11. A water pollution control process as in claim 10 wherein said oxidation takes place in the presence of acid tolerant. iron-oxidizing bacteria.  
  I2. A water pollution control process as in claim 2 wherein said reaction occurs in a plurality of zones.  
  13. A water pollution control process as in claim 12 wherein said iron source includes iron in an elemental, ferrous or combined state, or mixtures thereof, which iron is oxidized to the ferrous state, ferric state or mixtures thereof in a zone separate from a zone wherein said compound is formed.  
  14. A water pollution control process as in claim 13 wherein said sulfur oxide anion, sodium cation, ammonium cation, or mixtures thereof, are added to a first heated zone separately from a second zone in which ferric ion is prepared biotically or abiotically.  
  15. A water pollution control process as in claim 14 wherein said second zone includes biotic preparation of ferric ion and sulfuric acid.  
  16. A water pollution control process as in claim 15 wherein said second zone includes at least two stages. each being maintained at a different pH for biotic oxidation of Fe to Fe in a first stage thereof. and Fe to Fe in a second stage.  
  17. A water pollution control process as in claim 1 wherein maintaining said reaction includes the steps of:  
 a. commencing said reaction at a pH below a pH conducive to the formation of ferrous or ferric hydroxides to form at least some of said compound,  
 I). adjusting the pH upward to within at least the lower end of the range of pH at which production of one or more of said hydroxides could occur, while reducing the ferric ion concentration, and  
 c. selectively forming said compound in the absence of substantial production of said hydroxides.  
 18. A water pollution control process as in claim 17 which includes the step of seeding said reaction with crystals of said compound prior to raising said pH.  
  19. A water pollution control process as in claim 18 wherein the pH is maintained below about 5.5 and the temperature in the range of from about l20-l F.  
  20. A water pollution control process as in claim 2 wherein said iron is an aqueous solution of ferrous ion, ferric ion, and mixtures thereof and said acid is sulfuric acid.  
  21. A water pollution control process as in claim 20 wherein said iron and sulfuric acid sources are selected from waste acid, steel pickle liquor, scrap iron, ironbearing slag, pyrites, acid mine water, black water. gob, pyrites leachate, fly ash, S0 and sO -containing flue gas, and mixtures thereof.  
  22. A water pollution control process as in claim 2l wherein said reaction takes place in an aqueous medium, and said S0 and SO -containing flue gas is sparged in said aqueous reaction medium to provide both heat and said acid values.