PATENT DOCUMENT

Abstract:
System and method of treating waste water includes: receiving waste water at a first pressure and a first temperature, the waste water comprising dissolved solids and VOCs; pressurizing the waste water to a second pressure; preheating the pressurized waste water to a second temperature to produce distilled water and pressurized/preheated water; heating the pressurized/preheated to a third temperature to produce pressurized/heated water; removing dissolved solids from the pressurized/heated water, by an evaporator operated at a third pressure less than the second pressure, to produce steam and brine water; and crystallizing the brine water, by a crystallizer operated at a fourth pressure greater than the second pressure, to produce a solid mass waste product and steam. Steam produced by the crystallizer, at the fourth pressure and a fourth temperature, is a heat source for the preheater and/or heater, and steam produced by the evaporator is a heat source for the crystallizer.

Full Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
       [0001]    This patent application claims the benefit of U.S. Provisional Patent Application Nos. 61/573,900, 61/573,957, 61/573,958, 61/573,956, 61/573,955, 61/573,954, 61/573,953 and 61/573,952, all filed on Sep. 14, 2011, the disclosures of which are hereby incorporated by reference in their entireties. 
     
    
     FIELD OF THE INVENTION 
       [0002]    The present invention is generally directed toward the treatment of water and, more particularly, toward the treatment of water containing large amounts of dissolved solids as may result, for example, from use of the water as a fracking fluid used in drilling gas wells. However, the embodiment proposed herein may be used in any situation where impurities to be removed from water exist. 
       BACKGROUND OF THE INVENTION 
       [0003]    Ensuring a supply of potable water has been a frequent concern in many locations. Further concerns arise about the environmental impact of the disposal of contaminated water. 
         [0004]    Conventional water treatment techniques for such purposes as, for example, municipal water treatment and/or obtaining potable water from sea water are known and are successful in many instances. However, some current activities show those techniques to have limited cost effectiveness. 
         [0005]    For example, mining with water used to fracture rock or shale formations to recover natural gas (e.g., in the shale regions in the United States and western Canada including, but not limited to, Pennsylvania, Maryland, New York, Texas, Oklahoma, West Virginia and Ohio) requires a very large amount of water input and a significant amount of return (flowback) water that contains a great deal of contaminants and impurities. In order for this flowback water to be used in an environmentally responsible manner, it needs to be relatively free of contaminants/impurities. Water used, for example, in natural gas well drilling and production may contain organic materials, volatile and semi-volatile compounds, oils, metals, salts, etc. that have made economical treatment of the water to make it potable or reusable, or even readily and safely disposable, more difficult. It is desirable to remove or reduce the amount of such contaminants/impurities in the water to be re-used, and also to remove or reduce the amount of such contaminants/impurities in water that is disposed of. 
         [0006]    The present invention is directed toward overcoming one or more of the above-identified problems. 
       SUMMARY OF THE INVENTION 
       [0007]    The present invention can take numerous forms among which are those in which waste water containing a large amount of solids, including, for example, dissolved salts, is pressurized to allow considerable heat to be applied before the water evaporates, and is then subjected to separation and recovery apparatus to recover relatively clean water for reuse and to separate solids that include the afore-mentioned dissolved salts. In some instances, the concentrated solids may be disposed of as is, e.g., in a landfill. Where that is not acceptable (e.g., for reasons of leaching of contaminants), the concentrated solids may be supplied to a thermal, pyrolytic, reactor (referred to herein as a “crystallizer”) for transforming them into a vitrified mass which can be placed anywhere glass is acceptable. 
         [0008]    Particular apparatus for systems and processes in accordance with the present invention can be adapted from apparatus that may be presently currently available, but which has not been previously applied in the same manner. As an example, conventional forms of flash evaporation equipment, such as are used for treating sea water, in one or in multiple stages, may be applied herein as a salts concentration apparatus. Likewise, conventional forms of gasification/vitrification reactors, such as are used for municipal solid waste (“MSW”) processing including, but not limited, to plasma gasification/vitrification reactors, may be applied for final separation of the contaminants from the water and for initial heating of the waste water. 
         [0009]    The present disclosure presents examples of such systems and processes in which, in one or more successive concentration stages, steam output of a flash evaporator used to concentrate salts is raised in pressure by mechanical vapor compressors from a low level (e.g., 5 psia) to a substantially higher level (e.g., 150 psia), accompanied by elevation of the steam temperature. The steam is applied to heat incoming waste water for treatment and permits use of a smaller and less expensive heat exchanger than would be needed without such pressurization. 
         [0010]    Additionally, in some examples, steam from one or more stages of salts concentration is pressurized (e.g., from 5 psia up to 150 psia) before applying the steam to a stripper to remove, for example, volatile organic compounds (“VOCs”), and making the water available for reuse in a prior or subsequent stage and the VOCs available for reaction in a pyrolytic (e.g., plasma) reactor or crystallizer. 
         [0011]    In addition, examples can include use of a turbine to expand steam (e.g., having an input of steam exiting a reactor or crystallizer at 150 psia and an output of steam at 15 psia) which goes then to a VOC stripper for use as described above. A turbine, or the like, for steam pressure reduction generates power or mechanical energy that reduces overall energy consumption. 
         [0012]    Such uses of compressors and turbines, while adding some additional initial costs, can save significant operating costs. 
         [0013]    The present disclosure, among other things, also presents examples of such systems and processes in which, in one or more successive concentration stages, steam output from a flash evaporator used to concentrate salts is reduced in pressure from, for example, 150 psia input pressure to 25 psia output pressure, and the output steam is then sent to the stripper. The steam from the crystallizer (e.g., at 180 psia) is sent back to heat the pressurized waste water in each stage. A portion of the steam from the crystallizer is sent to the stripper after expanding in a turbine (e.g., a mechanical vapor turbine). A turbine is used to expand this steam before sending it to a stripper of volatile organic compounds (“VOCs”). 
         [0014]    The system and process of the present invention also includes, for example, applying saturated steam from the crystallizer to a condenser prior to flash evaporation of waste water and, therefore, a heater stage can be avoided. A preheater is used to heat incoming waste water (e.g., from 60° F. to 134° F.) by use of the condensate from the condenser. 
         [0015]    The present disclosure, among other things, further presents examples of such systems and processes in which, in one or more successive concentration stages, steam output of a flash evaporator used to concentrate salts is reduced in pressure from, for example, 150 psia input to 5 psia downstream. The output steam is then repressurized to, e.g., 180 psia, prior to being applied to a crystallizer. 
         [0016]    The system and process of the present invention further includes, for example, that saturated steam from the reactor/crystallizer is applied to a condenser prior to flash evaporation of waste water and, therefore, an extra heater stage can be avoided. A preheater, provided before the condenser, is used to heat incoming waste water (e.g., from 60° F. to 134° F.) by use of the condensate from the condenser. 
         [0017]    The present disclosure, among other things, further presents examples of such systems and processes in which, in one or more successive concentration stages, waste water with dissolved solids (salts) is pressurized (e.g., from 15 psia to 400 psia) and heated (e.g., to 445° F.) before flash evaporation to a significantly lower flash pressure and temperature (e.g., 15 psia and 212° F.) and brine water with more concentrated salts. 
         [0018]    Steam output from the concentration stages is, at least in part, supplied to a stripper to remove volatile organic compounds (“VOCs”). Additional steam from the concentration stages is pressurized (e.g., to 665 psia) prior to recycling back to the concentration stages as a heating fluid for incoming waste water. 
         [0019]    Brine water from the concentration stages may be disposed of as is, with a significant amount of clean water recovered (e.g., as distilled water from heat exchangers of the concentration stages). Brine water may alternatively be treated in a thermal (e.g., plasma) reactor or crystallizer in order to separate the salts and recover water included in the brine water from the concentration stages. 
         [0020]    Present examples described herein include operation of a crystallizer at a significantly higher pressure (e.g., 665 psia) than in many other thermal reactor systems in order to achieve a large temperature difference in heat exchangers of the concentration stages. 
         [0021]    Examples described herein also include supplying saturated steam from the crystallizer directly to condensers of the concentration stages, from each of which it is then applied as a heating fluid of a preheater for the waste water. Such a system will not normally require any additional heating of the waste water prior to flash evaporation. 
         [0022]    The present disclosure, among other things, presents examples of such systems and processes in which, in one or more concentration stages, waste water with dissolved solids (salts) is pressurized (e.g., to 400 psia) and heated (e.g., to 445° F.) before flash evaporation in a single flash evaporator to which multiple concentration stages supply waste water in parallel. For example, the waste water is split into three equal flows that are individually pressurized and heated prior to being subjected to flash evaporation together. 
         [0023]    The flash evaporator produces steam that is then usable as a heating medium and brine water with more concentrated salts than the original waste water. 
         [0024]    The resulting combined brine water from the concentration stages may be disposed of as is, with a significant amount of clean water recovered (e.g., as distilled water from heat exchangers of the concentration stages). Brine water may alternatively be treated in a pyrolytic (e.g., plasma) reactor or crystallizer in order to separate the salts and recover water included in the brine water from the concentration stages. 
         [0025]    Where a crystallizer is used, it can provide superheated steam (developed from steam from the single, or plural, flash evaporator(s)) that is applied directly to condensers of the concentration stages, from each of which it is then applied as a heating fluid of a preheater for the waste water. Such a system will not normally require additional heating of the waste water prior to flash evaporation. 
         [0026]    While the another embodiment of the present invention is described with respect to  FIGS. 17-20  as including stages operating in parallel, it should be understand that any of the stages of the other embodiments may also be operated in parallel without departing from the spirit and scope of the present invention. Additionally, the embodiment of  FIGS. 17-20  may also be operated in series. 
         [0027]    A system for treating waste water is disclosed, the system including: a pump receiving waste water at a first pressure and a first temperature and pressurizing the received waste water to a second pressure greater than the first pressure, the waste water comprising dissolved solids, volatile organic compounds and other components generally and collectively called impurities; first and second preheaters receiving the pressurized waste water from the pump and preheating the pressurized waste water in successive stages to a second temperature greater than the first temperature to produce pressurized/preheated waste water, each of the first and second preheaters producing distilled water without boiling of the waste water across heat transfer surfaces; a condenser receiving the pressurized/preheated waste water and further heating the pressurized/preheated waste water to a third temperature greater than the second temperature to produce a pressurized/further heated waste water without boiling of the waste water across heat transfer surfaces; a heater receiving the pressurized/further heated waste water and still further heating the pressurized/further heated waste water to a fourth temperature greater than the third temperature to produce pressurized/heated waste water without boiling of the waste water across heat transfer surfaces; and an evaporator, operated at a third pressure less than the second pressure, removing dissolved solids from the pressurized/heated waste water by evaporation caused by depressurization of the waste water to produce steam and brine water, wherein the brine water has a total dissolved solids content greater than a total dissolved solids content of the received waste water, wherein steam from the evaporator is superheated to a fifth temperature greater than the fourth temperature and is used as a heat source by at least one of the heater, condenser and second preheater without boiling of the waste water across heat transfer surfaces. 
         [0028]    The second pressure may be approximately 120-180 psia, and the third pressure may be approximately 4-6 psia. 
         [0029]    The fourth temperature may be approximately 286−430° F., and the firth temperature may be approximately 400−600° F. 
         [0030]    In one form, the pump, first and second preheaters, condenser, heater and evaporator comprise a stage, and wherein the system comprises multiple stages with the brine water output by one stage used as the received waste water of a next stage. The brine water output by each stage has a total dissolved solids content that is higher than that of a previous stage. 
         [0031]    In another form, the system further includes a crystallizer crystallizing the brine water to produce a solid mass of waste product and steam, which may be a vitrified glass. The steam from the crystallizer may be mixed with steam from the evaporator and superheated to the fifth temperature, wherein the mixed and superheated steam may be used as a heat source by at least one of the heater, condenser and second preheater without boiling of the waste water across heat transfer surfaces. 
         [0032]    In a further form, the crystallizer includes a plasma crystallizer and includes a plasma torch for vaporizing the water from the brine water and producing the solid mass of waste product and steam. The system further includes a stripper initially receiving the waste water and removing volatile organic compounds from the waste water prior to the waste water being pressurized by the pump, wherein the removed volatile organic compounds are used as a heat source by the plasma torch to crystallize the brine water. The steam produced by the evaporator, when cooled, produces distilled water. Additionally, the steam produced by the evaporator may be used as a heat source by the stripper without boiling of the waste water across heat transfer surfaces. The steam produced by the evaporator may also be used as a heat source by the first preheater without boiling of the waste water across heat transfer surfaces. 
         [0033]    In yet a further form, the pump, first and second preheaters, condenser, heater and evaporator comprise a stage, and wherein the system comprises multiple stages operating in parallel with each receiving a portion of the waste water. The brine water output by each stage has a total dissolved solids content that is higher than that of the received waste water. The brine water from each stage is combined and supplied to the crystallizer which crystallizes the brine water to produce a solid mass of waste product and steam. 
         [0034]    In still a further form, the pump, first and second preheaters, condenser, heater and evaporator comprise a stage, wherein the system comprises multiple stages with the brine water output by one stage used as the received waste water of a next stage, and wherein the received waste water at stages subsequent to a first stage is at a third pressure less than the first pressure. 
         [0035]    A system for treating waste water is also disclosed, the system including: a pump receiving waste water at a first pressure and a first temperature and pressurizing the received waste water to a second pressure greater than the first pressure, the waste water comprising dissolved solids, volatile organic compounds and other components generally and collectively called impurities; a preheater receiving the pressurized waste water from the pump and preheating the pressurized waste water to a second temperature greater than the first temperature to produce pressurized/preheated waste water without boiling of the waste water across heat transfer surfaces; a condenser receiving the pressurized/preheated waste water and further heating the pressurized/preheated waste water to a third temperature greater than the second temperature to produce a pressurized/heated waste water without boiling of the waste water across heat transfer surfaces; an evaporator, operated at a third pressure less than the second pressure, removing dissolved solids from the pressurized/heated waste water by evaporation caused by depressurization of the waste water to produce steam and brine water, wherein the brine water has a total dissolved solids content greater than a total dissolved solids content of the received waste water; and a crystallizer, operated at a fourth pressure greater than the second pressure, receiving the brine water and crystallizing the brine water to produce a solid mass of waste product and steam, wherein steam from the crystallizer, at the fourth pressure and a fourth temperature greater than the third temperature, is used as a heat source by at least one of the condenser and preheater without boiling of the waste water across heat transfer surfaces, and wherein steam from the evaporator is used as a heat source by the crystallizer without boiling of the waste water across heat transfer surfaces. 
         [0036]    In one form, the first pressure may be approximately 11.8-17.6 psia, and the first temperature may be approximately 480-72° F. 
         [0037]    In one form, the second pressure may be approximately 120-180 psia, and the third temperature may be approximately 288-432° F. 
         [0038]    In one form, the second pressure may be approximately 320-480 psia, and the third temperature may be approximately 356-534° F. 
         [0039]    In one form, the third pressure may be approximately 20-30 psia, the fourth pressure may be approximately 144-216 psia, and the fourth temperature may be approximately 298-448° F. 
         [0040]    In one form, the third pressure may be approximately 4-6 psia, the fourth pressure may be approximately 144-216 psia, and the fourth temperature may be approximately 298-448° F. 
         [0041]    In one form, the third pressure may be approximately 12-18 psia, the fourth pressure may be approximately 532-798 psia, and the fourth temperature may be approximately 400-600° F. 
         [0042]    In another form, the crystallizer includes a plasma crystallizer and includes a plasma torch for vaporizing the water from the brine water and producing the solid mass of waste product and steam. The system further includes a stripper initially receiving the waste water and removing volatile organic compounds from the waste water prior to the waste water being pressurized by the pump, wherein the removed volatile organic compounds are used as a heat source by the plasma torch to crystallize the brine water without boiling of the waste water across heat transfer surfaces. 
         [0043]    In a further form, the system further included a mechanical vapor turbine receiving the steam from the crystallizer and reducing its pressure to the third pressure, wherein the reduced pressure steam is combined with the steam from the evaporator and used as a heat source by the stripper. 
         [0044]    In yet a further form, the system further includes a mechanical vapor compressor receiving the steam from the evaporator and increasing its pressure to the fourth pressure, wherein the increased pressure steam is combined with the steam from the crystallizer and used as a heat source by at least one of the condenser and preheater without boiling of the waste water across heat transfer surfaces. 
         [0045]    In still a further form, the pump, preheater, condenser and evaporator comprise a stage, and wherein the system comprises multiple stages with the brine water output by one stage used as the received waste water of a next stage, and wherein the brine water output by a last stage is input to the crystallizer. The brine water output by each stage has a total dissolved solids content that is higher than that of a previous stage. 
         [0046]    In an additional form, the pump, preheater, condenser and evaporator comprise a stage, and wherein the system comprises multiple stages operating in parallel with each stage receiving a portion of the waste water, and wherein the brine water from each stage is combined and supplied to the crystallizer. The brine water output by each stage has a total dissolved solids content that is higher than that of the received waste water. 
         [0047]    In yet and additional form, the pump, preheater, condenser and evaporator comprise a stage, wherein the system comprises multiple stages with the brine water output by one stage used as the received waste water of a next stage, and wherein the received waste water at stages subsequent to a first stage is at the third pressure. 
         [0048]    A method of treating waste water is also disclosed, the method including the steps of: (a) receiving waste water at a first pressure and a first temperature, the waste water comprising dissolved solids, volatile organic compounds and other components generally and collectively called impurities; (b) pressurizing the received waste water to a second pressure greater than the first pressure; (c) preheating the pressurized waste water to a second temperature greater than the first temperature, wherein said preheating step is performed by first and second preheaters in successive stages to produce pressurized/preheated waste water, each of the first and second preheaters producing distilled water without boiling of the waste water across heat transfer surfaces; (d) heating the pressurized/preheated waste water to a third temperature greater than the second temperature to produce a pressurized/heated waste water without boiling of the waste water across heat transfer surfaces; (e) further heating the pressurized/heated waste water to a fourth temperature greater than the third temperature to produce pressurized/further heated waste water without boiling of the waste water across heat transfer surfaces; and (f) removing, by evaporation caused by depressurization of the waste water, dissolved solids from the pressurized/further heated waste water by an evaporator operated at a third pressure less than the second pressure to produce steam and brine water, wherein the brine water has a total dissolved solids content greater than a total dissolved solids content of the received waste water, wherein steam from the evaporator is superheated to a fifth temperature greater than the fourth temperature and is used as a heat source in at least one of steps (c)—by the second preheater, (d) and (e) without boiling of the waste water across heat transfer surfaces. 
         [0049]    The second pressure may be approximately 120-180 psia, and the third pressure may be approximately 4-6 psia. 
         [0050]    The fourth temperature may be approximately 286-430° F., and the firth temperature may be approximately 400-600° F. 
         [0051]    In one form, steps (a)-(f) comprise a stage, and wherein the method is performed in multiple stages with the brine water output by step (f) in one stage used as the received waste water in step (a) of a next stage. The brine water output in step (f) of each stage has a total dissolved solids content that is higher than that of a previous stage. 
         [0052]    In another form, the method further includes the steps of: (g) crystallizing the brine water to produce a solid mass of waste product and steam. The steam produced by step (g) is mixed with steam produced by step (f) and superheated to the fifth temperature, wherein the mixed and superheated steam may be used as a heat source in at least one of steps (c)—by the second preheater, (d) and (e) without boiling of the waste water across heat transfer surfaces. A plasma crystallizer using a plasma torch may be used to crystallize the brine water. The solid mass may include a vitrified glass of the salts in the brine water. 
         [0053]    In a further form, the method further includes the steps of: (b′) prior to step (b), removing the volatile organic compounds from the received waste water, wherein the removed volatile organic compounds are used as a heat source by the plasma torch to crystallize the brine water. The steam produced by step (f) may be used as a heat source in step (b′). The steam produced by step (f) may be used as a heat source in step (c)—by the first preheater. 
         [0054]    In yet a further form, steps (a)-(f) comprise a stage, and wherein the method is performed in multiple stages operating in parallel with each stage receiving a portion of the waste water. The brine water output in step (f) of each stage has a total dissolved solids content that is higher than that of the received waste water. The brine water output in step (f) of each stage is combined and supplied to a crystallizer which crystallizes the combined brine water to produce a solid mass of waste product and steam. 
         [0055]    In still a further form, steps (a)-(f) comprise a stage, and wherein the method is performed in multiple stages with the brine water output by step (f) in one stage used as the received waste water in step (a) of a next stage, and wherein the received waste water at step (a) in stages subsequent to a first stage is at a third pressure less than the first pressure. 
         [0056]    A method of treating waste water is also disclosed, the method including the steps of: (a) receiving waste water at a first pressure and a first temperature, the waste water comprising dissolved solids, volatile organic compounds and other components generally and collectively called impurities; (b) pressurizing the received waste water to a second pressure greater than the first pressure; (c) preheating the pressurized waste water to a second temperature greater than the first temperature to produce distilled water and pressurized/preheated waste water without boiling of the waste water across heat transfer surfaces; (d) heating the pressurized/preheated to a third temperature greater than the second temperature to produce pressurized/heated waste water without boiling of the waste water across heat transfer surfaces; (e) removing, by evaporation caused by depressurization of the waste water, dissolved solids from the pressurized/heated water, by an evaporator operated at a third pressure less than the second pressure, to produce steam and brine water, wherein the brine water has a total dissolved solids content greater than a total dissolved solids content of the received waste water; and (f) crystallizing the brine water, by a crystallizer operated at a fourth pressure greater than the second pressure, to produce a solid mass of waste product and steam, wherein steam produced by step (f), at the fourth pressure and a fourth temperature greater than the third temperature, is used as a heat source in at least one of steps (c) and (d), and wherein steam produced by step (e) is used as a heat source in step (g). 
         [0057]    In one form, the first pressure may be approximately 11.8-17.6 psia, and the first temperature may be approximately 480-72° F. 
         [0058]    In one form, the second pressure may be approximately 120-180 psia, and the third temperature may be approximately 288-432° F. 
         [0059]    In one form, the second pressure may be approximately 320-480 psia, and the third temperature may be approximately 356-534° F. 
         [0060]    In one form, the third pressure may be approximately 20-30 psia, the fourth pressure may be approximately 144-216 psia, and the fourth temperature may be approximately 298-448° F. 
         [0061]    In one form, the third pressure may be approximately 4-6 psia, the fourth pressure may be approximately 144-216 psia, and the fourth temperature may be approximately 298-448° F. 
         [0062]    In one form, the third pressure may be approximately 12-18 psia, the fourth pressure may be approximately 532-798 psia, and the fourth temperature may be approximately 400-600° F. 
         [0063]    In another form, step (f) uses a plasma torch to crystallize the brine water, and wherein the method further includes the steps of: (b′) prior to step (b), removing the volatile organic compounds from the received waste water, wherein the removed volatile organic compounds are used as a heat source by the plasma torch to crystallize the brine water. 
         [0064]    In a further form, the steam produced by step (f) is reduced in pressure to the third pressure, and wherein the reduced pressure steam is combined with steam produced in step (e) and used as a heat source in step (b′). 
         [0065]    In yet a further form, the steam produced in step (e) in increased in pressure to the fourth pressure, and wherein the increased pressure steam is combined with steam produced in step (f) and used as a heat source in at least one of steps (c) and (d). 
         [0066]    In still a further form, steps (a)-(e) comprise a stage, and wherein the method is performed in multiple stages with the brine water output by step (e) in one stage used as the received waste water in step (a) of a next stage, and wherein the brine water output by step (e) in a last stage is input to the crystallizer at step (f). The brine water output by step (e) of each stage has a total dissolved solids content that is higher than that of a previous stage. 
         [0067]    In yet another form, steps (a)-(e) comprise a stage, and wherein the method is performed in multiple stages operating in parallel with each stage receiving a portion of the waste water, and wherein the brine water output by step (e) in each stage is combined and supplied to the crystallizer at step (f). The brine water output by step (e) of each stage has a total dissolved solids content that is higher than that of the waste water received at that particular stage. 
         [0068]    In still another form, steps (a)-(e) comprise a stage, and wherein the method is performed in multiple stages operating in parallel with each stage receiving a portion of the waste water, wherein the brine water output by step (e) in each stage is combined and supplied to the crystallizer at step (f), and wherein the received waste water at stages subsequent to a first stage is at the third pressure. 
         [0069]    Further explanations and examples of various aspects of the present invention are presented in the following disclosure. 
         [0070]    It is an object of the present invention to provide a system and method for the economic and environmental treatment of waste water. 
         [0071]    Various other objects, aspects and advantages of the present invention can be obtained from a study of the specification, the drawings, and the appended claims. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0072]    Further possible embodiments are shown in the drawings. The present invention is explained in the following in greater detail as an example, with reference to exemplary embodiments depicted in drawings. In the drawings: 
           [0073]      FIGS. 1, 2 and 3  are schematic flow diagrams of particular examples of stages of a treatment system in accordance with the present invention; 
           [0074]      FIG. 4  is a schematic flow diagram of an exemplary thermal reactor for use in a water treatment system in conjunction with elements such as those shown in  FIGS. 1-3  in accordance with the present invention; 
           [0075]      FIGS. 5, 6 and 7  are schematic flow diagrams of stages of a treatment system in accordance with a further embodiment of the present invention; 
           [0076]      FIG. 8  is a schematic flow diagram of an exemplary thermal reactor configured for use with water treatment stages such as those shown in  FIGS. 5-7  in accordance with the further embodiment of the present invention; 
           [0077]      FIGS. 9, 10 and 11  are schematic flow diagrams of particular examples of stages of a treatment system in accordance with yet a further embodiment of the present invention; 
           [0078]      FIG. 12  is a schematic flow diagram of an exemplary thermal reactor configured for use in a water treatment system in conjunction with treatment stages and elements such as those shown in  FIGS. 9-11  in accordance with yet a further embodiment of the present invention; 
           [0079]      FIGS. 13, 14 and 15  are schematic flow diagrams of particular examples of stages of a treatment system in accordance with still a further embodiment of the present invention; and 
           [0080]      FIG. 16  is a schematic flow diagram of an exemplary thermal reactor configured for use in a water treatment system in conjunction with treatment stages and elements such as those shown in  FIGS. 13-15  in accordance with still a further embodiment of the present invention; 
           [0081]      FIGS. 17, 18 and 19  are schematic flow diagrams of particular examples of stages of a treatment system in accordance with another embodiment of the present invention; and 
           [0082]      FIG. 20  is a schematic flow diagram of an exemplary thermal reactor configured for use in a water treatment system in conjunction with treatment stages and elements such as those shown in  FIGS. 17-19  in accordance with another embodiment of the present invention. 
       
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
       [0083]      FIGS. 1, 2 and 3  will be individually discussed, but first their general relation to each other in an exemplary multi-stage system will be described.  FIG. 1  shows Stage #1. This first stage takes in waste water at an inlet  20 , processes it and produces first stage brine water at an outlet  30  of the first stage. The first stage brine water from the outlet  30  is input to the second stage shown in  FIG. 2  (Stage #2) for additional processing, and a resulting second stage brine water is produced as an output at outlet  50 . Similarly, the brine water from outlet  50  of the second stage is supplied as an input to the third stage shown in  FIG. 3  (Stage #3) that has additional processing, resulting in a third stage output of brine water at an outlet  70 . 
         [0084]    It will be seen and appreciated by one skilled in the art how the successive stages of  FIGS. 1, 2 and 3  increase the concentration of salts in the brine water (e.g., Total Dissolved Solids—“TDS”). It will also be appreciated how the number of stages is a variable that can be chosen according to various factors including, but not limited to, the salts content of the original waste water and the desired salt content after concentration. In general, a system in accordance with these exemplary embodiments may include any one or more stages such as are shown, for example, in  FIGS. 1-3 . The examples presented herein are merely illustrative of systems and methods that may be chosen not merely for good technical performance but also for reasons relating to economic factors, such as, for example, initial capital cost and operating cost, as well as convenience factors, such as, for example, space requirements and portability. While three stages are shown and described herein, one skilled in the art will appreciate that any number of stages may be utilized depending on the particular application without departing from the spirit and scope of the present invention. 
         [0085]    Each of the  FIGS. 1-4 , merely by way of further example and without limitation, are described in this specification, and include legends, including numerical values (all of which are merely representative approximations and are not necessarily exact technical values and/or calculations). Further, these legends are not necessarily the only suitable values that represent the nature and characteristics of materials as applied to, affected by, and resulting from the operations of the exemplary system(s). Not all such legends will be repeated in this text, although all form a part of this disclosure and are believed understandable to persons of ordinary skill in water treatment and thermal processes. As appreciated by one skilled in the art, such data are sometimes referred to as heat and material balances. It is specifically to be understood and will be appreciated by one skilled in the art that the various values indicated in the legends may have a tolerance of ±20%, as they are representative approximations and not exact technical values. 
         [0086]    Referring to  FIG. 1 , which shows Stage #1, the waste water progresses from the input  20  to the output  30  successively through a pump  11 , preheaters  12   a  and  12 , a condenser  13 , an additional heater  14 , and a flash evaporator  15 . In the preheater  12   a , the heating medium is the excess steam available from a crystallizer  90  (see  FIG. 4 ), while for the preheater  12 , the heating medium is the hot water available from the condenser  13 . 
         [0087]    The pump  11  elevates the waste water pressure from approximately 14.7 psia (1 atm) to approximately 150 psia. The level of pressurization of waste water in all stages is such that there is no boiling of the waste water inside and across the heat exchanger surfaces of all heat exchangers used in this system. This is done to prevent formation of deposits (scales, fouling etc.) on the heat exchanger surfaces. The temperature is also raised by the successive preheaters  12   a  and  12 , the condenser  13  and the heater  14 , so the input waste water to the flash evaporator  15  at inlet  15   a  is at 150 psia and 358° F. 
         [0088]    The elevation in temperature is the effect of steam from one steam output  80  of the crystallizer subsystem  90  of  FIG. 4 . That steam is mixed in a mixer  16  of  FIG. 1  with part of the steam from the flash evaporator  15  at line  15   b  that goes through a compressor  17  before it reaches the mixer  16  at input  16   a . Some of the steam from the evaporator  15  at line  15   b  is also fed to the stripper  130  (see  FIG. 4 ). The output  16   b  of the mixer  16  is a superheated steam at approximately 500° F. and 150 psia which, following its use as a heating fluid in the heater  14 , continues to the condenser  13  and the preheater  12  until it exits the preheater  12  at outlet  12   b  as distilled water. Additionally, as shown in  FIG. 1 , the output of preheater  12   a  at outlet  12   c  is also distilled water. Under certain operating conditions, the steam addition from the crystallizer  90  may be negative, i.e., steam is sent as excess to the crystallizer  90  for other uses (e.g., as a heat source for the stripper  130 ). 
         [0089]    The Stage #1 output  30  has the volume of waste water reduced from the input  10  with the salts more concentrated to 25% TDS, which is increased from the initial approximately 20% TDS in the exemplary waste water at the input  20 . 
         [0090]    Stage #2 of the system as shown in  FIG. 2  has elements substantially like those of Stage #1 in  FIG. 1 , but with some different operating parameters as shown in the legends in  FIG. 2 . Referring to  FIG. 2 , which shows Stage #2, the waste water progresses from the input  30  to the output  50  successively through a pump  31 , preheaters  32   a  and  32 , a condenser  33 , an additional heater  34 , and a flash evaporator  35 . In the preheater  32   a , the heating medium is the excess steam available from a crystallizer  90  (see  FIG. 4 ), while for the preheater  32 , the heating medium is the hot water available from the condenser  33 . 
         [0091]    The pump  31  elevates the waste water pressure from approximately 5 psia at its input to approximately 150 psia. The temperature is also raised by the successive preheaters  32   a  and  32 , the condenser  33  and the heater  34 , so the input waste water to the flash evaporator  35  at inlet  35   a  is at 150 psia and 358° F. 
         [0092]    The elevation in temperature is the effect of steam from one steam output  80  of the crystallizer subsystem  90  of  FIG. 4 . That steam is mixed in a mixer  36  of  FIG. 2  with part of the steam from the flash evaporator  35  at line  35   b  that goes through a compressor  37  before it reaches the mixer  36  at input  36   a . Some of the steam from the evaporator  35  at line  35   b  is also fed to the stripper  130  (see  FIG. 4 ). The output  36   b  of the mixer  36  is a superheated steam at approximately 500° F. and 150 psia which, following its use as a heating fluid in the heater  34 , continues to the condenser  33  and the preheater  32  until it exits the preheater  32  at outlet  32   b  as distilled water. Additionally, as shown in  FIG. 2 , the output of preheater  32   a  at outlet  32   c  is also distilled water. Under certain operating conditions, the steam addition from the crystallizer  90  may be negative, i.e., steam is sent as excess to the crystallizer  90  for other uses (e.g., as a heat source for the stripper  130 ). 
         [0093]    The Stage #2 output  50  has the volume of waste water reduced from the input  30  with the salts more concentrated to 31% TDS, which is increased from the initial approximately 25% TDS in the exemplary brine water at the input  30 . 
         [0094]    Similarly, Stage #3 of  FIG. 3  has elements substantially like those of  FIG. 2 , but with still some differences in operating parameters as shown in the legends in  FIG. 3 . Referring to  FIG. 3 , which shows Stage #3, the waste water progresses from the input  50  to the output  70  successively through a pump  51 , preheaters  52   a  and  52 , a condenser  53 , an additional heater  54 , and a flash evaporator  55 . In the preheater  52   a , the heating medium is the excess steam available from a crystallizer  90  (see  FIG. 4 ), while for the preheater  52 , the heating medium is the hot water available from the condenser  53 . 
         [0095]    The pump  51  elevates the waste water pressure from approximately 5 psia at its input to approximately 150 psia. The temperature is also raised by the successive preheaters  52   a  and  52 , the condenser  53  and the heater  54 , so the input waste water to the flash evaporator  55  at inlet  55   a  is at 150 psia and 358° F. 
         [0096]    The elevation in temperature is the effect of steam from one steam output  80  of the crystallizer subsystem  90  of  FIG. 4 . That steam is mixed in a mixer  56  of  FIG. 3  with part of the steam from the flash evaporator  55  at line  55   b  that goes through a compressor  57  before it reaches the mixer  56  at input  56   a . Some of the steam from the evaporator  55  at line  55   b  is also fed to the stripper  130  (see  FIG. 4 ). The output  56   b  of the mixer  56  is a superheated steam at approximately 500° F. and 150 psia which, following its use as a heating fluid in the heater  54 , continues to the condenser  53  and the preheater  52  until it exits the preheater  52  at outlet  52   b  as distilled water. Additionally, as shown in  FIG. 2 , the output of preheater  52   a  at outlet  52   c  is also distilled water. Under certain operating conditions, the steam addition from the crystallizer  90  may be negative, i.e., steam is sent as excess to the crystallizer  90  for other uses (e.g., as a heat source for the stripper  130 ). 
         [0097]    The Stage #3 output  70  has the volume of waste water reduced from the input  50  with the salts more concentrated to 39% TDS, which is increased from the initial approximately 31% TDS in the exemplary brine water at the input  50 . 
         [0098]    The exemplary system includes multiple (three) concentration stages ( FIGS. 1-3 ) that are substantially alike in the combination of equipment used. However, other exemplary systems with multiple concentration stages may have individual stages of more viewed combinations of equipment without departing from the spirit and scope of the present invention. 
         [0099]    The level of pressurization of waste water in all stages is such that there is no boiling (nucleate or other type) of the waste water inside and across the heat exchanger surfaces of the condensers, heaters and preheaters of each stage. This prevents the formation of deposits (scales, fouling etc.) on the heat exchanger surfaces and reduces the requirement for cleaning of the heat exchangers. This results in the reduction of the operating cost. 
         [0100]      FIG. 4  represents an exemplary embodiment of applying the output brine water (line  70 ) of the Stage #3 treatment ( FIG. 3 ) to a plasma crystallizer  90 . The plasma crystallizer  90  is an example of a known pyrolytic reactor that can be used to finish separation of water from salts dissolved therein. One skilled in the art will appreciate, however, that other thermal reactors may also be used without departing from the spirit and scope of the present invention. The example of a plasma reactor, which can be consistent with known plasma gasification/vitrification reactors, operated with one or more plasma torches  92 , as is well-known in published literature, is believed to provide opportunity for a favorable cost-benefit ratio. 
         [0101]    In general, for multistage operation, the plasma crystallizer  90  (or other reactor) is utilized after the final concentration stage when the output brine water has been concentrated to a desired level, as described in the above example. It can also be suitable to have a multistage system not only for salts concentration (as in  FIGS. 1-3 ), but also a separation subsystem with a reactor (e.g., plasma crystallizer  90 ) after any individual one of the early concentration stages (e.g., after either, or both, of Stages #1 and #2). However, it is generally more cost effective to have a single separation subsystem after the last of a determined number of concentration stages for the desired separation. 
         [0102]    In general, any thermal reactor may be used to separate the salts and the water. A reactor operated to produce disposable salts (referred to herein as a “crystallizer”) is generally suitable. Where the salts have toxicity, it may be desirable to operate the reactor in a manner so they are vitrified or made into glass. Accordingly, any reference to a crystallizer herein can also include a vitrifier. 
         [0103]    As shown in  FIG. 4 , the crystallizer  90  has a salts output at an outlet  95  that is generally equivalent to the total salts content of the original waste water. The water output of the total system is recovered as clean distilled water from the preheaters  12   a ,  12 ,  32   a ,  32 ,  52   a ,  52  of the respective stages of  FIGS. 1-3 , and/or may be recovered directly from excess steam exiting the crystallizer system  90  at line  80  and/or the excess steam exiting the respective flash evaporators  15 ,  35 ,  55  at line  99  (the excess steam is condensed to form distilled water). The pressure of the steam in line  99  is first increased by a compressor  100  from approximately 5 psia to 15 psia at line  110 . This excess steam  110  is then utilized to heat air in the heater  120  and then condensed in condenser  125  to produce distilled water at line  125   a . The condenser  125  can be cooled by air or by plant cooling tower water. 
         [0104]      FIG. 4  shows the brine water  70  entering the crystallizer  90  via a pump  91  that raises the pressure to 150 psia.  FIG. 4  also shows how steam from the crystallizer  90  can be redirected back to the respective earlier Stages of  FIGS. 1-3 . The steam output from the crystallizer  90  at line  80  may be provided back to the various Stages #1, #2 and #3 and used for heating by the respective heaters and condensers therein. Heated air at line  115  from the heater  120  is used in the stripper  130  which is utilized to remove, for example, volatile organic compounds (“VOCs”) from the waste water. Some excess steam may also be used for other purposes, e.g., to preheat the waste water in a preheater or a condenser. 
         [0105]    Before treatment in the Stages shown in  FIGS. 1-3 , the incoming waste water  10  can be, for example, sent to the stripper  130  where steam  115  is used to remove VOCs from the waste water  10 .  FIG. 4  shows steam from the concentration Stages #1, #2 and #3 at an input  99  of the compressor  100  that is elevated to a temperature of 213° F. for use in the stripper  130 . The excess steam can be used directly in the stripper  130 , as shown in  FIG. 4 , or used to heat air in a separate heat exchanger where the heated air is then used in the stripper to remove the VOCs. Additionally, the steam from the compressor  100  can be applied to another compressor  101  to increase its temperature and pressure to that of the steam in line  80 , and then combined with the steam in line  80 . 
         [0106]    The stripped wastewater is sent as feed to the input  20  to Stage #1 of  FIG. 1 . The VOCs which are removed from the waste water  10  exit the stripper  130  through a conduit  135  which is sent to a condenser  140 , in which the VOCs are condensed to form liquid by using, for example, cooling water or air. The VOCs exit the condenser  140  at outlet  136  which connects to the plasma crystallizer  90 . The VOCs are fed in front of the plasma torch  92  (e.g., along with brine water  70  from the pump  91 ) such that they intensely mix with the high temperature gases exiting from the plasma torch  92 . The plasma torch  92  is operated using appropriate gas (e.g., air, oxygen, hydrogen, etc.) that will aid in, or result in, the complete destruction of the VOCs. The VOCs are substantially converted to carbon dioxide and steam. The heat generated by this conversion of VOCs to carbon dioxide and steam is utilized in the plasma crystallizer  90 , along with heat inputted through the plasma torch  92 , to vaporize the water from the brine water  70 . This reduces the amount of heat and the corresponding amount of electricity utilized in the plasma crystallizer  90 , thus increasing its cost effectiveness. 
         [0107]    The steam exiting the plasma crystallizer  90  can be periodically vented to the atmosphere (not shown) to keep the levels of non-condensable gases low enough such that they do not degrade the performance of the heat exchangers used in the inventive system and process. 
         [0108]    It is therefore seen that systems and processes in accordance with the present invention can make use of known and available components (such as, for example, flash evaporators for concentration of salts and plasma (or other) gasifier reactors for crystallization (or vitrification) of the salts) in particular innovative ways with insight as to both the capital cost and the operating cost. A need for such cost effective water treatment has been heightened by practices such as, for example, the use of large amounts of water in natural gas drilling. However, the present invention may be used in any situation where impurities to be removed exist. 
         [0109]    In general summary, but without limitation, an embodiment of the present invention can be characterized in the following ways, for example: A system, and a corresponding method, in which waste water is supplied to one or more stages of equipment including a pump for pressurizing the water (e.g., to at least about 10 times atmospheric pressure), a heater that heats the pressurized waste water well above normal boiling temperature, a flash evaporator, or other device, that receives the heated, pressurized water and results in fluid evaporation and concentration of solids that were in the waste water. In for example, instances in which the waste (brine) water with concentrated solids cannot be otherwise readily and safely disposed of, a thermal or pyrolytic reactor is provided to crystallize or otherwise yield a form of the solids that can be readily and safely disposed of. In one form, such a reactor may also be applied as a heater for the original incoming waste water. Also, or alternatively, such a reactor may be used to form a vitrified glass of the salts output of any water treatment system that produces a brine water. 
         [0110]    Furthermore, the examples of  FIGS. 1-4  show how use can be made of flash evaporators operated at a low downstream pressure (e.g., 5 psia or only about one-third of 1 atm) along with compressors, as well as with a mixer for steam from a flash evaporator (after compression in a compressor) added with steam returned from a reactor. All of which is believed to contribute significantly to reduced operating costs which can be very beneficial, even though initial capital costs may be increased. 
         [0111]      FIGS. 5-8  illustrate a further embodiment of the present invention.  FIGS. 5, 6 and 7  will be individually discussed, but first their general relation to each other in an exemplary multi-stage system will be described.  FIG. 5  shows Stage #1. This first stage takes in waste water at an inlet  200 , processes it and produces first stage brine water at an outlet  220  of the first stage. The first stage brine water from the outlet  220  is input to the second stage shown in  FIG. 6  (Stage #2) for additional processing, and a resulting second stage brine water is produced as an output at outlet  240 . Similarly, the brine water from outlet  240  of the second stage is supplied as an input to the third stage shown in  FIG. 7  (Stage #3) that has additional processing, resulting in a third stage output of brine water at an outlet  260 . 
         [0112]    It will be seen and appreciated by one skilled in the art how the successive stages of  FIGS. 5, 6 and 7  increase the concentration of salts in the brine water (e.g., Total Dissolved Solids—“TDS”). It will also be appreciated how the number of stages is a variable that can be chosen according to various factors including, but not limited to, the salts content of the original waste water and the desired salt content after concentration. In general, a system in accordance with these exemplary embodiments may include any one or more stages such as are shown, for example, in  FIGS. 5-7 . The examples presented herein are merely illustrative of systems and methods that may be chosen not merely for good technical performance but also for reasons relating to economic factors, such as, for example, initial capital cost and operating cost, as well as convenience factors, such as, for example, space requirements and portability. While three stages are shown and described herein, one skilled in the art will appreciate that any number of stages may be utilized depending on the particular application without departing from the spirit and scope of the present invention. 
         [0113]    Each of the  FIGS. 5-8 , merely by way of further example and without limitation, are described in this specification, and include legends, including numerical values (all of which are merely representative approximations and are not necessarily exact technical values and/or calculations). Further, these legends are not necessarily the only suitable values that represent the nature and characteristics of materials as applied to, affected by, and resulting from the operations of the exemplary system(s). Not all such legends will be repeated in this text, although all form a part of this disclosure and are believed understandable to persons of ordinary skill in water treatment and thermal processes. As appreciated by one skilled in the art, such data are sometimes referred to as heat and material balances. It is specifically to be understood and will be appreciated by one skilled in the art that the various values indicated in the legends may have a tolerance of ±20%, as they are representative approximations and not exact technical values. 
         [0114]    Referring to  FIG. 5 , the waste water progresses from the input  200  to the output  240  successively through a pump  201 , a preheater  202 , a condenser  203 , and a flash evaporator  205 . One alternative is to have, in place of a single preheater  202 , a series of preheaters or heat exchangers. The heating medium for the preheater  202  can be excess steam available from a crystallizer  265  (see  FIG. 8 ) and/or hot water from the condenser  203 . 
         [0115]    In this example, the pump  201 , preheater  202 , and condenser  203  elevate the waste water pressure to 150 psia and the temperature to 360° F. at the inlet  206  to the flash evaporator  205  without use of any heater elements between the condenser  203  and flash evaporator  205 . The pump  201  elevates the pressure from 14.7 psia (1 atm) to 150 psia. The level of pressurization of waste water in all stages is such that there is no boiling of the waste water inside and across the heat exchanger surfaces of all heat exchangers used in this system. This is done to prevent the formation of deposits (scales, fouling etc.) on the heat exchanger surfaces. The preheater  202  elevates the temperature from 60° F. to 134° F., while the condenser  202  further elevates the temperature to 360° F. Additionally, the preheater  202  produces distilled water at outlet  207 . 
         [0116]    For drawing convenience, each concentration Stage ( FIGS. 5-7 ) shows a heater (e.g., heater  204  in  FIG. 5 , heater  224  in  FIG. 6 , heater  244  in  FIG. 7 ) which may be omitted entirely or, if present, not supplied with any heating fluid. As shown in  FIGS. 5-7 , that heater  204 ,  224 ,  244  has zero input and zero output of heating fluid (e.g., DowTherm™). For system equipment economy, heater  204 ,  224 ,  244  is preferably omitted. However, systems may be arranged as shown and provide the option to operate or to not operate such a heater  204 ,  224 ,  244 . Further explanation of what enables avoiding use of a heater  204 ,  224 ,  244  is given below. 
         [0117]    One aspect of Stage #1 of  FIG. 5  is, as shown in the legend to the right of the flash evaporator  205 , that it is operated so the flash pressure, i.e., the downstream or output pressure of the flash evaporator  205 , is approximately 25 psia, contrasting with the input or upstream pressure of 150 psia. The effect of this change in the pressure is that a portion of the water component of the waste water is separated from the dissolved solids in the form of steam. The remaining waste water becomes more concentrated in dissolved solids and exits the flash evaporator at outlet  220 . 
         [0118]    The condenser  203  receives some saturated steam directly from the crystallizer  265  of  FIG. 8  at line  266  which, with the preheater  202  elevating the waste water temperature from 60° F. to 134° F. before the condenser  203 , provides waste water at 360° F. from the condenser  203  and, favorably, there no need for the presence or operation of the heater  204 . Under certain operating conditions, the steam addition from the crystallizer  265  may be negative, i.e., steam is sent as excess to the crystallizer  265  for other uses (e.g., as a heat source for the stripper  270 ). 
         [0119]    The Stage #1 output  220  has the volume of waste water reduced from the input  200  with the salts more concentrated to approximately 23% TDS, which is increased from the initial approximately 20% TDS in the exemplary waste water at the input  200 . 
         [0120]    Stages #2 and #3 in  FIGS. 6 and 7 , respectively, have essentially the same equipment as shown in  FIG. 5  for Stage #1 but with some different operating parameters as shown in the legends of  FIGS. 6-7 . Each of Stages #2 and #3 may also omit, or not operate, a heater between the condenser and flash evaporator of that stage. 
         [0121]    Referring to  FIG. 6  (Stage #2), the brine water progresses from the input  200  to the output  240  successively through a pump  221 , a preheater  222 , a condenser  223 , and a flash evaporator  225 . One alternative is to have, in place of a single preheater  222 , a series of preheaters or heat exchangers. The heating medium for the preheater  222  can be excess steam available from a crystallizer  265  (see  FIG. 8 ) and/or hot water from the condenser  223 . 
         [0122]    In this example, the pump  221 , preheater  222 , and condenser  223  elevate the waste water pressure to 150 psia and the temperature to 360° F. at the inlet  226  to the flash evaporator  225  without use of any heater elements between the condenser  223  and flash evaporator  225 . The pump  221  elevates the pressure from 25 psia to 150 psia. The preheater  222  elevates the temperature from 239° F. to 253° F., while the condenser  222  further elevates the temperature to 360° F. Additionally, the preheater  222  produces distilled water at outlet  227 . 
         [0123]    One aspect of Stage #2 of  FIG. 6  is, as shown in the legend to the right of the flash evaporator  225 , that it is operated so the flash pressure, i.e., the downstream or output pressure of the flash evaporator  225 , is approximately 25 psia, contrasting with the input or upstream pressure of 150 psia. The effect of this change in the pressure is that a portion of the water component of the waste water is separated from the dissolved solids in the form of steam. The remaining waste water becomes more concentrated in dissolved solids and exits the flash evaporator at outlet  240 . 
         [0124]    The condenser  223  receives some saturated steam directly from the crystallizer  265  of  FIG. 8  at line  266  which, with the preheater  222  elevating the waste water temperature from 239° F. to 253° F. before the condenser  223 , provides waste water at 360° F. from the condenser  223  and, favorably, there no need for the presence or operation of the heater  224 . Under certain operating conditions, the steam addition from the crystallizer  265  may be negative, i.e., steam is sent as excess to the crystallizer  265  for other uses (e.g., as a heat source for the stripper  270 ). 
         [0125]    The Stage #2 output  240  has the volume of waste water reduced from the input  220  with the salts more concentrated to approximately 26% TDS, which is increased from the initial approximately 23% TDS in the exemplary waste water at the input  220 . 
         [0126]    Referring to  FIG. 7  (Stage #3), the brine water progresses from the input  240  to the output  260  successively through a pump  241 , a preheater  242 , a condenser  243 , and a flash evaporator  245 . One alternative is to have, in place of a single preheater  242 , a series of preheaters or heat exchangers. The heating medium for the preheater  242  can be excess steam available from a crystallizer  265  (see  FIG. 8 ) and/or hot water from the condenser  243 . 
         [0127]    In this example, the pump  241 , preheater  242 , and condenser  243  elevate the waste water pressure to 150 psia and the temperature to 360° F. at the inlet  246  to the flash evaporator  245  without use of any heater elements between the condenser  243  and flash evaporator  245 . The pump  241  elevates the pressure from 25 psia to 150 psia. The preheater  242  elevates the temperature from 239° F. to 254° F., while the condenser  242  further elevates the temperature to 360° F. Additionally, the preheater  242  produces distilled water at outlet  247 . 
         [0128]    One aspect of Stage #3 of  FIG. 7  is, as shown in the legend to the right of the flash evaporator  245 , that it is operated so the flash pressure, i.e., the downstream or output pressure of the flash evaporator  245 , is approximately 25 psia, contrasting with the input or upstream pressure of 150 psia. The effect of this change in the pressure is that a portion of the water component of the waste water is separated from the dissolved solids in the form of steam. The remaining waste water becomes more concentrated in dissolved solids and exits the flash evaporator at outlet  260 . 
         [0129]    The condenser  243  receives some saturated steam directly from the crystallizer  265  of  FIG. 8  at line  266  which, with the preheater  242  elevating the waste water temperature from 239° F. to 254° F. before the condenser  243 , provides waste water at 360° F. from the condenser  243  and, favorably, there no need for the presence or operation of the heater  244 . Under certain operating conditions, the steam addition from the crystallizer  265  may be negative, i.e., steam is sent as excess to the crystallizer  265  for other uses (e.g., as a heat source for the stripper  270 ). 
         [0130]    The Stage #3 output  260  has the volume of waste water reduced from the input  240  with the salts more concentrated to approximately 30% TDS, which is increased from the initial approximately 26% TDS in the exemplary waste water at the input  220 . 
         [0131]    The exemplary system includes multiple (three) concentration stages ( FIGS. 5-7 ) that are substantially alike in the combination of equipment used. However, other exemplary systems with multiple concentration stages may have individual stages of more varied combinations of equipment without departing from the spirit and scope of the present invention. 
         [0132]    The level of pressurization of waste water in all stages is such that there is no boiling (nucleate or other type) of the waste water inside and across the heat exchanger surfaces of the condensers and preheaters of each stage. This prevents the formation of deposits (scales, fouling etc.) on the heat exchanger surfaces and reduces the requirement for cleaning of the heat exchangers. This results in the reduction of the operating cost. 
         [0133]      FIG. 8  represents an example of applying the output brine water (line  260 ) of the Stage #3 treatment ( FIG. 7 ) to a plasma crystallizer  265 . The plasma crystallizer  265  is an example of a known pyrolytic reactor that can be used to finish separation of water from salts dissolved in it. One skilled in the relevant art will appreciate, however, that other thermal reactors may also be used without departing from the spirit and scope of the present invention. The example of a plasma reactor, which can be consistent with known plasma gasification/vitrification reactors, operated with one or more plasma torches  267 , as is well-known in published literature, is believed to provide opportunity for a favorable cost-benefit ratio. 
         [0134]    In general, for multistage operation, the plasma crystallizer  265  (or other reactor) is utilized at the final concentration stage when the output brine water has been concentrated to a desired level, as described in the above example. It can also be suitable to have a multistage system not only for salts concentration (as in  FIGS. 5-7 ), but also a separation subsystem with a reactor after any individual one of the early concentration stages (e.g., after either, or both, of Stages #1 and #2). However, it is generally more cost effective to have a single separation subsystem after the last of a determined number of concentration stages for the desired separation. 
         [0135]    In general, any thermal reactor may be used to separate the salts and the water. A reactor operated to produce disposable salts (referred to herein as a “crystallizer”) is generally suitable. Where the salts have toxicity, it may be desirable to operate the reactor in a manner so they are vitrified or made into glass. Accordingly, any reference to a crystallizer herein can also include a vitrifier. 
         [0136]    As shown in  FIG. 8 , the crystallizer  265  has a salts output at an outlet  268  equivalent to the total salts content of the original wastewater. The water output of the total system is now recovered as clean distilled water from the preheaters  202 ,  222 ,  242  of the respective Stages of  FIGS. 5-7 , and/or may also be recovered directly from steam exiting the crystallizer  265 . 
         [0137]      FIG. 8  shows brine water  260  entering the crystallizer  265  via a pump  280  that raises the pressure to 180 psia.  FIG. 8  also shows how steam from the crystallizer  265  can be redirected back to the respective earlier Stages of  FIGS. 5-7 . The steam output from the crystallizer  265  at line  266  may be provided back to the various Stages #1, #2 and #3 and used for heating by the respective preheaters and condensers therein. Also,  FIG. 8  shows an “Excess Steam to Stripper” of a certain amount at line  269 . This steam  269  is used in a stripper  270  which is utilized to remove volatile organic compounds (“VOCs”) from the waste water before processing. Some excess steam from the crystallizer  265  may also be used for other purposes, e.g., to preheat the input waste water in a preheater or condenser. 
         [0138]    Before treatment in the Stages shown in  FIGS. 5-7 , the incoming waste water  10  can be, for example, sent to the stripper  270  where the steam  269  is used to remove VOCs from the waste water  10 .  FIG. 8  shows steam from concentration Stages #1, #2 and #3 at an input  272  joined at a junction  273  with exiting steam from the crystallizer  265  that has been reduced in pressure by expansion in a mechanical vapor turbine  275  to recover energy and reduce the total amount of energy used in the process. The excess steam  269  can be used directly in the stripper  270 , as shown in  FIG. 8 , or used to heat air in a separate heat exchanger where the heated air is then used in the stripper to remove the VOCs. The stripped waste water is sent as feed to the input  200  to Stage #1 of  FIG. 5 . The VOCs which are removed from the waste water  10  exit the stripper through a conduit  277  which connects to the plasma crystallizer  265 . Additionally or alternatively, a condenser with a knock-out pot (not shown) can be used between the plasma crystallizer  265  and the stripper  270  with the condensed VOCs (as well as any stripped VOCs) fed directly to the plasma crystallizer  265 . The VOCs are fed in front of the plasma torch  267  (e.g., along with brine water  260  from Stage #3 from the pump  280 ) such that they intensely mix with the high temperature gases exiting from the plasma torch  267 . The plasma torch  267  is operated using appropriate gas (e.g., air, oxygen, hydrogen, etc.) that will aid in, or result in, the complete destruction of the VOCs. The VOCs are substantially converted to carbon dioxide and steam. The heat generated by this conversion of VOCs to carbon dioxide and steam is utilized in the plasma crystallizer  265 , along with heat inputted through the plasma torch  267 , to vaporize the water from the brine water  260 . This reduces the amount of heat and the corresponding amount of electricity utilized in the plasma crystallizer  265 , thus increasing its cost effectiveness. 
         [0139]    The steam exiting the plasma crystallizer  265  can be periodically vented to the atmosphere (not shown) to keep the levels of non-condensable gases low enough such that they do not degrade the performance of the heat exchangers used in the inventive system and process. 
         [0140]    It is therefore seen that systems and processes in accordance with the further embodiment of the present invention can make use of known and available components, such as, for example, flash evaporators for concentration of salts and plasma (or other) gasifier reactors for crystallization (or vitrification) of the salts, in particular innovative ways with insight as to both the capital cost and the operating cost. A need for such cost effective water treatment has been heightened by practices such as the use of large amounts of water in natural gas drilling However, the present invention may be used in any situation where impurities to be removed exist. 
         [0141]    In general summary, but without limitation, the further embodiment of the present invention can be characterized in the following ways, for example: A system, and a corresponding method, in which waste water is supplied to one or more stages of equipment including a pump for pressurizing the water (e.g., to at least about 10 times atmospheric pressure), a heater that heats the pressurized water well above normal boiling temperature, a flash evaporator, or other device, that receives the heated, pressurized water and results in fluid evaporation and concentration of solids that were in the wastewater, and, for instances in which the brine water with concentrated solids cannot be otherwise readily and safely disposed of, a thermal or pyrolytic reactor to crystallize or otherwise yield a form of the solids that can be readily and safely disposed of, such a reactor may also be applied as a heater for the original incoming waste water. Also, or alternatively, such a reactor may be used to form a vitrified glass of the salts output of any water treatment system that produces a brine water. 
         [0142]    Furthermore, the examples provided herein show how use can be made of flash evaporators operated at reduced downstream pressure (e.g., 25 psia compared to 150 psia upstream pressure) along with an expander (e.g., turbine), for energy recovery from the steam output of a crystallizer. All of which is believed to contribute significantly to reduced operating costs which can be very beneficial, even though initial capital costs may be increased. 
         [0143]      FIGS. 9-12  illustrate yet a further embodiment of the present invention.  FIGS. 9, 10 and 11  will be individually discussed, but first their general relation to each other in an exemplary multi-stage system will be described.  FIG. 9  shows Stage #1. This first stage takes in waste water at an inlet  300 , processes it and produces first stage brine water at an outlet  320  of the first stage. The first stage brine water from the outlet  320  is input to the second stage shown in  FIG. 10  (Stage #2) for additional processing, and a resulting second stage brine water is produced as an output at outlet  340 . Similarly, the brine water from outlet  340  of the second stage is supplied as an input to the third stage shown in  FIG. 11  (Stage #3) that has additional processing, resulting in a third stage output of brine water at an outlet  360 . 
         [0144]    It will be seen and appreciated by one skilled in the art how the successive stages of  FIGS. 9, 10 and 11  increase the concentration of salts in the brine water (e.g., Total Dissolved Solids—“TDS”). It will also be appreciated how the number of stages is a variable that can be chosen according to various factors including, but not limited to, the salts content of the original waste water and the desired salt content after concentration. In general, a system in accordance with these exemplary embodiments may include any one or more stages such as are shown, for example, in  FIGS. 9-11 . The examples presented herein are merely illustrative of systems and methods that may be chosen not merely for good technical performance but also for reasons relating to economic factors, such as, for example, initial capital cost and operating cost, as well as convenience factors, such as, for example, space requirements and portability. While three stages are shown and described herein, one skilled in the art will appreciate that any number of stages may be utilized depending on the particular application without departing from the spirit and scope of the present invention. 
         [0145]    Each of the  FIGS. 9-12 , merely by way of further example and without limitation, are described in this specification, and include legends, including numerical values (all of which are merely representative approximations and are not necessarily exact technical values and/or calculations). Further, these legends are not necessarily the only suitable values that represent the nature and characteristics of materials as applied to, affected by, and resulting from the operations of the exemplary system(s). Not all such legends will be repeated in this text, although all form a part of this disclosure and are believed understandable to persons of ordinary skill in water treatment and thermal processes. As appreciated by one skilled in the art, such data are sometimes referred to as heat and material balances. It is specifically to be understood and will be appreciated by one skilled in the art that the various values indicated in the legends may have a tolerance of ±20%, as they are representative approximations and not exact technical values. 
         [0146]    Referring to  FIG. 9 , the waste water progresses from the input  300  to the output  340  successively through a pump  301 , a preheater  302 , a condenser  303 , and a flash evaporator  305 . One alternative is to have, in place of a single preheater  302 , a series of preheaters or heat exchangers. The heating medium for the preheater  302  can be excess steam available from a crystallizer  365  (see  FIG. 12 ) and/or hot water from the condenser  303 . 
         [0147]    In this example, the pump  301 , preheater  302 , and condenser  303  elevate the waste water pressure to 150 psia and the temperature to 360° F. at the inlet  306  to the flash evaporator  305  without use of any heater elements between the condenser  303  and flash evaporator  305 . The pump  301  elevates the pressure from 14.7 psia (1 atm) to 150 psia. The level of pressurization of waste water in all stages is such that there is no boiling of the waste water inside and across the heat exchanger surfaces of all heat exchangers used in this system. This is done to prevent the formation of deposits (scales, fouling, etc.) on the heat exchanger surfaces. The preheater  302  elevates the temperature from 60° F. to 134° F., while the condenser  302  further elevates the temperature to 360° F. Additionally, the preheater  302  produces distilled water at outlet  307 . 
         [0148]    For drawing convenience, each concentration Stage ( FIGS. 9-11 ) shows a heater (e.g., heater  304  in  FIG. 9 , heater  324  in  FIG. 10 , heater  344  in  FIG. 11 ) between the condenser and flash evaporator, which may be omitted entirely or, if present, not supplied with any heating fluid. As shown in  FIGS. 9-11 , that heater  304 ,  324 ,  344  has zero input and zero output of heating fluid (e.g., DowTherm™). For system equipment economy, heater  304 ,  324 ,  344  is preferably omitted. However, systems may be arranged as shown and provide the option to operate or to not operate such a heater  304 ,  324 ,  344 . Further explanation of what enables avoiding use of a heater  304 ,  324 ,  344  is given below. 
         [0149]    One aspect of Stage #1 of  FIG. 9  is, as shown in the legend to the right of the flash evaporator  305 , that it is operated so the flash pressure, i.e., the downstream or output pressure of the flash evaporator  305 , is approximately 5 psia, contrasting with the input or upstream pressure of 150 psia and the flash pressure of 25 psia in  FIGS. 5-8 . The effect of this change in the pressure is that a larger portion of the water component of the waste water is separated from the dissolved solids in the form of steam. The remaining waste water becomes more concentrated in dissolved solids and exits the flash evaporator at outlet  320 . 
         [0150]    The condenser  303  receives some saturated steam directly from the crystallizer  365  of  FIG. 12  at line  366  which, with the preheater  302  elevating the waste water temperature from 60° F. to 134° F. before the condenser  303 , provides waste water at 360° F. from the condenser  303  and, favorably, there no need for the presence or operation of the additional heater  304 . Under certain operating conditions, the steam addition from the crystallizer  365  may be negative, i.e., steam is sent as excess to the crystallizer  365  for other uses (e.g., as a heat source for the stripper  370 ). 
         [0151]    The Stage #1 output  320  has the volume of waste water reduced from the input  300  with the salts more concentrated to approximately 25% TDS, which is increased from the initial approximately 20% TDS in the exemplary waste water at the input  300 . 
         [0152]    Stages #2 and #3 in  FIGS. 10 and 11 , respectively, have essentially the same equipment as shown in  FIG. 9  for Stage #1 but with some different operating parameters as shown in the legends of  FIGS. 10-11 . Each of Stages #2 and #3 may also omit, or not operate, a heater between the condenser and flash evaporator of that stage. 
         [0153]    Referring to  FIG. 10  (Stage #2), the brine water progresses from the input  300  to the output  340  successively through a pump  321 , a preheater  322 , a condenser  323 , and a flash evaporator  325 . One alternative is to have, in place of a single preheater  322 , a series of preheaters or heat exchangers. The heating medium for the preheater  322  can be excess steam available from a crystallizer  365  (see  FIG. 12 ) and/or hot water from the condenser  323 . 
         [0154]    In this example, the pump  321 , preheater  322 , and condenser  323  elevate the waste water pressure to 150 psia and the temperature to 360° F. at the inlet  326  to the flash evaporator  325  without use of any heater elements between the condenser  323  and flash evaporator  325 . The pump  321  elevates the pressure from 5 psia to 150 psia. The preheater  322  elevates the temperature from 162° F. to 197° F., while the condenser  322  further elevates the temperature to 360° F. Additionally, the preheater  322  produces distilled water at outlet  327 . 
         [0155]    One aspect of Stage #2 of  FIG. 10  is, as shown in the legend to the right of the flash evaporator  325 , that it is operated so the flash pressure, i.e., the downstream or output pressure of the flash evaporator  325 , is approximately 5 psia, contrasting with the input or upstream pressure of 150 psia and the flash pressure of 25 psia in  FIGS. 5-8 . The effect of this change in the pressure is that a larger portion of the water component of the waste water is separated from the dissolved solids in the form of steam. The remaining waste water becomes more concentrated in dissolved solids and exits the flash evaporator at outlet  340 . 
         [0156]    The condenser  323  receives some saturated steam directly from the crystallizer  365  of  FIG. 12  at line  366  which, with the preheater  322  elevating the waste water temperature from 162° F. to 197° F. before the condenser  323 , provides waste water at 360° F. from the condenser  323  and, favorably, there no need for the presence or operation of the heater  324 . Under certain operating conditions, the steam addition from the crystallizer  365  may be negative, i.e., steam is sent as excess to the crystallizer  365  for other uses (e.g., as a heat source for the stripper  370 ). 
         [0157]    The Stage #2 output  340  has the volume of waste water reduced from the input  320  with the salts more concentrated to approximately 31% TDS, which is increased from the initial approximately 25% TDS in the exemplary waste water at the input  320 . 
         [0158]    Referring to  FIG. 11  (Stage #3), the brine water progresses from the input  340  to the output  360  successively through a pump  341 , a preheater  342 , a condenser  343 , and a flash evaporator  345 . One alternative is to have, in place of a single preheater  342 , a series of preheaters or heat exchangers. The heating medium for the preheater  342  can be excess steam available from a crystallizer  365  (see  FIG. 12 ) and/or hot water from the condenser  343 . 
         [0159]    In this example, the pump  341 , preheater  342 , and condenser  343  elevate the waste water pressure to 150 psia and the temperature to 360° F. at the inlet  346  to the flash evaporator  345  without use of any heater elements between the condenser  343  and flash evaporator  345 . The pump  341  elevates the pressure from 5 psia to 150 psia. The preheater  342  elevates the temperature from 162° F. to 197° F., while the condenser  342  further elevates the temperature to 360° F. Additionally, the preheater  342  produces distilled water at outlet  347 . 
         [0160]    One aspect of Stage #3 of  FIG. 11  is, as shown in the legend to the right of the flash evaporator  345 , that it is operated so the flash pressure, i.e., the downstream or output pressure of the flash evaporator  345 , is approximately 5 psia, contrasting with the input or upstream pressure of 150 psia and the flash pressure of 25 psia in  FIGS. 5-8 . The effect of this change in the pressure is that a larger portion of the water component of the waste water is separated from the dissolved solids in the form of steam. The remaining waste water becomes more concentrated in dissolved solids and exits the flash evaporator at outlet  360 . 
         [0161]    The condenser  343  receives some saturated steam directly from the crystallizer  365  of  FIG. 12  at line  366  which, with the preheater  342  elevating the waste water temperature from 162° F. to 197° F. before the condenser  343 , provides waste water at 360° F. from the condenser  343  and, favorably, there no need for the presence or operation of the heater  344 . Under certain operating conditions, the steam addition from the crystallizer  365  may be negative, i.e., steam is sent as excess to the crystallizer  365  for other uses (e.g., as a heat source for the stripper  370 ). 
         [0162]    The Stage #3 output  360  has the volume of waste water reduced from the input  340  with the salts more concentrated to approximately 39% TDS, which is increased from the initial approximately 31% TDS in the exemplary waste water at the input  320 . 
         [0163]    The exemplary system includes multiple (three) concentration stages ( FIGS. 9-11 ) that are substantially alike in the combination of equipment used. However, other exemplary systems with multiple concentration stages may have individual stages of more varied combinations of equipment without departing from the spirit and scope of the present invention. 
         [0164]    The level of pressurization of waste water in all stages is such that there is no boiling (nucleate or other type) of the waste water inside and across the heat exchanger surfaces of the condensers and preheaters of each stage. This prevents the formation of deposits (scales, fouling, etc.) on the heat exchanger surfaces and reduces the requirement for cleaning of the heat exchangers. This results in the reduction of the operating cost. 
         [0165]      FIG. 12  represents an example of applying the output brine water (line  360 ) of the Stage #3 treatment ( FIG. 11 ) to a plasma crystallizer  365 . The plasma crystallizer  365  is an example of a known pyrolytic reactor that can be used to finish separation of water from salts dissolved in it. One skilled in the relevant art will appreciate, however, that other thermal reactors may also be used without departing from the spirit and scope of the present invention. The example of a plasma reactor, which can be consistent with known plasma gasification/vitrification reactors, operated with one or more plasma torches  367 , as is well-known in published literature, is believed to provide opportunity for a favorable cost-benefit ratio. 
         [0166]    In general, for multistage operation, the plasma crystallizer  365  (or other reactor) is utilized at the final concentration stage when the output brine water has been concentrated to a desired level, as described in the above example. It can also be suitable to have a multistage system not only for salts concentration (as in  FIGS. 9-11 ), but also a separation subsystem with a reactor after any individual one of the early concentration stages (e.g., after either, or both, of Stages #1 and #2). However, it is generally more cost effective to have a single separation subsystem after the last of a determined number of concentration stages for the desired separation. 
         [0167]    In general, any thermal reactor may be used to separate the salts and the water. A reactor operated to produce disposable salts (referred to herein as a “crystallizer”) is generally suitable. Where the salts have toxicity, it may be desirable to operate the reactor in a manner so they are vitrified or made into glass. Accordingly, any reference to a crystallizer herein can also include a vitrifier. 
         [0168]    As shown in  FIG. 12 , the crystallizer  365  has a salts output at an outlet  368  equivalent to the total salts content of the original wastewater. The water output of the total system is now recovered as clean distilled water from the preheaters  302 ,  322 ,  342  of the respective Stages of  FIGS. 9-11 , and/or may also be recovered directly from steam exiting the crystallizer  365 . 
         [0169]      FIG. 12  shows brine water  360  entering the crystallizer  365  via a pump  380  that raises the pressure to 180 psia.  FIG. 12  also shows how steam from the crystallizer  365  can be redirected back to the respective earlier Stages of  FIGS. 9-11 . The steam output from the crystallizer  365  at line  366  may be provided back to the various Stages #1, #2 and #3 and used for heating by the respective preheaters and condensers therein. Also,  FIG. 12  shows an “Excess Steam to Stripper” of a certain amount at line  369 . This steam  369  is used in a stripper  370  which is utilized to remove volatile organic compounds (“VOCs”) from the waste water before processing. Some excess steam from the crystallizer  365  may also be used for other purposes, e.g., to preheat the input waste water in a preheater or condenser. 
         [0170]    Before treatment in the Stages shown in  FIGS. 9-11 , the incoming waste water  10  can be, for example, sent to the stripper  370  where the steam  369  is used to remove VOCs from the waste water  10 . The excess steam  369  can be used directly in the stripper  370 , as shown in  FIG. 12 , or used to heat air in a separate heat exchanger where the heated air is then used in the stripper to remove the VOCs. The stripped waste water is sent as feed to the input  300  to Stage #1 of  FIG. 9 . The VOCs which are removed from the waste water  10  exit the stripper through a conduit  377  which connects to the plasma crystallizer  365 . Additionally or alternatively, a condenser with a knock-out pot (not shown) can be used between the plasma crystallizer  365  and the stripper  370  with the condensed VOCs (as well as any stripped VOCs) fed directly to the plasma crystallizer  365 . The VOCs are fed in front of the plasma torch  367  (e.g., along with brine water  360  from Stage #3 from the pump  380 ) such that they intensely mix with the high temperature gases exiting from the plasma torch  367 . The plasma torch is operated using appropriate gas (e.g., air, oxygen, hydrogen, etc.) that will aid in, or result in, the complete destruction of the VOCs. The VOCs are substantially converted to carbon dioxide and steam. The heat generated by this conversion of VOCs to carbon dioxide and steam is utilized in the plasma crystallizer  365 , along with heat inputted through the plasma torch  367 , to vaporize the water from the brine water  360 . This reduces the amount of heat and the corresponding amount of electricity utilized in the plasma crystallizer  365 , thus increasing its cost effectiveness. 
         [0171]    The steam exiting the plasma crystallizer  365  can be periodically vented to the atmosphere (not shown) to keep the levels of non-condensable gases low enough such that they do not degrade the performance of the heat exchangers used in the inventive system and process. 
         [0172]      FIG. 12  also shows some steam (e.g., about 36% of the input, in lbs/hr) from the flash evaporators  305 ,  325 ,  345  of concentration Stages #1, #2 and #3 at an input  372  goes to a compressor  375  that is elevated to 180 psia and a temperature of 373° F. for part of the steam that goes back to the treatment Stages of  FIGS. 9-11 . 
         [0173]    It is therefore seen that systems and processes in accordance with the yet further embodiment of the present invention can make use of known and available components, such as, for example, flash evaporators for concentration of salts and plasma (or other) gasifier reactors for crystallization (or vitrification) of the salts, in particular innovative ways with insight as to both the capital cost and the operating cost. A need for such cost effective water treatment has been heightened by practices such as the use of large amounts of water in natural gas drilling However, the present invention may be used in any situation where impurities to be removed exist. 
         [0174]    In general summary, but without limitation, the yet further embodiment of the present invention can be characterized in the following ways, for example: A system, and a corresponding method, in which waste water is supplied to one or more stages of equipment including a pump for pressurizing the water (e.g., to at least about 10 times atmospheric pressure), a heater that heats the pressurized water well above normal boiling temperature, a flash evaporator, or other device, that receives the heated, pressurized water and results in fluid evaporation and concentration of solids that were in the wastewater, and, for instances in which the brine water with concentrated solids cannot be otherwise readily and safely disposed of, a thermal or pyrolytic reactor to crystallize or otherwise yield a form of the solids that can be readily and safely disposed of, such a reactor may also be applied as a heater for the original incoming waste water. Also, or alternatively, such a reactor may be used to form a vitrified glass of the salts output of any water treatment system that produces a brine water. 
         [0175]    Furthermore, the examples provided herein show how use can be made of flash evaporators operated at low downstream pressure (e.g., 5 psia or only about one-third of 1 atm) along with a compressor elevating the pressure of some steam from the flash evaporators to, e.g., 180 psia, before being added with steam from the reactor that goes back to the earlier concentrations Stages. All of which is believed to contribute significantly to reduced operating costs which can be very beneficial, even though initial capital costs may be increased. 
         [0176]      FIGS. 13-15  illustrate still a further embodiment of the present invention.  FIGS. 13, 14 and 15  will be individually discussed, but first their general relation to each other in an exemplary multi-stage system will be described.  FIG. 13  shows Stage #1. This first stage takes in waste water at an inlet  400 , processes it and produces first stage brine water at an outlet  420  of the first stage. The first stage brine water from the outlet  420  is input to the second stage shown in  FIG. 14  (Stage #2) for additional processing, and a resulting second stage brine water is produced as an output at outlet  440 . Similarly, the brine water from outlet  440  of the second stage is supplied as an input to the third stage shown in  FIG. 15  (Stage #3) that has additional processing, resulting in a third stage output of brine water at an outlet  460 . 
         [0177]    It will be seen and appreciated by one skilled in the art how the successive stages of  FIGS. 13, 14 and 15  increase the concentration of salts in the brine water (e.g., Total Dissolved Solids—“TDS”). It will also be appreciated how the number of stages is a variable that can be chosen according to various factors including, but not limited to, the salts content of the original waste water and the desired salt content after concentration. In general, a system in accordance with these exemplary embodiments may include any one or more stages such as are shown, for example, in  FIGS. 13-15 . The examples presented herein are merely illustrative of systems and methods that may be chosen not merely for good technical performance but also for reasons relating to economic factors, such as, for example, initial capital cost and operating cost, as well as convenience factors, such as, for example, space requirements and portability. While three stages are shown and described herein, one skilled in the art will appreciate that any number of stages may be utilized depending on the particular application without departing from the spirit and scope of the present invention. 
         [0178]    Each of the  FIGS. 13-16 , merely by way of further example and without limitation, are described in this specification, and include legends, including numerical values (all of which are merely representative approximations and are not necessarily exact technical values and/or calculations). Further, these legends are not necessarily the only suitable values that represent the nature and characteristics of materials as applied to, affected by, and resulting from the operations of the exemplary system(s). Not all such legends will be repeated in this text, although all form a part of this disclosure and are believed understandable to persons of ordinary skill in water treatment and thermal processes. As appreciated by one skilled in the art, such data are sometimes referred to as heat and material balances. It is specifically to be understood and will be appreciated by one skilled in the art that the various values indicated in the legends may have a tolerance of ±20%, as they are representative approximations and not exact technical values. 
         [0179]    Referring to  FIG. 13  (Stage #1), the waste water progresses from the input  400  to the output  440  successively through a pump  401 , a preheater  402 , a condenser  403 , and a flash evaporator  405 . One alternative is to have, in place of a single preheater  402 , a series of preheaters or heat exchangers. The heating medium for the preheater  402  can be excess steam available from a crystallizer  465  (see  FIG. 16 ) and/or hot water from the condenser  403 . 
         [0180]    In this example, the pump  401 , preheater  402 , and condenser  403  elevate the waste water pressure to 400 psia and the temperature to 445° F. at the inlet  406  to the flash evaporator  405  without use of any heater elements between the condenser  403  and flash evaporator  405 . The pump  401  elevates the pressure from 14.7 psia (1 atm) to 400 psia. The level of pressurization of waste water in all stages is such that there is no boiling of the waste water inside and across the heat exchanger surfaces of all heat exchangers used in this system. This is done to prevent the formation of deposits (scales, fouling, etc.) on the heat exchanger surfaces. The preheater  402  elevates the temperature from 60° F. to 254° F., while the condenser  402  further elevates the temperature to 445° F. Additionally, the preheater  402  produces distilled water at outlet  407 . 
         [0181]    For drawing convenience, each concentration Stage ( FIGS. 13-15 ) shows a heater (e.g., heater  404  in  FIG. 13 , heater  424  in  FIG. 14 , heater  444  in  FIG. 15 ) between the condenser and flash evaporator, which may be omitted entirely or, if present, not supplied with any heating fluid. As shown in  FIGS. 13-15 , that heater  404 ,  424 ,  444  has zero input and zero output of heating fluid (e.g., DowTherm™). For system equipment economy, heater  404 ,  424 ,  444  is preferably omitted. However, systems may be arranged as shown and provide the option to operate or to not operate such a heater  404 ,  424 ,  444 . Further explanation of what enables avoiding use of a heater  404 ,  424 ,  444  is given below. 
         [0182]    One aspect of Stage #1 of  FIG. 13  is, as shown in the legend to the right of the flash evaporator  405 , that it is operated so the flash pressure, i.e., the downstream or output pressure of the flash evaporator  405 , is approximately 15 psia, contrasting with the input or upstream pressure of 400 psia. The effect of this change in the pressure is that a larger portion of the water component of the waste water is separated from the dissolved solids in the form of steam. The remaining waste water becomes more concentrated in dissolved solids and exits the flash evaporator at outlet  420 . 
         [0183]    The condenser  403  receives some saturated steam directly from the crystallizer  465  of  FIG. 16  at line  466  which, with the preheater  402  elevating the waste water temperature from 60° F. to 254° F. before the condenser  403 , provides waste water at 445° F. from the condenser  403  and, favorably, there no need for the presence or operation of the additional heater  404 . In the exemplary system, the elevation in temperature is the effect of steam from the steam output  466  of the crystallizer subsystem  465  of  FIG. 16 . That steam continues to the condenser  403  and the preheater  402  until it exits the preheater  402  at line  407  as distilled water. Under certain operating conditions, the steam addition from the crystallizer  465  may be negative, i.e., steam is sent as excess to the crystallizer  465  for other uses (e.g., as a heat source for the stripper  470 ). 
         [0184]    The Stage #1 output  420  has the volume of waste water reduced from the input  400  with the salts more concentrated to approximately 27% TDS, which is increased from the initial approximately 20% TDS in the exemplary waste water at the input  400 . 
         [0185]    Stages #2 and #3 in  FIGS. 14 and 15 , respectively, have essentially the same equipment as shown in  FIG. 13  for Stage #1 but with some different operating parameters as shown in the legends of  FIGS. 14-15 . Each of Stages #2 and #3 may also omit, or not operate, a heater between the condenser and flash evaporator of that stage. 
         [0186]    Referring to  FIG. 14  (Stage #2), the brine water progresses from the input  400  to the output  440  successively through a pump  421 , a preheater  422 , a condenser  423 , and a flash evaporator  425 . One alternative is to have, in place of a single preheater  422 , a series of preheaters or heat exchangers. The heating medium for the preheater  422  can be excess steam available from a crystallizer  465  (see  FIG. 16 ) and/or hot water from the condenser  423 . 
         [0187]    In this example, the pump  421 , preheater  422 , and condenser  423  elevate the waste water pressure to 400 psia and the temperature to 445° F. at the inlet  426  to the flash evaporator  425  without use of any heater elements between the condenser  423  and flash evaporator  425 . The pump  421  elevates the pressure from 15 psia to 400 psia. The preheater  422  elevates the temperature from 212° F. to 272° F., while the condenser  422  further elevates the temperature to 445° F. Additionally, the preheater  422  produces distilled water at outlet  427 . 
         [0188]    One aspect of Stage #2 of  FIG. 14  is, as shown in the legend to the right of the flash evaporator  425 , that it is operated so the flash pressure, i.e., the downstream or output pressure of the flash evaporator  425 , is approximately 15 psia, contrasting with the input or upstream pressure of 400. The effect of this change in the pressure is that a larger portion of the water component of the waste water is separated from the dissolved solids in the form of steam. The remaining waste water becomes more concentrated in dissolved solids and exits the flash evaporator at outlet  440 . 
         [0189]    The condenser  423  receives some saturated steam directly from the crystallizer  465  of  FIG. 16  at line  466  which, with the preheater  422  elevating the waste water temperature from 212° F. to 272° F. before the condenser  423 , provides waste water at 445° F. from the condenser  423  and, favorably, there no need for the presence or operation of the heater  424 . In the exemplary system, the elevation in temperature is the effect of steam from the steam output  466  of the crystallizer subsystem  465  of  FIG. 16 . That steam continues to the condenser  423  and the preheater  422  until it exits the preheater  422  at line  427  as distilled water. Under certain operating conditions, the steam addition from the crystallizer  465  may be negative, i.e., steam is sent as excess to the crystallizer  465  for other uses (e.g., as a heat source for the stripper  470 ). 
         [0190]    The Stage #2 output  440  has the volume of waste water reduced from the input  420  with the salts more concentrated to approximately 36% TDS, which is increased from the initial approximately 27% TDS in the exemplary waste water at the input  420 . 
         [0191]    Referring to  FIG. 15  (Stage #3), the brine water progresses from the input  440  to the output  460  successively through a pump  441 , a preheater  442 , a condenser  443 , and a flash evaporator  445 . One alternative is to have, in place of a single preheater  442 , a series of preheaters or heat exchangers. The heating medium for the preheater  442  can be excess steam available from a crystallizer  465  (see  FIG. 16 ) and/or hot water from the condenser  443 . 
         [0192]    In this example, the pump  441 , preheater  442 , and condenser  443  elevate the waste water pressure to 400 psia and the temperature to 445° F. at the inlet  446  to the flash evaporator  445  without use of any heater elements between the condenser  443  and flash evaporator  445 . The pump  441  elevates the pressure from 15 psia to 400 psia. The preheater  442  elevates the temperature from 212° F. to 273° F., while the condenser  442  further elevates the temperature to 445° F. Additionally, the preheater  442  produces distilled water at outlet  447 . 
         [0193]    One aspect of Stage #3 of  FIG. 15  is, as shown in the legend to the right of the flash evaporator  445 , that it is operated so the flash pressure, i.e., the downstream or output pressure of the flash evaporator  445 , is approximately 15 psia, contrasting with the input or upstream pressure of 400. The effect of this change in the pressure is that a larger portion of the water component of the waste water is separated from the dissolved solids in the form of steam. The remaining waste water becomes more concentrated in dissolved solids and exits the flash evaporator at outlet  460 . 
         [0194]    The condenser  443  receives some saturated steam directly from the crystallizer  465  of  FIG. 16  at line  466  which, with the preheater  442  elevating the waste water temperature from 212° F. to 273° F. before the condenser  443 , provides waste water at 445° F. from the condenser  443  and, favorably, there no need for the presence or operation of the heater  444 . In the exemplary system, the elevation in temperature is the effect of steam from the steam output  466  of the crystallizer subsystem  465  of  FIG. 16 . That steam continues to the condenser  443  and the preheater  442  until it exits the preheater  442  at line  447  as distilled water. Under certain operating conditions, the steam addition from the crystallizer  465  may be negative, i.e., steam is sent as excess to the crystallizer  465  for other uses (e.g., as a heat source for the stripper  470 ). 
         [0195]    The Stage #3 output  340  has the volume of waste water reduced from the input  440  with the salts more concentrated to approximately 48% TDS, which is increased from the initial approximately 36% TDS in the exemplary waste water at the input  420 . 
         [0196]    The exemplary system includes multiple (three) concentration stages ( FIGS. 13-15 ) that are substantially alike in the combination of equipment used. However, other exemplary systems with multiple concentration stages may have individual stages of more varied combinations of equipment without departing from the spirit and scope of the present invention. 
         [0197]    The level of pressurization of waste water in all stages is such that there is no boiling (nucleate or other type) of the waste water inside and across the heat exchanger surfaces of the condensers and preheaters of each stage. This prevents the formation of deposits (scales, fouling, etc.) on the heat exchanger surfaces and reduces the requirement for cleaning of the heat exchangers. This results in the reduction of the operating cost. 
         [0198]      FIG. 16  represents an example of applying the output brine water (line  460 ) of the Stage #3 treatment ( FIG. 15 ) to a plasma crystallizer  465 . The plasma crystallizer  465  is an example of a known pyrolytic reactor that can be used to finish separation of water from salts dissolved in it. One skilled in the relevant art will appreciate, however, that other thermal reactors may also be used without departing from the spirit and scope of the present invention. The example of a plasma reactor, which can be consistent with known plasma gasification/vitrification reactors, operated with one or more plasma torches  467 , as is well-known in published literature, is believed to provide opportunity for a favorable cost-benefit ratio. 
         [0199]    In general, for multistage operation, the plasma crystallizer  465  (or other reactor) is utilized at the final concentration stage when the output brine water has been concentrated to a desired level, as described in the above example. It can also be suitable to have a multistage system not only for salts concentration (as in  FIGS. 13-15 ), but also a separation subsystem with a reactor after any individual one of the early concentration stages (e.g., after either, or both, of Stages #1 and #2). However, it is generally more cost effective to have a single separation subsystem after the last of a determined number of concentration stages for the desired separation. 
         [0200]    In general, any thermal reactor may be used to separate the salts and the water. A reactor operated to produce disposable salts (referred to herein as a “crystallizer”) is generally suitable. Where the salts have toxicity, it may be desirable to operate the reactor in a manner so they are vitrified or made into glass. Accordingly, any reference to a crystallizer herein can also include a vitrifier. 
         [0201]    As shown in  FIG. 16 , the crystallizer  465  has a salts output at an outlet  468  equivalent to the total salts content of the original wastewater. The water output of the total system is now recovered as clean distilled water from the preheaters  402 ,  422 ,  442  of the respective Stages of  FIGS. 13-15 , and/or may also be recovered directly from steam exiting the crystallizer  465 . 
         [0202]      FIG. 16  shows brine water  460  entering the crystallizer  465  via a pump  480  that raises the pressure to 665 psia.  FIG. 16  also shows how steam from the crystallizer  465  can be redirected back to the respective earlier Stages of  FIGS. 13-15 . The steam output from the crystallizer  465  at line  466  may be provided back to the various Stages #1, #2 and #3 and used for heating by the respective preheaters and condensers therein. Also,  FIG. 16  shows an “Excess Steam to Stripper” of a certain amount at line  469 . This steam  469  is used in a stripper  470  which is utilized to remove volatile organic compounds (“VOCs”) from the waste water before processing. Some excess steam from the crystallizer  465  may also be used for other purposes, e.g., to preheat the input waste water in a preheater or condenser. 
         [0203]    Before treatment in the Stages shown in  FIGS. 13-15 , the incoming waste water  10  can be, for example, sent to the stripper  470  where the steam  469  is used to remove VOCs from the waste water  10 . The excess steam  469  can be used directly in the stripper  470 , as shown in  FIG. 16 , or used to heat air in a separate heat exchanger where the heated air is then used in the stripper to remove the VOCs. The stripped waste water is sent as feed to the input  400  to Stage #1 of  FIG. 13 . The VOCs which are removed from the waste water  10  exit the stripper through a conduit  477  which connects to the plasma crystallizer  465 . Additionally or alternatively, a condenser with a knock-out pot (not shown) can be used between the plasma crystallizer  465  and the stripper  470  with the condensed VOCs (as well as any stripped VOCs) fed directly to the plasma crystallizer  465 . The VOCs are fed in front of the plasma torch  467  (e.g., along with brine water  460  from Stage #3 from the pump  480 ) such that they intensely mix with the high temperature gases exiting from the plasma torch  467 . The plasma torch  467  is operated using appropriate gas (e.g., air, oxygen, hydrogen, etc.) that will aid in, or result in, the complete destruction of the VOCs. The VOCs are substantially converted to carbon dioxide and steam. The heat generated by this conversion of VOCs to carbon dioxide and steam is utilized in the plasma crystallizer  465 , along with heat inputted through the plasma torch  467 , to vaporize the water from the brine water  460 . This reduces the amount of heat and the corresponding amount of electricity utilized in the plasma crystallizer  465 , thus increasing its cost effectiveness. 
         [0204]    The steam exiting the plasma crystallizer  465  can be periodically vented to the atmosphere (not shown) to keep the levels of non-condensable gases low enough such that they do not degrade the performance of the heat exchangers used in the inventive system and process. 
         [0205]      FIG. 16  also shows some steam from the flash evaporators  405 ,  425 ,  445  of concentration Stages #1, #2 and #3 at an input  472  goes to a compressor  475  that elevates the steam to a pressure of 665 psia and a temperature of 500° F. to be recycled as part of the steam that goes back to the treatment Stages of  FIGS. 13-15 . 
         [0206]    It is therefore seen that systems and processes in accordance with the still further embodiment of the present invention can make use of known and available components, such as, for example, flash evaporators for concentration of salts and plasma (or other) gasifier reactors for crystallization (or vitrification) of the salts, in particular innovative ways with insight as to both the capital cost and the operating cost. A need for such cost effective water treatment has been heightened by practices such as the use of large amounts of water in natural gas drilling However, the present invention may be used in any situation where impurities to be removed exist. 
         [0207]    In general summary, but without limitation, the still further embodiment of the present invention can be characterized in the following ways, for example: A system, and a corresponding method, in which waste water is supplied to one or more stages of equipment including a pump for pressurizing the water (e.g., to about 400 psia), a preheater that heats the pressurized waste water well above normal boiling temperature, a condenser that effects further heating of the pressurized waste water, a flash evaporator, or other device, that receives the heated, pressurized waste water and results in fluid evaporation and concentration of solids that were in the waste water. In for example, instances in which the waste (brine) water with concentrated solids cannot be otherwise readily and safely disposed of, a thermal or pyrolytic reactor is provided to crystallize or otherwise yield a form of the solids that can be readily and safely disposed of. In one form, such a reactor may also be applied as a heater for the original incoming waste water. Also, or alternatively, such a reactor may be used to form a vitrified glass of the salts output of any water treatment system that produces a brine water. 
         [0208]    Furthermore, the examples described herein show how use can be made of flash evaporators operated at a considerable difference of upstream pressure (e.g., 400 psia) and downstream pressure (e.g., 15 psia). To do so, the pyrolytic reactor of the inventive system is operated at a significantly higher pressure than is usual for such equipment (e.g., a plasma crystallizer operated at a pressure of 665 psia and steam developed in the reactor is supplied directly to the condensers of the earlier salts concentration Stages). All of which is believed to contribute significantly to reduced operating costs which can be very beneficial, even though initial capital costs may be increased. 
         [0209]      FIGS. 17-20  illustrate another embodiment of the present invention.  FIGS. 17, 18 and 19  will be individually discussed, but first their general relation to each other in an exemplary multi-stage system (here with three stages) will be described. 
         [0210]    Each of the  FIGS. 17-20 , merely by way of further example and without limitation, are described in this specification, and include legends, including numerical values (all of which are merely representative approximations and are not necessarily exact technical values and/or calculations). Further, these legends are not necessarily the only suitable values that represent the nature and characteristics of materials as applied to, affected by, and resulting from the operations of the exemplary system(s). Not all such legends will be repeated in this text, although all form a part of this disclosure and are believed understandable to persons of ordinary skill in water treatment and thermal processes. As appreciated by one skilled in the art, such data are sometimes referred to as heat and material balances. It is specifically to be understood and will be appreciated by one skilled in the art that the various values indicated in the legends may have a tolerance of ±20%, as they are representative approximations and not exact technical values. 
         [0211]    A separate batch of wastewater  500  is supplied to each of the inlets  510   a ,  510   b , and  510   c  of  FIGS. 17-19 , respectively. Each Stage heats and pressurizes the waste water that is then supplied to a single flash evaporator  515   a ,  515   b  and  515   c , respectively. The flash evaporators  515   a ,  515   b  and  515   c  have brine water outputs, at an outlet  530   a ,  530   b  and  530   c , respectively, that is combined into a single output  530  from wastewater to each of the inputs  510   a ,  510   b  and  510   c.    
         [0212]    Referring to  FIGS. 17, 18 and 19 , which represent Stages #1A, #1B and #1C, respectively, each batch of waste water progresses from the input  510   a ,  510   b ,  510   c  to the output  530   a ,  530   b ,  530   c  successively through a pump  511   a ,  511   b ,  511   c , a preheater  512   a ,  512   b ,  512   c , a condenser  513   a ,  513   b ,  513   c , and a flash evaporator  515   a ,  515   b ,  515   c . One alternative is to have, in place of a single preheater  512   a ,  512   b ,  512   c , a series of preheaters or heat exchangers. The heating medium for the preheater  512   a ,  512   b ,  512   c  can be excess steam available from a crystallizer  565  (see  FIG. 20 ) and/or hot water from the condenser  513   a ,  513   b ,  513   c.    
         [0213]    For convenience, when referring to the same element in the various Stages, the reference letters a-c will be omitted and only the reference number will be used. It is to be understood that the element referred to is the same element in all three Stages. 
         [0214]    Referring to  FIGS. 17-19 , the pump  511 , preheater  512 , and condenser  513  elevate the waste water pressure to 400 psia and the temperature to 445° F. at the inlet  506  to the flash evaporator  515  without use of any heater elements between the condenser  513  and flash evaporator  515 . The pump  511  elevates the pressure from 14.7 psia (1 atm) to 400 psia. The level of pressurization of waste water in all stages is such that there is no boiling of the waste water inside and across the heat exchanger surfaces of all heat exchangers used in this system. This is done to prevent the formation of deposits (scales, fouling, etc.) on the heat exchanger surfaces. The preheater  512  elevates the temperature from 60° F. to 199° F., while the condenser  513  further elevates the temperature to 445° F. Additionally, the preheater  512  produces distilled water at outlet  507 . 
         [0215]    For drawing convenience, each concentration Stage ( FIGS. 17-19 ) shows a heater  514  (e.g., heater  514   a  in  FIG. 17 , heater  514   b  in  FIG. 18 , heater  514   c  in  FIG. 19 ) between the condenser and flash evaporator, which may be omitted entirely or, if present, not supplied with any heating fluid. As shown in  FIGS. 17-19 , the heater  514  has zero input and zero output of heating fluid (e.g., DowTherm™). For system equipment economy, the heater  514  is preferably omitted. However, systems may be arranged as shown and provide the option to operate or to not operate such a heater  514 . Further explanation of what enables avoiding use of a heater  514  is given below. 
         [0216]    One aspect of Stages #1A, #1B and #1C of  FIGS. 17, 18 and 19  is, as shown in the legend to the right of the flash evaporator  515 , that it is operated so the flash pressure, i.e., the downstream or output pressure of the flash evaporator  515 , is approximately 15 psia, contrasting with the input or upstream pressure of 400 psia. The effect of this change in the pressure is that a larger portion of the water component of the waste water is separated from the dissolved solids in the form of steam. The remaining waste water becomes more concentrated in dissolved solids and exits the flash evaporator at outlet  530 . 
         [0217]    The condenser  513  receives some saturated steam directly from the crystallizer  565  of  FIG. 20  at line  566  which, with the preheater  512  elevating the waste water temperature from 60° F. to 199° F. before the condenser  513 , provides waste water at 445° F. from the condenser  513  and, favorably, there no need for the presence or operation of the additional heater  514 . In the exemplary system, the elevation in temperature is the effect of steam from the steam output  566  of the crystallizer subsystem  565  of  FIG. 20 . That steam continues to the condenser  513  and the preheater  512  until it exits the preheater  512  at line  507  as distilled water. Under certain operating conditions, the steam addition from the crystallizer  565  may be negative, i.e., steam is sent as excess to the crystallizer  565  for other uses (e.g., as a heat source for the stripper  570 ). 
         [0218]    The output  530  of the various parallel Stages has the volume of waste water reduced from the input  510  with the salts more concentrated to a brine water to approximately 27% TDS, which is increased from the initial approximately 20% TDS in the exemplary waste water at the input  510 . 
         [0219]    In each of  FIGS. 17-19 , it is shown the individual stages outputs  530   a ,  530   b ,  530   c  of the system&#39;s single flash evaporator  515   a ,  515   b ,  515   c , respectively, are equal. The combined inputs  510   a ,  510   b ,  510   c  to the treatment stages make up 6000 lbs/hr, including salts of 1200 lbs/hr. The brine water outputs  530   a ,  530   b ,  530   c  of the single flash evaporators  515   a ,  515   b ,  515   c , respectively, include each stage&#39;s output which are combined (as shown in  FIG. 20  as conduit  530 ), equals a total of 4491 lbs/hr, which includes the 1200 lbs/hr of salts in the three inputs  510   a ,  510   b ,  510   c . The salts are now 27% of each Stage and of the total outputs in Total Dissolved Solids (“TDS”), compared to just 20% at the inputs. 
         [0220]    The exemplary system includes multiple (three) concentration stages ( FIGS. 17-19 ) that are substantially alike in the combination of equipment used. However, other exemplary systems with multiple concentration stages may have individual stages of more varied combinations of equipment without departing from the spirit and scope of the present invention. 
         [0221]    The level of pressurization of waste water in all stages is such that there is no boiling (nucleate or other type) of the waste water inside and across the heat exchanger surfaces of the condensers and preheaters of each stage. This prevents the formation of deposits (scales, fouling, etc.) on the heat exchanger surfaces and reduces the requirement for cleaning of the heat exchangers. This results in the reduction of the operating cost. 
         [0222]      FIG. 20  represents an example of applying the output brine water (line  530  with the combined individual outputs  530   a ,  530   b ,  530   c ) of the single flash evaporators  515   a ,  515   b ,  515   c , respectively, of the concentration Stages #1A, #1B, #1C to a plasma crystallizer  565 . The plasma crystallizer  565  is an example of a known pyrolytic reactor that can be used to finish separation of water from salts dissolved in it. One skilled in the relevant art will appreciate, however, that other thermal reactors may also be used without departing from the spirit and scope of the present invention. The example of a plasma reactor, which can be consistent with known plasma gasification/vitrification reactors, operated with one or more plasma torches  567 , as is well-known in published literature, is believed to provide opportunity for a favorable cost-benefit ratio. 
         [0223]    The exemplary arrangement shown in  FIGS. 17-20  uses a single plasma crystallizer  565 , as well as a multiple flash evaporators  515   a ,  515   b ,  515   c , for any number of parallel waste water flows (which are of equal volume and content in the illustrated example, but can vary from each other). Alternatively the multiple flash evaporators  515   a ,  515   b ,  515   c  may be replaced by a single flash evaporator. The size and cost of equipment can, at least in some instances, be favorable for use of a combination of multiple pressurizing and heating elements and a single concentration element. 
         [0224]    In general, any thermal reactor may be used to separate the salts and the water. A reactor operated to produce disposable salts (referred to herein as a “crystallizer”) is generally suitable. Where the salts have toxicity, it may be desirable to operate the reactor in a manner so they are vitrified or made into glass. Accordingly, any reference to a crystallizer herein can also include a vitrifier. 
         [0225]    As shown in  FIG. 20 , the crystallizer  565  has a salts output at an outlet  568  equivalent to the total salts content of the original wastewater. The water output of the total system is now recovered as clean distilled water from the preheaters  512   a ,  512   b ,  512   c  of the respective parallel Stages of  FIGS. 17-19 , and/or may also be recovered directly from steam exiting the crystallizer  565 . 
         [0226]      FIG. 20  shows brine water  530  entering the crystallizer  565  via a pump  580  that raises the pressure to 665 psia.  FIG. 20  also shows how steam from the crystallizer  565  can be redirected back to the respective earlier Stages of  FIGS. 17-19 . The steam output from the crystallizer  565  at line  566  may be provided back to the various Stages #1A, #1B, #1C and used for heating by the respective preheaters and condensers therein. Also,  FIG. 20  shows an “Excess Steam to Stripper” of a certain amount at line  569 . This steam  569  is used in a stripper  570  which is utilized to remove volatile organic compounds (“VOCs”) from the waste water before processing. Some excess steam from the crystallizer  565  may also be used for other purposes, e.g., to preheat the input waste water in a preheater or condenser. 
         [0227]    Before treatment in the Stages shown in  FIGS. 17-19 , the incoming waste water  10  can be, for example, sent to the stripper  570  where the steam  569  is used to remove VOCs from the waste water  10 .  FIG. 20  shows steam  569  developed from concentration Stages #1A, #1B, #1C at an input  572  joined at a junction  573  with exiting steam from the crystallizer  565  that has been reduced in pressure by expansion in a mechanical vapor turbine  575  to recover energy and reduce the total amount of energy used in the process. The excess steam  569  can be used directly in the stripper  570 , as shown in  FIG. 20 , or used to heat air in a separate heat exchanger where the heated air is then used in the stripper to remove the VOCs. The stripped waste water  500  is sent as feed to the inputs  510   a ,  510   b ,  510   c  of Stages #1A, #1B, #1C, respectively, as shown in  FIGS. 17-19 . The VOCs which are removed from the waste water  10  exit the stripper through a conduit  577  which connects to the plasma crystallizer  565 . Additionally or alternatively, a condenser with a knock-out pot (not shown) can be used between the plasma crystallizer  565  and the stripper  570  with the condensed VOCs (as well as any stripped VOCs) fed directly to the plasma crystallizer  565 . The VOCs are fed in front of the plasma torch  567  (e.g., along with brine water  530  from the pump  580 ) such that they intensely mix with the high temperature gases exiting from the plasma torch  567 . The plasma torch  567  is operated using appropriate gas (e.g., air, oxygen, hydrogen, etc.) that will aid in, or result in, the complete destruction of the VOCs. The VOCs are substantially converted to carbon dioxide and steam. The heat generated by this conversion of VOCs to carbon dioxide and steam is utilized in the plasma crystallizer  565 , along with heat inputted through the plasma torch  567 , to vaporize the water from the brine water  560 . This reduces the amount of heat and the corresponding amount of electricity utilized in the plasma crystallizer  465 , thus increasing its cost effectiveness. 
         [0228]    The steam exiting the plasma crystallizer  565  can be periodically vented to the atmosphere (not shown) to keep the levels of non-condensable gases low enough such that they do not degrade the performance of the heat exchangers used in the inventive system and process. 
         [0229]    It is therefore seen that systems and processes in accordance with the another embodiment of the present invention can make use of known and available components, such as, for example, flash evaporators for concentration of salts and plasma (or other) gasifier reactors for crystallization (or vitrification) of the salts, in particular innovative ways with insight as to both the capital cost and the operating cost. A need for such cost effective water treatment has been heightened by practices such as the use of large amounts of water in natural gas drilling However, the present invention may be used in any situation where impurities to be removed exist. 
         [0230]    In general summary, but without limitation, the another embodiment of the present invention can be characterized in the following ways, for example: A system, and a corresponding method, in which waste water is supplied to one or more stages of equipment including a pump for pressurizing the water (e.g., about 400 psia), a preheater that heats the pressurized waste water well above normal boiling temperature, a condenser that effects further heating of the pressurized waste water, a single, or plural, flash evaporator(s), or other concentration device(s), that receives the heated, pressurized water flows from multiple parallel stages of pressurizing and heating elements and results in fluid evaporation and concentration of solids that were in the waste water. In, for example, instances in which the waste (brine) water with concentrated solids cannot be otherwise readily and safely disposed of, a thermal or pyrolytic reactor is provided to crystallize or otherwise yield a form of the solids that can be readily and safely disposed of. In one form, such a reactor may also be applied as a heater for the original incoming wastewater. Also, or alternatively, such a reactor may be used to form a vitrified glass of the salts output of any water treatment system that produces a brine water. 
         [0231]    The examples described herein show how use can be made of a single flash evaporator receiving multiple heated and pressurized flows of waste water with the concentrated output of the flash evaporator subjected to final separation of salts and water in a single reactor. 
         [0232]    It will be apparent to those skilled in the art that numerous modifications and variations of the described examples and embodiments are possible in light of the above teachings of the disclosure. The disclosed examples and embodiments are presented for purposes of illustration only. Other alternate embodiments may include some or all of the features disclosed herein. Therefore, it is the intent to cover all such modifications and alternate embodiments as may come within the true scope of this invention, which is to be given the full breadth thereof. Additionally, the disclosure of a range of values is a disclosure of every numerical value within that range.