Patent Publication Number: US-2009223882-A1

Title: Dual-Train Wastewater Reclamation and Treatment System

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
     The present application claims priority co-pending non-provisional application entitled “Dual-Train Wastewater Reclamation and Treatment System”, Ser. No. 11/276,880, filed by inventors Randall J. Jones and Stephen P. Markle on Mar. 17, 2006, which claimed priority to then co-pending United States provisional patent application entitled “Advanced Oxidation System For Wastewater Treatment,” having Ser. No. 60/665,736, filed by inventor Randall Jones on Mar. 28, 2005, and then co-pending United States provisional patent application entitled “Dual-Train Wastewater Reclamation and Treatment System,” having Ser. No. 60/777,520, filed by inventors Randall J. Jones and Stephen P. Markle on Feb. 24, 2006, all of which are entirely incorporated herein by reference. 
    
    
     BACKGROUND OF THE INVENTION 
     1. Field of the Invention 
     The present invention relates generally to wastewater treatment systems, and more particularly wastewater treatment systems where holding large volumes of sludge for later disposal is difficult. As such, this invention particularly relates to waste water treatment for ships, off-shore structures and platforms other large transportation vehicles, mobile/portable treatment systems (i.e., military support, disaster relief, etc.), remote treatment systems (i.e. highway rest stops, campgrounds, etc.), industrial wastewater treatment, food processing, dairy and other light industrial wastewater treatment applications. 
     2. Discussion of the Related Art 
     Land-based wastewater treatment solutions tend to occupy relatively large spaces to effectuate wastewater treatment. Space, however, is a premium on transportation vehicles (like cruise ships), mobile treatment systems (such as used in military support), and remote treatment systems (like campgrounds), as well as other similarly situated treatment scenarios. 
     Ordinarily, wastewater systems combine blackwater and graywater prior to treatment. Blackwater and graywater, however, are very different in terms of chemical makeup (composition, viscosity), volume, perception by passengers and crew, and treatment under the law. For example, blackwater must be treated to a higher standard in most operating areas. Most ships are fitted with vacuum flush systems with blackwater pollutant concentrations much greater than those found in graywater. Shipboard water production, storage and management necessitates costly infrastructure. 
     Shipboard wastewater systems are typically based on biological treatment. While biological based systems can work, biological systems are complicated to operate, have a large footprint in terms of tankage and deck space, are susceptible to periodic chemical upsets, can be expensive to operate due to costs of chemicals, require provisioning of these chemicals, have long start-up times (order of days) and produce large amounts of sludge. 
     Finally, discharge of wastewater is regulated. Compliance with regulations can be difficult and may require holding volumes of wastewater for days to complete Biochemical Oxygen Demand (BOD) testing and other compliance testing. If the treated wastewater ultimately fails compliance testing, the process must be continued, which results in lost time and requires larger holding tanks. 
     Wastewater treatment systems have been disclosed in the following United States or foreign patents: U.S. Pat. No. 3,822,786 (Marschall), U.S. Pat. No. 3,945,918 (Kirk), U.S. Pat. No. 4,053,399 (Donnelly et al.), U.S. Pat. No. 4,072,613 (Alig), U.S. Pat. No. 4,156,648 (Kuepper), U.S. Pat. No. 4,197,200 (Alig), U.S. Pat. No. 4,214,887 (van Gelder), U.S. Pat. No. 4,233,152 (Hill et al.), U.S. Pat. No. 4,255,262 (O&#39;Cheskey et al.), U.S. Pat. No. 4,961,857 (Ottengraf et al.), U.S. Pat. No. 5,053,140 (Hurst), U.S. Pat. No. 5,178,755 (LaCrosse), U.S. Pat. No. 5,180,499 (Hinson et al.), U.S. Pat. No. 5,256,299 (Wang et al.), U.S. Pat. No. 5,308,480 (Hinson et al.), U.S. Pat. No. 6,811,705 (Puetter), EPO 261822 (Garrett), WO 93/24413 (Hinson) and U.S. Pat. No. 6,195,825 (Jones). None of these references, however, disclose the aspects of the current invention. 
     What is needed is a wastewater treatment system that has a small footprint, produces dischargeable effluent minutes after startup, requires virtually no chemical additions, is simple to operate, minimizes sludge production from biological activity, is constructed of the most durable components, and produces a high quality effluent exceeding most stringent effluent requirements day-after-day. What is also needed is a wastewater treatment system that can treat the same volume of wastewater in a smaller space and/or in faster time than currently existing systems to reduce the space occupied by holding tanks and treatment equipment. 
     What is also needed is a system that can accurately predict treatment compliance results to enable more efficient and predictable compliance success. 
     SUMMARY OF THE INVENTION 
     The invention is summarized below only for purposes of introducing embodiments of the invention. The ultimate scope of the invention is to be limited only to the claims that follow the specification. 
     Generally, the present invention is incorporated in an integrated, split treatment system that treats blackwater for compliance and sludge reduction and treats graywater for reuse, blending and compliance (referred herein as the “dual-train water reclamation and treatment system” or “treatment system”). For blackwater, the treatment system incorporates five general phases (or zones): (1) screening, (2) clarifying, (3) filtering, (4) advanced oxidation, and (5) sludge reducing. For graywater, the treatment system incorporates three general phases (or zones): (1) screening (2) filtering, and (3) advanced oxidation. Each train of the treatment system (blackwater and graywater) can operate as a stand-alone system or can be assimilated into an integrated treatment train for both graywater and blackwater. This system is particularly useful in today&#39;s restrictive regulatory environment. 
     One advantage of the treatment system is the ability to treat blackwater differently from graywater. Reuse of graywater is becoming more socially acceptable; blackwater reuse is not. Moreover, reuse of reclaimed sewage also bears the risk to human health associated with equipment failure. 
     Another advantage of the treatment system is that it reduces the space needed for wastewater treatment, and space is a premium for mobile units like cruise ships and other aquatic vessels. The system is compact in size, simple in design, inexpensive to operate, built for long term reliable operation in the marine environment, hatchable, and modular in construction affording ease of tailoring with selection of correct number of standardized modules. 
     Another advantage of the water reclamation and treatment system is the use of turbidity, UV transmittance and ORP readings to predict final BOD levels for compliance or non-compliance in advance of the compliance test results to enable a more predictable and efficient treatment. In addition, it affords reach-back, real-time monitoring of effluent quality. 
     Another advantage of the water reclamation and treatment system is the ability to handle wastewater that lacks predictable levels of contamination and pH. Ferries or military vessels may wait for many hours, days, weeks, or even months between heavy loading events. This type of varied influent can greatly affect a biological based treatment system. Among other things, a varied influent causes a lengthy period of limited effectiveness while biological colonies reform. Unlike the biological systems in use in many of these applications, varied influent does not affect the water reclamation and treatment system. In this case, the treatment system immediately reacts and begins treatment without regard to effluent strength or pH. In addition, biological treatment systems typically require a fixed amount of time (1-2 weeks) to establish a viable colony for wastewater treatment. In this case, the water reclamation and treatment system begins treating wastewater immediately after system startup. 
     The description of the invention that follows, together with the accompanying drawings, should not be construed as limiting the invention to the example shown and described, because those skilled in the art to which this invention pertains will be able to devise other forms thereof within the ambit of the appended claims. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         FIG. 1  illustrates an embodiment of an integrated water reclamation and treatment system  10 . 
         FIG. 2  is a flow chart that reflects an embodiment of a blackwater treatment train  100 . 
         FIG. 3  a flow chart that reflects an embodiment of a graywater treatment train  200 . 
         FIG. 4  illustrates an embodiment of a blackwater clarifying zone  120  and a sludge reduction zone  170 . 
         FIG. 5  illustrates an embodiment of a stirred reactor  300 . 
         FIG. 6  illustrates an embodiment footprint/plan for a 20-gpm blackwater treatment train  100 . 
         FIG. 7  illustrates an embodiment footprint/plan for a 30-gpm blackwater treatment train  100 . 
         FIG. 8  illustrates an embodiment footprint/plan for a 25-gpm graywater treatment train  200 . 
         FIG. 9  illustrates an embodiment footprint/plan for a 100-gpm graywater treatment train  200 . 
         FIG. 10  illustrates an embodiment of the modularity of the system  10 . 
         FIG. 11  is a flow chart that reflects an embodiment of an alternate blackwater treatment train  100 . 
         FIG. 12  is a flow chart that illustrates a functional diagram of flow zones of the system. 
     
    
    
     DESCRIPTION OF PREFERRED EMBODIMENT 
     The descriptions below are merely illustrative of the presently preferred embodiments of the invention and no limitations are intended to the detail of construction or design herein shown other than as defined in the appended claims. In this specification, the term “graywater” refers to discarded liquid from sources such as deck drains, lavatories, showers, dishwashers, laundries, drinking fountains and potentially equipment cooling water. “Graywater” does not include industrial wastes, infectious wastes, human body wastes, and animal waste. In this specification, the term “blackwater” refers to sources such as wastes of human origin from water closets (toilets), urinals, and medical facilities transported by the ships soiled drain system (a/k/a sewage). It also includes animal wastes from spaces containing live animals. When graywater is combined with blackwater, the waste stream is characterized as blackwater. In this specification, the term “technical water” includes water for laundry, flushing water, cooling water, vehicle wash, etc. In this specification, the term “advanced oxidation” refers to a process that typically involves the generation and use of the hydroxyl free radical (OH − ) as a strong oxidant to destroy compounds that cannot be oxidized by conventional oxidants such as oxygen, ozone, and chlorine. 
     General Design Overview 
     The water reclamation and treatment system  10  splits treatment into a blackwater treatment train  100  and a graywater treatment train  200 . By splitting the treatment of blackwater and graywater, the treatment system can reclaim graywater for reuse. Reusing graywater offers several advantages. Among other things, reusing graywater (1) reduces fresh water making requirement/consumption, (2) reduces plant operating costs, (3) reduces tankage requirement (and ultimately the treatment footprint), (4) reduces ship propulsion plant costs by reduced ship displacement resulting from smaller tankage requirements, (5) protects the environment, and (6) reduces the volume of wastewater needing to undergo blackwater treatment. 
     The graywater and blackwater treatment trains differ in arrangement due to the unique differences of the influent treated. The principle difference is the location where filtration occurs. In graywater trains, filtration preferably occurs prior to advanced oxidation. In blackwater trains, filtration preferably depends on the level of total suspended solids (TSS). For blackwater with TSS less than 500 parts per million (PPM), filtration preferably occurs post-advanced oxidation. For blackwater with TSS greater than 500 parts per million (PPM), filtration preferably occurs prior to advanced oxidation. 
       FIG. 1  provides an example embodiment of an integrated dual train system designed for shipboard use. Of course, the system shown in  FIGS. 1-12  could be adapted for other uses (such as land-based uses) as well as other wastewater volumes and loading conditions.  FIG. 12  illustrates the four principle zones of the water reclamation and treatment system  10 . Whether as an integrated system or as a standalone system, the water reclamation and treatment system  10  comprises: a solids separation zone, a filtration zone, and an advanced oxidation zone, with the option of adding a sludge reduction zone. 
     Preferred Blackwater Treatment Train 
     The blackwater treatment train  100  can be used as a standalone system to treat wastewater. Alternatively, the blackwater treatment train  100  can be used as a retrofit to enhance existing systems. As illustrated in  FIG. 1 , the blackwater treatment train  100  can treat raw wastewater or wastewater first treated by an existing bioreactor. 
     As shown in  FIGS. 1 and 2 , a first influent  102  enters the blackwater treatment train  100 . Typically, this occurs directly from an installed blackwater collection system by way of a positive displacement pump. Alternatively, the first influent could enter from existing bioreactors. Initially, the first influent  102  enters a blackwater solids separation zone  108 . While there are many ways to achieve a solids separation zone, it is preferred that the blackwater solids separation zone  108  further comprises a blackwater screening zone  110  and a clarifying zone  120 . 
     The blackwater screening zone  110  performs initial solids separation. It is preferred that the blackwater screening zone  110  utilizes a 200-micron mesh rotary sieve  111  for initial solid separation. Screened effluent  112  can be held in an aerated equalization tank  114 . Screened solids from the rotary sieve  111  are directed to either thermal destruction device or to the sludge reduction zone  170  (discussed below). 
     The first influent  102  comprises traditional blackwater sources, but could also include other sources. For example, in shipboard designs, it is preferred to include galley wastewater (sinks and grinders) as part of the first influent  102 . In such cases, it is preferred that galley wastewater enter the blackwater treatment train  100  after first being directed through grease traps. Sources such as galley wastewater can be added directly to the aerated equalization tank  114  as shown in  FIG. 1 . 
     Next, blackwater screening zone effluent  118  is pumped to a clarifying zone  120 . A preferred embodiment of the clarifying zone  120  is shown in  FIG. 4 . It is preferred that the clarifying zone  120  include a macerating pump  121 , a flocculator  122 , a clarifier, an air dissolving pump  130  and a blackwater intermediate tank  135 . The macerating pump  121  helps homogenize the incoming feed to an optimum particle size compatible with the clarifier. An example of a macerator pump  121  is Barnes model number DGV2042L. An example of an air-dissolving pump  130  is made by Nukini, model M25NPD-15Z. It is preferred that the air-dissolving pump  130  stream a small amount of air into the wastewater as the wastewater passes through the flocculator  122 . 
     While many types of clarifiers are available, the preferred clarifier is a stainless steel hydraulic-lift dissolved air flotation device having a cone-shaped top, which is referred to in this specification as a hydraulic separator  129 . Effluent from the flocculator  122  flows into the hydraulic separator  129  at the inlet  128 . Air from the air-dissolving pump  130  is streamed through diffusers  134 . When released from the pipe diffusers  134 , dissolved air forms very fine bubbles that move upwards. This imparts an upward velocity to the fluid. As this air contacts solid material it tends to agglomerate onto its surface imparting a positive buoyant force. This combination of upward fluid velocity and positive buoyancy floats solids to the surface where they are removed at specific intervals to the sludge reduction tank  172 . It is also preferred to add a solution of aluminum chlorohydrate by a dosing pump to attain an optimum concentration (roughly 30 ppm), which will assist flocculation and floatation of solids. 
     Closing outlet valve  132  permits liquid wastewater that continues to flow through inlet  128  to raise the liquid wastewater level in the hydraulic separator  129 . Ultimately, the liquid wastewater level will rise to the point that it force the separated sludge  126  (for this specification, the term “separated sludge” also includes water from the top of the hydraulic separator  129 ) into the inverted cone region at the top of the hydraulic separator  129 . When the level is sufficiently high, separated sludge  126  (which has formed a floating blanket) is directed through the outfall pipe located at the top of the hydraulic separator  129  into the sludge reduction tank  172 . It is preferred to keep the separated sludge in a liquid, flowable state so that it will flow without need for mechanical means. With a flowable separated sludge and having the top of the hydraulic separator  129  higher than the sludge reduction tank  172  inlet and normal operating level, sludge flows by gravity into the sludge reduction tank  172 . 
     The sludge reduction tank  172  is segmented into two regions by a baffle plate  171 . The baffle is oriented to form a barrier at the top of the tank and open at the bottom allowing communication between the two tank regions. One side of the baffle plate  171  forms a sludge reduction region  173  and the other side of the baffle plate  171  forms an uptake region  175 . Separated sludge  126  from the hydraulic separator  129  enters the sludge reduction region  173  of the sludge reduction tank  172  near the top of the vessel. Separated sludge  126 , so introduced, will retain its buoyancy and tend to rise to the top of the tank; while liquid is displaced downward. Clarified water, which can pass under the baffle plate  171  collects in the uptake region  175  before flowing by gravity into the blackwater intermediate tank  135 . 
     Ozonated finishing tank effluent  182  can be introduced into the sludge reduction tank  172 , preferably in the sludge reduction region  173  in sufficient quantity to oxidize the odoriferous material. A simple smell test works here. The sludge reduction tank  172  treats sludge through advanced oxidation, with sludge characteristics transformed by ozonation and oxidation. This substantially reduces sludge volume by oxidation to carbon dioxide gas, water and other materials. In addition, the sludge reduction tank  172  promotes solid and liquid separation. This step also further clarifies the sludge mixture, forcing clarified water downward in the device, around the baffle and into the clarified water uptake region  175 . As additional sludge enters the sludge reduction tank  172  from the hydraulic separator  129 , an equal amount of sludge reduction tank  172  clarified water flows under the baffle and into the uptake region  175 . When the water level reaches the uptake outfall  177 , it is directed to the blackwater intermediate tank  135 . 
     The preferred sludge reduction tank  172  is cylindrical in shape. For separated sludge  126  flow rates of 0.5 gpm, the preferred sludge reduction tank would be approximately 8 feet tall and 3 feet in diameter, having a total ozonated volume of approximately 320 gallons, and providing a total retention time of 10 hours. In addition, the preferred baffle plate  171  is a flat plate that is positioned within the cylindrical tank as a chord, running from inside wall to inside wall of the sludge reduction tank  172 . 
     Reacted sludge  174  is directed to an onboard disposal system for thermal destruction or held for overboard discharge at-sea or pumped ashore. Unlike most, if not all, sludge burning incinerators in use today, which suffer from odor problems from incineration of odiferous sludge from bioreactors, the sludge reduction zone  170  removes virtually all odors from the reacted sludge  174 , making it suitable for destruction by thermal devices. 
     When the outlet valve  132  is open, clarified water  124  flows into the blackwater intermediate tank  135 . Likewise sludge reduction tank  172  clarified water  176  from the sludge reduction zone  170  also flows into the blackwater intermediate tank  135  and mixes with the clarified water  124 . 
     Clarification zone effluent  138  proceeds to a blackwater filtration zone  160 . It is preferred that the blackwater filtration zone  160  comprises blackwater ultrafilters  162  and a blackwater flush tank  164 . It is preferred that the blackwater ultrafilters  162  be pressure fed external plate and frame ultrafiltration membranes, such as the Pleiade Series manufactured by Novasep Orelis. This membrane system has approximately 753 square feet (70 square meters) of surface area/module, and can process up to 26.5 gallons-per-minute (6 m 3 /hr) per module. System capacity may be increased by adding additional modules. The blackwater ultrafilters  162  should be periodically flushed with water produced by the blackwater ultrafilters  162  and stored in the blackwater flush tank  164 . 
     Blackwater retentate  192 , comprised of solids and other material that did not pass through the blackwater ultrafilters  162 , is directed to the sludge reduction zone  170  for treatment, or bioreactor if installed. Blackwater permeate (i.e., effluent from the filters)  190  is directed to a blackwater advanced oxidation zone  140 . 
     It is preferred that the blackwater advanced oxidation zone  140  comprises an ozone generator  180 , at least one, but preferably two blackwater stirred reactors  142 ,  144 , a blackwater disinfecting zone  150  and a finishing tank  154 . Prior to entering a stirred reactor, it is preferred to infuse blackwater permeate  190  with ozone. Ozone can be produced in a blackwater ozone generation zone  180  from ship service oil free compressed air. Many different ozone generators could work. For example, the 240-g/hr ozone generator sold by Pacific Ozone, Model R-SGA642, is preferred for treating 30 gpm flows of blackwater. The ozone can be dissolved into a pressurized stream of blackwater finishing tank effluent  156  for circulation to the blackwater stirred reactors  142 ,  144  and the sludge reduction tank  172 . 
     The preferred design of the blackwater stirred reactors  142 ,  144  is shown in  FIG. 5 . It is preferred to have blackwater stirred reactors  142 ,  144  arranged in series. Within each blackwater stirred reactor  142 ,  144 , neutrally buoyant media  310  provide sufficient surface area for the interaction and oxidation of dissolved ozone and soluble and insoluble organic material. For treating 30 gpm flows, it is preferred to size each blackwater stirred reactor  142 ,  144  to provide at least 11 minutes of residence time for the ozone oxidation reaction to occur. 
     Next, blackwater stirred reactor effluent  146  is directed to a blackwater disinfection zone  150  and treated with ultraviolet light. Ultraviolet radiation is advantageous because it damages the genetic structure of bacteria, viruses, and parasites, making them incapable of reproducing and/or killing them. In addition, ultraviolet radiation removes ozone. It is preferred that the blackwater disinfection zone  150  comprises a UV unit  152 . It is preferred to use a medium pressure, high intensity UV unit  152  that produces polychromatic light for destruction of residual organic material, and disinfection. An example of such a unit is the Hyde Marine Model QMD100B1. The UV unit  152  can feature an automatic cleaning wiper, which can be controlled by the control system  450 . The UV unit  152  also transforms any residual ozone into fast reacting species, such as hydrogen peroxide and hydroxyl radicals further consuming any residual organic carbon based material. In addition, the destruction of residual ozone through this process allows for post-membrane filtration with ultra filtration where such filters would not ordinarily tolerate ozone-enriched water without damage. UV treated water is then directed to the finishing tank  154 . 
     Ozone infused water in the finishing tank  154  is recirculated back to the stirred reactors and UV unit until the level in the finishing tank  154  reaches a predetermined level. Blackwater finishing tank effluent  157  is then either pumped directly overboard if compliant, or pumped to onboard ship storage tanks for eventual discharge. 
     Blackwater finishing tank effluent  157  is typically colorless and odorless since ozone reaction with wastewater removes color and odors. This phenomenon is unique and important since most other technologies used for treating wastewater such as bioreactors or membrane-bioreactors do not consistently produce effluent of this visual and olfactory quality. 
     The use of gravity separation after grinding in this application is unique owing to the sludge reduction capabilities of the sludge holding and sludge reduction tank  172 . This allows the system to be operated in remote environments where sludge limitations and disposal are major obstacles to system operation and standard treatment methods would be undesirable in part due to quantities of sludge produced 
     Alternate Embodiment of Blackwater Treatment Train 
     Alternatively, the blackwater filtration zone  160  could be moved from its location prior to the blackwater advanced oxidation zone  140  and after the clarification zone  120  to after the blackwater stirred reaction zone  140  as shown in  FIG. 11 . This alternate blackwater treatment train is preferred when the total suspended solids (TSS) is less than 500 parts per million. 
     Preferred Graywater Treatment Train 
     The graywater treatment train  200  can be used as a standalone system to treat and reuse graywater or discharge all or part of the treated graywater. It is preferred to use the same component design for any graywater treatment train component that has a counterpart in the blackwater treatment train and vice versa. The blackwater treatment train  100  and graywater treatment train  200 , however, are separate treatment trains and wastewater is not comingled between the two trains other than where expressly stated. In other words, the two treatment trains share only component design; they do not physically share components. 
     As shown in  FIGS. 1 and 3 , a second influent  202  enters the graywater treatment train  200 . Typically, the second influent  202  first enters a graywater solids separation zone  208 . While there are many ways to achieve a solids separation zone, it is preferred to employ a screening zone  210  after being pumped from a graywater holding tank (not shown). Preferably, the graywater screening zone  210  includes a resiliently mounted shaker screen  212  where separation of larger material occurs. The screen is mounted on an equalization tank  215 . Screened solids  216  collected from the graywater screening zone  210  are directed to the sludge reduction zone  170 . 
     Next, the graywater screening zone effluent  218  is directed from equalization tank  215  to a graywater filtration zone  220 . It is preferred that the graywater filtration zone  220  include pre-filters  222  graywater ultrafilters  226 , a backwash tank  224  and a graywater intermediate tank  235 . 
     The pre-filters  222  are preferably skid mounted, stainless steel vessels. The pre-filters  222  house polyethylene filter sleeves that will remove particulate material, reducing suspended solids and oil/grease in the graywater stream. The redundant nature of the configuration ensures an uninterrupted flow of filtered water to the graywater ultrafilters  226 . The system self-cleans using its own filtered water. In the preferred embodiment, the pre-filters  222  are sized to remove particulate larger than 5 micron in size, filters with this capability are available from Wastewater Resources, Inc, model number AQM  30 . 
     Next, pre-filter effluent  223  is directed to the graywater ultrafilters  222 . The graywater ultrafilters  222  preferably use 20-nanometer ceramic membranes such as those manufactured by the Novasep Orelis company of Lyon, France. When using ceramic membranes, surface wash water is preferably ozonated and it is preferred not to use chlorine. The preferred source of ozonated surface wash water is from the graywater finishing tank  254 . A pH neutralization chemical is preferred to adjust the pH of the reclaim water to a pH of 7.5. For a 25-gpm design, it is expected that between 50 and 80 gallons per month of pH neutralizer will be required, volume is dependent upon pH of influent graywater. 
     Alternatively, the graywater filters  222  can use 20-nanometer polysulfone synthetic membranes, such as those manufactured by Wastewater Resources, Inc., model number PC1140. When using polysulfone synthetic membranes (the alternative ultrafilter embodiment), it is preferred to add chlorine to the backwash water for disinfection of the modules. If polysulfone synthetic membranes are used, it is preferred to add a backwash tank  224  as shown in  FIG. 3 . Chlorine use for the backwash tank  224  should not exceed 20 gallons per month for a 25-gpm system. A pH neutralization chemical is also preferred hereto adjust the pH of the reclaim water to a pH of 7.5. It is expected that between 50 and 80 gallons per month of pH neutralizer will be required, volume is dependent upon pH of influent graywater. 
     For a 25-gpm design using polysulfone synthetic membranes (the alternative ultrafilter embodiment), a 94-gallon backwash tank  224  constructed from ¼-inch polypropylene, such as the one manufactured by Navalis Environmental Systems, LLC, model number TK24-007-01, is preferred. For a 25-gpm design using polysulfone synthetic membranes (the alternative ultrafilter embodiment), the membranes are each 12-in in diameter and 36-in in height with 1,140 ft 2  of surface area. The process is designed to filter particles in the range of 0.02 to 0.04 microns at up to 130 degrees F. with particulate loading not to exceed 750 ppm. This will allow for backwashing at 24 to 30 minute intervals for two minutes. When using polysulfone synthetic membranes (the alternative ultrafilter embodiment), water for the backwash tank  224  is preferred from the graywater finishing tank  254 . 
     Graywater filter permeate  227  is collected in the graywater intermediate tank  235 . Graywater intermediate tank effluent  238  proceeds to a graywater advanced oxidation zone  240 . It is preferred that the graywater advanced oxidation zone  240  comprise an ozone generator  280 , at least one, but preferably two graywater stirred reactors  242 ,  244 , a graywater disinfecting zone  250  and a graywater finishing tank  254 . Prior to entering a graywater stirred reactor, it is preferred to infuse intermediate tank effluent  238  with ozone. Ozone can be produced in a graywater ozone generation zone  280  from ship service oil free compressed air. Many different ozone generators could work. For example, the 120-g/hr ozone generator sold by Pacific Ozone, Model R-SGA442, is preferred for treating 100 gpm flows of graywater. The ozone can be dissolved into a pressurized stream of graywater finishing tank effluent  256  for circulation to the graywater stirred reactors  240 ,  242 . A second graywater finishing tank effluent  258  can be directed to the graywater backwash tank  224  in the alternative ultrafilter embodiment that uses polysulfone ultrafilters. 
     The preferred design of the graywater stirred reactors  242 ,  244  is shown in  FIG. 5 . It is preferred to have graywater stirred reactors  242 ,  244  arranged in series. Within each graywater stirred reactor  242 ,  244 , neutrally buoyant media  310  provide sufficient surface area for the interaction and oxidation of dissolved ozone and soluble and insoluble organic material. It is preferred to size each graywater stirred reactor  242 ,  244  to provide at least 5 minutes of residence time for the ozone oxidation reaction to occur. 
     Stirred reactor effluent  246  proceeds to a graywater disinfection zone  250  and disinfected with ultraviolet light. It is preferred that the graywater disinfection zone  250  comprises a UV unit  252 . It is also preferred to use a medium pressure, high intensity UV unit  252  that produces polychromatic light for destruction of residual organic material, and disinfection. An example of such a unit is the Hyde Marine QMD100B1. The UV unit  252  can feature an automatic cleaning wiper (as controlled by the control system  450 ). The UV unit  252  also transforms any residual ozone into fast reacting species, such as hydrogen peroxide and hydroxyl radicals further consuming any residual carbon based material. 
     Graywater finishing tank effluent  290  may be reused  292  (e.g., directed back to laundry feed tanks for reuse as reclaimed technical water), blended  294  with graywater screening zone effluent  218 , or discharged  296  where regulations permit. The graywater finishing tank  254  also serves as source water of backwash for the backwash tank  224 . 
     Graywater retentate  228  from the graywater filtration zone  220  can be directed to the blackwater sludge reduction zone  170 . Alternatively, graywater retentate  228  could be directed to a ships graywater transfer system (not shown). 
     Preferred Stirred Reactor 
       FIG. 5  illustrates the preferred stirred reactor  300 . It is preferred to use the stirred reactor  300  for the blackwater stirred reactors  142 ,  144  and the graywater stirred reactors  242 ,  244 . Referring to  FIG. 5 , the stirred reactor  300  comprises two cylindrically shaped chambers: a cylindrical acceleration chamber  302  and a fluidized media chamber  304 . The two chambers are mounted coaxially with respect to each other (i.e., one inside the other). Two washer-shaped perforated plates  306  on either end cap the fluidized media chamber  304 . One perforated plate is mounted near the top of the stirred reactor  300  and the other near the bottom. The volume between the perforated plates  306  houses fluidized media  310 . These upper and lower perforated plates  306  hold the fluidized media  310  in place and away from inlet and outlet ports. It is preferred that the perforations be sized to allow maximum flow while retaining the fluidized media  310  between perforated plates  306 . 
     The cylindrical acceleration chamber  302  is smaller in cross section and mounted between the perforated plates  306 . The preferred stirred reactor  300  has inlet ports  308  and outlet ports  309  for admitting and exhausting the liquid. At the top of the stirred reactor  300 , a mixer  312  with a shaft  314  containing multiple blades  316  passes down though the cylindrical acceleration chamber  302 . The mixer  312  moves fluid in the cylindrical acceleration chamber  302  down and out to the fluidized media chamber  304  through the bottom perforated plate  306 . Ozone enriched fluids react with dissolved ozone and tiny, outgassed ozone bubbles which have formed on the fluidized bed, walls of the chamber, and float freely within the chamber. This enhanced oxidation reactor allows for advanced treatment in a small space. 
     The preferred stirred reactor  300  is for a 100-gpm graywater or 30-gpm blackwater treatment train is constructed from 316 stainless steel, approximately 3 feet diameter, 8 feet tall, having a fluidized media chamber  304  volume of 282 gallons and a combined inside/outside chamber volume of 423 gallons. Thus, it is preferred that the fluidized media chamber  304  be about ⅔ of the size of the combined inside/outside chamber volume. 
     The preferred stirred reactor  300  is for a 25-gpm graywater and 10 gpm blackwater treatment train is constructed from 316 stainless steel, approximately 2 feet diameter, 5 feet tall, having a fluidized media chamber  304  volume of 79 gallons and a combined inside/outside chamber volume of 118 gallons. 
     The stirred reactor  300  can be used alone, in series or in parallel.  FIG. 1  illustrates two stirred reactors  300  connected in series. When connected in series, the outlet port  309  of one stirred reactor  300  can be connected to the series inlet port  308  if the second stirred reactor  300 . 
     The design of the advanced ozone reactor chambers and their incorporation of fluidized media held in place by perforated plates allows the process to reach maximum oxidation efficiency in order to meet modern standards. Earlier use of ozone in other designs limits the effectiveness of the process and may fail to meet these more stringent standards. 
     System Modularity 
     The treatment system  10  is expandable by design. It is preferred to construct a treatment system  10  from a standard family of 24-inch and 36-inch diameter tanks. The 24 and 36 inch families are directed to retrofit design applications. In addition,  FIG. 10  discloses an embodiment of a forward-fit blackwater component design. In a forward-fit design (i.e., new construction projects), larger diameter tanks can be more easily assimilated into the ship or other structure than in the typical retrofit situation. In this way, system treatment capacity is a function of the number of modular system components selected. Specific advantages of this design flexibility include:
         1. System capacity is related to residence time in the reactor vessels. The 100-gpm graywater treatment system shares common stirred reactor, tank, pumps and system component (with exception of ultrafiltration units) designs and materials with the 30-gpm blackwater treatment system.   2. System components are mounted on either 28-inch or 40-inch stainless steel squares that afford ease of mounting on ship foundations.   3. System blocks can be arranged in a variety of configurations to optimally use the space available, from a very compact square to open linear based on available footprint.   4. Ease of rigging to the designated system compartment:
           24-inch diameter system components fit through a 28″×28″ square or 40″ (1 meter) round opening   36-inch diameter system components fit through a 40″×40″ square or 57″ (1.5 meter) round opening   
           5. The arrangement enables design for easy access to areas requiring routine maintenance.   6. The system is designed for growth. The modular nature of its components enables ease of expansion. For example, the capacity of the 25-gpm Graywater System could easily be increased by addition of a filter module, and if necessary an additional reactor.       

     An illustration of the building block nature of system capacity and inherent flexibility are provided in  FIGS. 6-10 . 
     Example: 25 gpm Graywater Embodiment 
     As previously noted, the water reclamation and treatment system  10  can operate as a stand-alone system or as part or a more comprehensive treatment train. The following sections describe examples of how the treatment system  10  could be incorporated into different treatment trains. These examples should not be construed, however, as limiting the invention to the example shown and described, because those skilled in the art to which this invention pertains will be able to devise other forms thereof within the scope of the disclosure set forth herein. 
     While a treatment system can be designed to meet existing conditions and need, the following section summarizes an embodiment of the treatment system sized to treat 25-gpm of graywater. A plan/footprint of this embodiment is shown in  FIG. 8 . Referring now to  FIG. 8 , a first modular group  400  and a second modular group  410  of modules house the treatment system. The first modular group  400  comprises two rows of five modules, where each module is 28-inches square and constructed from stainless steel. The second modular group  410  comprises one module 28-inches by 41-inches. The modular sizing shown in this embodiment will permit a total footprint of 54 square feet. 
     This modular design can be arranged in a variety of configurations to optimally use the space available. The modular design enables ease of expansion. For example, the capacity of the 25-gpm system could easily be increased by addition of a filter module, and if necessary an additional stirred reactor. System components are mounted on 28-inch stainless steel squares that afford ease of mounting on ships foundations, and make a variety of configurations possible; from a very compact square to open linear. For ship use, each component preferably fits through a 28-inch opening for ease of rigging to the designated system compartment. Further, the arrangement allows for easy access to areas requiring routine maintenance. Other modular embodiments are shown in  FIGS. 6 ,  7 , and  9 . 
     It is preferred that the treatment system be fully automated and capable of remote control. It is preferred to use a control system  450 , such as an Allen Bradley Programmable Logic Controller (PLC). The control system  450  can interface with most ship interior communication and control systems providing system status where desired throughout the ship. The control system  450  can alert operational staff to issues requiring intervention. The control system  450  can also be configured for reach-back monitoring of system performance off ship through the addition of networking components such as modems or ethernet connections. This permits operators of the system to monitor and solve operational issues as they arise. 
     In this example, treatment system components are preferably fabricated from 316 Stainless Steel and should be impervious to ozone. System tanks are preferably constructed from ¼-inch 316 Stainless Steel. Internal piping should be press fit 316 Stainless Steel or CPVC for the filter assembly only. 
     In this example, the graywater screening zone  210  uses a shaker screen manufactured by Midwestern Industries, model Gyra-Vib MR 24 and a shaker tank manufactured by Navalis Environmental Systems, LLC (“Navalis”), model number TK24-008-01; graywater ultrafilters  222  manufactured by Wastewater Resources, Inc., model number PC1140; graywater intermediate tank  235  manufactured by Navalis, model number TK24-001-01; graywater stirred reactors  242 ,  244  manufactured by Navalis, model number TK24-003-01; UV unit  252  manufactured by Hyde Marine, model number QMD100B1; a graywater finishing tank manufactured by Navalis, model number TK24-002-01; graywater backwash tank  224  manufactured by Navalis, model number TK24-007-01; ozone generator  280  manufactured by Pacific Ozone, model number SGA 24 (60 g/hr); control system  450  manufactured by Navalis model number CP-GW-25; 30-gpm Process Pump manufactured by Nikuni, model number M40NP; 50-gpm Transfer Pump manufactured by Gould model number 11ASH262DO; 50-gpm Filter Charging Pump manufactured by Gould, model number 4SH2E2CO; 100-gpm Filter Backwash Pump manufactured by Gould, model number 8SH2H2CO; Ambient Ozone Monitor/Alarm/Shutdown manufactured by IN USA, model number IN-2000-L2-LC. 
     It has been found that during normal operation of the treatment system, a system sized to handle 25-gpm of graywater operated in the order of 18 hours a day can reclaim 100 m3/day of graywater for reuse. 
     Elevated ORP Reading and Relationship to Turbidity 
     The water reclamation and treatment system  10  will produce an effluent with elevated ORP (oxygen reduction potential) and a lowered turbidity when in regulatory compliance as a by-product of its design. The recirculation of final effluent through a stirred reactor  300  and subsequently UV light in the disinfection zone allows the process to be measured through ORP and turbidity scales. Both of these effects can be measured and quantified by digital instruments currently available. The preferred instruments are George Fischer digital ORP meter and transmitter, and the HACH 1720E digital Turbidimeter. These instruments yield a 4-20 ma output that can be monitored from the 450 (Program Logic Controller), which controls overall system operations. 
     The regulatory environment for discharge of treated wastewater into the ocean varies from location to location around the world. Typically Total Suspended Solids (TSS), Biochemical Oxygen Demand (BOD) and Fecal Coliform are the primary constituents regulated. TSS may be measured directly and immediately, during, and after treatment with existing instrumentation. Both Fecal Coliform and BOD require sampling and laboratory testing after waiting for a specified period of time. Thus wastewater treatment operators must wait the specified period of time before learning whether the treated wastewater has been sufficiently treated to have permitted discharge. At least in part because of distrust in technology prior to this invention, some operators have been known to hold effluent until reaching water outside of regulatory restrictions—even when using in a certified, properly functioning treatment device. As a result, real time effluent quality monitoring for these two constituents is not currently achievable, creating uncertainty as to the real-time continuous quality of effluent from wastewater treatment. 
     For example, United States 33 Code of Federal Regulations Part 159 subpart E establishes perhaps the most restrictive treated wastewater effluent discharge standards in the world today. Applying to cruise vessels when in certain waters of the State of Alaska, these ships must meet effluent quality standards of not more than 30 milligrams per liter TSS, 20 colony forming units per 100 milliliters Fecal Coliform and 30 milligrams per liter BOD. Typically ships with marine sanitation devices certified to meet these standards as a result of testing are permitted to discharge in these waters. However, spot-checking of ships by the State of Alaska has revealed that numerous ships are out of compliance even though they are operating certified systems, and they are prevented from further discharge until corrective action is accomplished. The causes for failure are numerous, but lack of real-time effluent monitoring capability has prevented instantaneous recognition of out-of-compliant system operation so that action might be taken to cease discharging. 
     Given that a properly sized and properly functioning UV unit operating in water of acceptable UV transmittance characteristics will effectively destroy or reduce to acceptable levels harmful bacteria, including the regulated Fecal Coliform, we have found that measuring ORP and turbidity of treated wastewater as soon as immediately after treatment can be used to forecast BOD. Measurable indication of BOD treatment compliance effectiveness at the time of discharge and displayed through the PLC control center  450  is now possible because both ORP and turbidity can be monitored immediately after treatment. Thus, to reduce the uncertainty of treatment compliance time for wastewater, it is preferred to take the following steps: (1) obtain a sample of effluent from a wastewater treatment train, (2) measure Turbidity, and (3) Measure Oxidation Reduction Potential (ORP), and (4) comparing that to pre-determined levels based on site-specific regulations. 
     Continuous monitoring of ORP and Turbidity through installed measurement devices connected to the PLC control center  450  indicates BOD levels within the effluent in real time. Indication of BOD (30 milligrams per liter) concentration compliance with 33CF159 subpart E requirement is provided if ORP is greater than 200 mV and turbidity is less than 3 NTU. Compliance with the international standard specified in International Convention for the Prevention of Ships Annex IV at 50 milligrams per liter is also indicated by ORP being greater than 200 mV and turbidity less than 3 NTU. This gives the operator an accurate active indication of compliance with modern standards not available through another means. Other BOD regulatory criteria can be achieved in a similar manner on a case-by-case basis. 
     This unique relationship takes into account both the visible (suspended solids) and the invisible (dissolved organics) through the use of turbidity, UV transmittance, and ORP. While the exact relationship between measured UV Transmittance and BOD not yet known, it is expected that testing would shown it to be a critical parameter that will be of more use than turbidity to predict BOD compliance. 
     Visible organics will register in higher turbidity and dissolved organics will register in lower transmittance and reduced ORP levels. Biological treatment systems that do not use advanced oxidation lack the necessary water chemistry to utilize this ratio and therefore cannot be monitored for compliance in real time. The use of the oxidation reaction in the configuration listed yield ORP levels that are high enough to affect a readable ratio. Previous attempts at this type of oxidation did not yield a readable, repeatable ratio because the levels, if they were observed, were not high enough to affect a ratio. Since the readings are both digital and inferred electronically, effluent quality data can then be easily transmitted from ship to shore for off ship effluent quality monitoring and system troubleshooting. 
     An alternate method for predicting BOD levels would be to recreate the unique advanced oxidation water chemistry by injecting ozone or other oxidizer into the stream at the appropriate location, expose to UV light, measure ORP and turbidity levels. 
     Although the invention has been described in detail with reference to one or more particular preferred embodiments, persons possessing ordinary skill in the art to which this invention pertains will appreciate that various modifications and enhancements may be made without departing from the spirit and scope of the claims that follow.