Abstract:
A method and system for collecting gaseous nitrogen compounds into an aqueous solution are provided. The method enables the combination of gaseous sulfur and nitrogen compounds in the aqueous solution to generate ammonium compound components, to include ammonium sulfate. Sulfur may be pressure injected into the solution as gaseous sulfur dioxide. Optionally, carbon may be introduced into the solution as gaseous carbon dioxide. The sulfur may be earlier sourced by a burning of a sulfurous solid. The pH of the solution may be monitored and the introduction of ammonia, carbon and/or sulfur may be halted or constrained while the pH of the solution is measured outside of specified range. The solution may be allowed to age to permit a mix of compounds of ammonium carbonate, ammonium bicarbonate and ammonium carbomate to restabilize and thereby encourage a renewed surge of ammonium sulfate generation.

Description:
CO-PENDING PATENT APPLICATION 
       [0001]    This Nonprovisional Patent Application is a Continuation-in-Part Application to Nonprovisional patent application Ser. No. 14/076,529 filed on Nov. 11, 2013 and titled “PROCESS AND APPARATUS FOR CAPTURING GASEOUS AMMONIA”. Nonprovisional Patent Application Ser. No. 14/076,529 is hereby incorporated by reference in its entirety and for all purposes, to include claiming benefit of the priority date of filing of Nonprovisional patent application Ser. No. 14/076,529. 
     
    
     FIELD OF THE INVENTION 
       [0002]    The present invention generally relates to the remediation of areas and materials that are present undesirable levels of nitrogen compounds, ammonia and/or ammonium compounds. More particularly, the present invention is directed to capturing gaseous ammonia in an aqueous solution by precipitation and conversion into a non-volatile ammoniacal salts. 
       BACKGROUND OF THE INVENTION 
       [0003]    The subject matter discussed in the background section should not be assumed to be prior art merely as a result of its mention in the background section. Similarly, a problem mentioned in the background section or associated with the subject matter of the background section should not be assumed to have been previously recognized in the prior art. The subject matter in the background section merely represents different approaches, which in and of themselves may also be inventions. 
         [0004]    Various natural processes, agricultural activities and sewage treatment operations generate outputs that include nitrogen compounds, ammonium compounds and ammonia, wherein the ammonia is generated in a gaseous state and/or out-gasses at ambient temperatures. Factory farming of livestock, offered as one example of a relevant industrialized agricultural activity that often generates excessive levels of nitrogen compounds and ammonia gas, is increasingly drawing attention as a source of nitrogen compounds pollution of soil, water and air. It is noted that both mammalian dung and avian feces contain nitrogen compounds that can contribute to pollution of the natural environment. Sewage treatment plants are also generally tasked with reducing or eliminating human contribution to nitrogen compounds pollution of the environment. In an additional area relevant to certain applications of the present invention, sites of drug and chemical manufacture can be contaminated by ammonia gas and other compounds containing nitrogen. 
         [0005]    The prior art provides methods of capturing ammonia by generating concentrated sulfuric acid solutions and transporting the concentrated acidic solution to a site where a target gaseous ammonia is located. The concentrated sulfuric acidic solution sulfuric is then mixed with a water volume to create an acid bath that is exposed to the target ammonia. This prior art method includes several short comings, not the least of which are the costs of handling and transportation and the risk of metal contamination of the concentrated sulfuric acid solution during storage and transit. 
         [0006]    Yet the prior art fails to provide optimal methods and systems that enable the extraction of nitrogen from gaseous ammonia and ammonium compounds present in outputs of many widely practiced industrial and agricultural systems. 
         [0007]    There is therefore a long-felt need to provide a method and apparatus that enable the collection of nitrogen compounds from laboratory facilities, industrial sites and agricultural operations. 
       OBJECTS OF THE INVENTION 
       [0008]    It is an object of the method of the present invention (hereinafter, “the invented method”) to remove gaseous ammonia from a site atmosphere by introducing sulfur dioxide as a solute to acidify an aqueous solution, wherein the sulfur dioxide is generated by burning sulfur on-site, and whereby the resultant acidic aqueous solution absorbs the gaseous ammonia and generates resultant chemical compounds that capture nitrogen from nitrogen compounds. 
         [0009]    It is an optional object of the invented to generate ammonium sulfate as a resultant compound of interaction sponsored within the acidic aqueous solution as a result of absorption of ammonia by the aqueous solution, and optionally absorbing carbon dioxide, from the site atmosphere. 
         [0010]    It is an additional optional object of the invented method to absorb ammonia and optionally absorbing carbon dioxide in the acidic aqueous solution, wherein the ammonia and the carbon dioxide is generated by bacterial processing of organic waste matter. 
         [0011]    It is a still additional optional object of the invented to generate ammonium sulfate as a resultant chemical compound of interaction of the acidic aqueous solution with ammonia, wherein the ammonia is generated by bacterial processing of organic waste matter. 
       SUMMARY 
       [0012]    Toward these and other objects that are made obvious in light of the present disclosure, an, organic ammonium sulfate product is produced by aerobically composting a source of nitrogen, such as animal waste or manure mixed with a carbon source to create a biomass having a high solids content, through highly selective aerobic bacteria action without addition of external heat. Preferably, the production process includes the steps of providing a composting apparatus located inside a composting building such as a barn, a shed, or a greenhouse, housing a composting trench; placing the animal waste or manure preferably collected from a CAFOs facility in said composting trench; mixing said animal waste or manure with a source of carbon to form a biomass having a high solids content; providing aerobic bacteria and supplying said aerobic bacteria with water and oxygen in sufficient amounts to highly selectively convert the waste amino acids, proteins, uric acid and any other available nitrogen compounds from the biomass into NH 3  and/or NH 4  and CO 2  without addition of external heat; moving said biomass down the composting trench as the aerobic composting process progresses; capturing the NH 3  and/or NH 4  and CO 2  from the atmosphere of the composting apparatus in an aqueous solution; adding a source of sulfate to said aqueous solution containing captured NH 3  and/or NH 4  and CO 2 , and processing said aqueous solution containing a source of sulfate and captured NH 3  and/or NH 4  and CO 2  to obtain ammonium polycarbonate and/or solid or concentrated liquid ammonium sulfate product. Preferably, the obtained ammonium sulfate product is certifiable as organic. 
         [0013]    Certain alternate preferred embodiments of invented method and an invented apparatus enable the extraction of nitrogen from gaseous ammonia by the application of sulfur dioxide generated by burning sulfur. In an optional aspect of the invented method, gaseous ammonia is introduced into an acidic aqueous solution and ammonium sulfate is produced from the resulting aqueous solution. Sulfur and/or sulfur dioxide may be introduced into the aqueous solution to further acidify the aqueous solution and sponsor the production of ammonium sulfate. Optionally of additionally, carbon and/or carbon dioxide may be introduced into the aqueous solution to further sponsor the production of ammonium sulfate. 
         [0014]    In a first application of the invented method, a volume of source air that comprises gaseous ammonia is introduced into an aqueous solution containing sulfur dioxide. The source air containing the ammonia gas may optionally simply be introduced into the water volume without filtering out of any constituents and/or without any significant or intended chemical processing. 
         [0015]    In another optional aspect of the invented method, the internal atmosphere of an enclosed structure containing ammonia gas and optionally carbon dioxide is at least partially scrubbed of the ammonia gas by exposing the enclosed internal atmosphere to an acidic aqueous solution. The aqueous solution preferably comprises sulfur dioxide generated by burning sulfur in the presence of oxygen. The acidified aqueous solution having received the sulfur dioxide then is exposed to gaseous ammonia to sponsor the production of chemical compounds within the aqueous solution whereby gaseous ammonia and nitrogen compounds are removed from the internal atmosphere. Ammonium sulfate may be produced as a resultant compound in certain alternate preferred embodiments of the invented method. 
         [0016]    In another optional aspect of the invented method, an enclosure is established at a site contaminated with a solid or liquid source material, wherein the source material contains ammonium compounds and emits gaseous ammonia. The enclosure may be a portable structure that is temporarily erected as the instant site and may be successively redeployed at alternate locations. Emission of ammonia gas may be facilitated or accelerated by aerating the source material, e.g., mechanically tilling solid source material, or churning a liquid source material with ambient air containing oxygen. A resultant acceleration of gaseous ammonia production by disturbance and/or introduction of oxygen into the source material may be effected by the organic function of bacteria present or seeded within the source material. 
         [0017]    In yet another optional aspect of the invented method, the pH of the aqueous solution may be monitored and the introduction of ammonia, sulfur dioxide and/or carbon dioxide may be halted while the pH is measured outside of a prespecified range, e.g., a range of preferably from approximately 4.0 to 5.0, or alternately a range of from 3.0 to 6.0. 
         [0018]    In a still additional optional aspect of the invented method, ammonium sulfate is filtered out and/or extracted from the aqueous solution and optionally provided for or used as an agricultural fertilizer. The ammonium sulfate may be removed from the aqueous solution as a concentrated solution or in combination with a portion of the aqueous solution. 
         [0019]    In an even other optional aspect of the invented method, gaseous sulfur dioxide is pressure injected and/or infused into the aqueous solution to sponsor formation of solid ammonium sulfate, other precipitates, and/or chemical components. 
         [0020]    In another optional aspect of the invented method, components are removed from the aqueous solution and the resultant water is reused in a following cycle of scrubbing gaseous ammonia from an enclosed atmosphere and/or ammonium sulfate generation. 
         [0021]    In a still other optional aspect of the invented method, the aqueous solution may be allowed to age to permit a mix of compounds within the aqueous solution, including but not limited to ammonium carbonate, ammonium bicarbonate and ammonium carbomate, to rebalance and thereby sponsor a renewed surge of ammonium sulfate generation. 
         [0022]    This Summary and Objects of the Invention is provided to introduce a selection of concepts in a simplified form that are further described below in the Detailed Description. This Summary is not intended to identify key features or essential features of the claimed subject matter, nor is it intended to be used to limit the scope of the claimed subject matter. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0023]    These, and further features of the invention, may be better understood with reference to the accompanying specification and drawings depicting the preferred embodiment, in which: 
           [0024]      FIG. 1A  is a process chart comprising aspects of the invented method; 
           [0025]      FIG. 1B  is a block diagram of a first preferred embodiment of the invented apparatus (hereinafter, “first system”) coupled with a gaseous ammonia source, the first system comprising a reaction chamber holding a water volume, an ammonia gas scrubber module coupled with the reaction chamber and the gaseous ammonia source, a sulfur dioxide module coupled with the reaction chamber and providing sulfur dioxide to the water volume, and a combined reverse osmosis module and electro dialysis coupled with the reaction chamber; 
           [0026]      FIG. 1C  is a block diagram of a second preferred embodiment of the invented apparatus (hereinafter, “second system”) coupled with a gaseous ammonia source, the second system comprising the first system and an agitator module coupled with a source material, the agitator module adapted to encourage production of gaseous ammonia by the gaseous ammonia source; 
           [0027]      FIG. 1D  is a block diagram a first preferred embodiment of the of the ammonia gas scrubber module of  FIG. 1B ; 
           [0028]      FIG. 1E  is a block diagram of a first preferred embodiment of the sulfur dioxide module of  FIG. 1B ; 
           [0029]      FIG. 1F  is a block diagram a first preferred embodiment of the combined reverse osmosis module and electro dialysis of  FIG. 1B ; 
           [0030]      FIG. 2  is a flow chart of a first preferred embodiment of the invented method (hereinafter, “first method”) that may be implemented by the first system of  FIG. 1B  and having optional aspects that may be implemented by the second system of  FIG. 1C ; 
           [0031]      FIG. 3  is a cut-away top view of the first system adapted to decontaminate an internal volume of air of a substantively enclosed and contaminated structure, wherein the enclosed air includes gaseous ammonia; 
           [0032]      FIG. 4  is a cut-away side view of the first system adapted to remediate a liquid spill, wherein a portable tent source enclosure is placed above and around the liquid spill and an air pump is placed and positioned to pump air into the liquid source material in order to sponsor an accelerated production of source ammonia from the liquid spill by bacterial action; 
           [0033]      FIG. 5  is an example of the first system enclosing an accumulation of a substantively solid source material that emits ammonia gas, wherein the first system is augmented with a rototiller applied to agitate the solid source material and accelerate the production and capturing of gaseous ammonia; 
           [0034]      FIG. 6  is a schematic diagram of an optional internal control system of the first system of  FIG. 1A  with optional modules that extend control to the second system of  FIG. 1B ; 
           [0035]      FIG. 7  is a schematic diagram of a controlled power distribution network of the control system of the first system of  FIG. 1A  and including optional elements of the second system of  FIG. 1B ; 
           [0036]      FIG. 8  is a cut-away view of elements of the first system of  FIG. 1  that direct gaseous ammonia from the enclosure of the source material and to delivery within the reaction chamber; 
           [0037]      FIG. 9  is a cut-away view of the distribution system for sulfur dioxide within the reaction chamber of the first system of  FIG. 1 ; 
           [0038]      FIG. 10  is a block diagram of a third alternate preferred embodiment of the present invention (hereinafter, “third system”) wherein a source of pressurized carbon dioxide is provided and is adapted to deliver gaseous carbon dioxide into the water volume and within the reaction chamber of the first system of  FIG. 1 ; 
           [0039]      FIG. 11  is a cut-away view of the distribution system for carbon dioxide within the reaction chamber of the third system of  FIG. 11 ; 
           [0040]      FIG. 12  is an illustration of a fifth motorized embodiment of the first system of  FIG. 1B ; 
           [0041]      FIG. 13  is an illustration of a carbon dioxide generation module that accepts mammalian exhalation a source of gaseous carbon dioxide as coupled with the third system of  FIG. 10 ; 
           [0042]      FIG. 14  is an alternate sixth preferred embodiment of the invented method showing process outline comprising aspects of the invented method; 
           [0043]      FIG. 15  is a schematic diagram of equipment and structures comprising an optional preferred setup of a production facility enabled for implementation of the sixth preferred embodiment of the invented method of  FIG. 14 ; 
           [0044]      FIG. 16  presents optional aspects and features of certain alternate preferred embodiments of the invented composting apparatus, wherein ammonia gas is produced by highly selective aerobic bacteria action without requiring an addition of external heat energy beyond available ambient heat energy 
           [0045]      FIG. 17  is a perspective view of a composting apparatus in accordance with a seventh preferred embodiment of the present invention; 
           [0046]      FIG. 18  is a perspective view of composting trench of composting apparatus of  FIG. 17 ; and 
           [0047]      FIG. 19  is a flow chart of organic ammonium sulfate product manufacture process of a seventh preferred embodiment of the method of the present invention. 
       
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
       [0048]    It is to be understood that this invention is not limited to particular aspects of the present invention described, as such may, of course, vary. It is also to be understood that the terminology used herein is for the purpose of describing particular aspects only, and is not intended to be limiting, since the scope of the present invention will be limited only by the appended claims. 
         [0049]    Methods recited herein may be carried out in any order of the recited events which is logically possible, as well as the recited order of events. 
         [0050]    Where a range of values is provided herein, it is understood that each intervening value, to the tenth of the unit of the lower limit unless the context clearly dictates otherwise, between the upper and lower limit of that range and any other stated or intervening value in that stated range, is encompassed within the invention. The upper and lower limits of these smaller ranges may independently be included in the smaller ranges and are also encompassed within the invention, subject to any specifically excluded limit in the stated range. Where the stated range includes one or both of the limits ranges excluding either or both of those included limits are also included in the invention. 
         [0051]    Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. Although any methods and materials similar or equivalent to those described herein can also be used in the practice or testing of the present invention, the methods and materials are now described. 
         [0052]    It must be noted that as used herein and in the appended claims, the singular forms “a”, “an”, and “the” include plural referents unless the context clearly dictates otherwise. It is further noted that the claims may be drafted to exclude any optional element. As such, this statement is intended to serve as antecedent basis for use of such exclusive terminology as “solely,” “only” and the like in connection with the recitation of claim elements, or use of a “negative” limitation. 
         [0053]    It will be appreciated that terms such as “front,” “back,” “top,” “bottom,” “left,” “right,” “horizontally,” “up,” “down,” and “side” used herein are merely for ease of description and refer to the orientation of the components as shown in the figures. It is to be understood that any orientation of the apparatus, and the components thereof described herein, is within the scope of the present invention. 
         [0054]    In a preferred embodiment, the term “organic” as used herein is a labeling certification term that refers to an agriculture product produced in accordance with the Code of Federal Regulations (“CFR”) Title 7 (Subtitle B, Chapter I, Subchapter M, Part 205). As used hereinafter, “organic ammonium sulfate” is interchangeable with “ammonium sulfate,” “organic ammonium sulfate product,” and/or “product.” As used herein, “plurality” means “one or more.” 
         [0055]    Referring now generally to the Figures and particularly to  FIGS. 1A, 1B and 1C ,  FIG. 1A  is a process chart comprising aspects of the invented method that may be instantiated by the first preferred embodiment  100  of the present invention (hereinafter, “the first system  100 ”). In step  1 . 00  the first system  100  is preferably co-located with a volume of source ammonia gas  102 . In step  1 . 02  and proximate to a water volume  104 , a sulfur mass  106  in a solid form is burned in the presence of atmospheric oxygen  108  to form gaseous sulfur dioxide  110 . The temperature of the source ammonia gas  102  and the water volume  104  is initially preferably within 5 degrees Celsius of the ambient temperature of the site environment of the first system  100  and also preferably within the temperatures range of greater than the freezing point of the water volume  104  and less than the boiling point of the water volume  104 . 
         [0056]    The water volume  104  is then acidified in step  1 . 04  by introduction of the sulfur dioxide  110  to form an acidic aqueous solution  112 , as indicated in  FIG. 1C . 
         [0057]    The acidic aqueous solution  112  is then exposed to the source ammonia gas  102 , and optionally carbon dioxide, in step  1 . 06 , wherein portions of the source ammonia gas  102 , and optionally gaseous carbon dioxide, is absorbed by the aqueous solution  112  in step  1 . 06 . It is understood that the source ammonia gas may  102  may be comprised within an enclosed atmospheric gas  114  that includes other atomic and molecular components, such as carbon dioxide, and that the acidic aqueous solution  112  may absorb carbon dioxide and additional molecules and free atoms from the enclosed atmospheric gas  114  in step  1 . 06 . It is further understood that the enclosed atmospheric gas  114  may be formed by adding ammonia, carbon dioxide and other products of bacteria acting on organic waste, e.g., dung or feces, to a pre-existing ambient atmosphere. 
         [0058]    Precipitates, other solutes and/or certain non-aqueous components of the aqueous solution  112 , e.g., ammonium sulfate, are concentrated and collected by circulation through a collection module  116  in step  1 . 08  to form an output solution  128  that is held in a holding tank  130  for removal from the first system  100 , and the pH of the aqueous solution  112  is monitored in step  1 . 10 . When a pH measurement of greater than 5.0 is determined in step  1 . 12 , the rate of volumetric exposure of the gaseous sulfur dioxide  110  is increased in step  1 . 14 , and when a pH measurement of lower than 4.0 is determined in step  1 . 16 , the rate of volumetric exposure of the gaseous sulfur dioxide  111  is decreased in step  1 . 80   
         [0059]    It is understood that the aqueous solution  112  is preferably substantively and continuously exposed to gaseous sulfur dioxide  110  in steps  1 . 06  through  1 . 18  albeit possibly at varying rates of volumetric exposure to the sulfur dioxide gas  110  is increased in step  1 . 14 . It is further understood that the absorption of the source ammonia gas  102  indicated in step  1 . 06  and the collection of solutes and non-aqueous components of the aqueous solution of step  1 . 08  are preferably continuously and contemporaneously occurring during the instantiation of the loop of steps  1 . 06 - 1 . 18 . 
         [0060]    An operator or an automated control system  118  may act and/or elect to stop the process loop of steps  1 . 02  through  1 . 18  in step  1 . 20  whereby the burning of the sulfur mass  106  and the processes of steps  1 . 04  through  1 . 18  are halted are minimized. 
         [0061]    Referring now generally to the Figures and particularly to  FIG. 1B ,  FIG. 1B  is a block diagram of the first system  100  that includes certain optional elements. The first system  100  is coupled to a source enclosure  120  that contains the source ammonia gas  102  and the enclosed atmospheric gas  114 . The source ammonia gas  102  may be emitted from a source material  121  containing ammonium and/or ammonium compounds, and the first system  100  is adapted to withdraw the source ammonia gas  102 , by itself and/or mixed within the enclosed atmospheric gas  114  located within the source enclosure  120 , into an ammonia scrubber module  122  through which the water volume  104  is circulated. The water volume  104  is maintained within a reaction chamber  124  and the ammonia scrubber module  122  (hereinafter, “the ammonia scrubber module  122 ”) is coupled to both the source enclosure  120  and the reaction chamber  124  and is further adapted to circulate the aqueous solution  112  to absorb the source ammonia gas  102 . The source ammonia gas  102  is thus removed from the source enclosure  120  and inserted into the water volume  104  as the water volume  104  is circulated through the ammonia scrubber  122 . A sulfur dioxide generation module  126  is also coupled with the reaction chamber  124  and is adapted to insert or infuse the gaseous sulfur dioxide  110  into the water volume  104  to form the aqueous solution  112  as the water volume  104  is circulated through the sulfur dioxide generation module  126 . The collection module  116  is a combined reverse osmosis module and electro dialysis module  116  (hereinafter, “the RO/ED module  116 ”) and is additionally coupled with the reaction chamber  124  by tuning  144  to withdraw aqueous solution  112  and preferably return water volume  104 . The RO/ED module  116  is adapted to remove certain chemicals, e.g., ammonium sulfate, from the aqueous solution  112  as the aqueous solution  112  is circulated through the RO/ED module  116 . A concentrate output holding tank  126  is coupled with the RO/ED module  116  and is adapted to receive a concentrated output solution  128  formed within the RO/ED module  116  and containing both (a.) a portion of the water volume  104  as a solvent and (b.) a solute or component of at least one type of resultant chemical, e.g., ammonium sulfate, formed within the aqueous solution  112  by the invented method. The aqueous solution  112  and the concentrated output solution  128  may thus include ammonium sulfate as a solute or component, whereby ammonium sulfate is produced in a manner that is in conformance one or more governmental, regulatory or organizational standards and the resultant ammonium sulfate may receive a certification of a preferred or particular origin, such as a being certified, graded, trademarked or marked as a special type of organic sulfate. It is understood that the receipt of such certifications or authorizations may increase the market value and perceived quality of the resultant ammonium sulfate of the concentrated output solution  128 . 
         [0062]    It is also understood that the first system  100  may include commercially available equipment or their equivalents, wherein the ammonia scrubber  122  may be or comprise, or be comprised within, a wet flue gas scrubber marketed by Deryck A Gibson Ltd. of Kingston Jamaica. In various alternate preferred embodiments of the present invention, the acidified aqueous solution  112  may presented to the source ammonia gas  102  within the ammonia scrubber  122  as a mist, a spray or a waterfall as the aqueous solution  112  is circulated through the ammonia scrubber  122 . The reaction chamber  124  may comprise sheets, walls, a bottom wall and or/ceiling wall of polyvinyl chloride or other suitable material known in the art. 
         [0063]    The sulfur dioxide module  126  may be or comprise, or be comprised within, a sulfur dioxide burner system as marketed by Harmon Systems International, LLC of Bakersfield, Calif., whereby the sulfur dioxide gas  110  may be generated and commingled with water volume  104  that is circulated through the sulfur dioxide module  126 . It is understood that the Harmon sulfur dioxide burner system oxidizes sulfur  106  into sulfur dioxide gas  110  by burning the elemental sulfur  106  with a propane torch in the presence of a pressurized circulating portion of the water volume  104  and air containing oxygen  108 . The sulfur dioxide gas  110  is combined with the water volume  104  to produce sulfurous acid, or H2SO3, within the aqueous solution  112   
         [0064]    In addition, the RO/ED module  116  may be or comprise, or be comprised within, a reverse osmosis/electro dialysis system as marketed by Ameridia Corporation of Moerdjik, Netherlands. 
         [0065]    A control module  200  of the first system  100  generates and communicates commands to direct the activity, and provides electrical power that enables the functioning, of the first system  100  in the removal gaseous ammonia and the generation of resultant chemical compounds and precipitates e.g., ammonium sulfate. A communications and power bus  132  of the control module  118  enables the control module  118  to send and receive commands and data within the first system  100  and selectively and controllably provide power to other modules  116   122 ,  126 , supply fans SF 01 , supply pumps SP 01 -SP 04 , motorized fluid return pumps R 01 -R 03 , and an output pump OP 01 . 
         [0066]    Referring now generally to the Figures and particularly to  FIG. 1C ,  FIG. 1C  is a block diagram of a second preferred embodiment of the invented system  136  (hereinafter, “the second system  136 ”) that includes the first system  100  and an agitator module  138  having an effector  140 . The effector  140  is positioned relative to the source material  121  and is adapted to agitate the source material  121  in order to sponsor bacterial activity that accelerates a production of the source ammonia gas  102  for capture within the enclosure. The agitator module  140  may be or comprise (a.) a motorized rototiller, wherein the effector  140  is or comprises a mechanical arm or rake that is motor driven to mechanically disturb and aerate the source material  121 ; (b.) a pressurized air pump, wherein the effector  140  is or comprises a gas hose that delivers pressurized ambient air into the source material  121  and thereby disturbs and aerates the source material  121  with the pressurized ambient air. 
         [0067]    Referring now generally to the Figures and particularly to  FIG. 1D ,  FIG. 1D  is a detailed block diagram of a first preferred embodiment of the ammonia scrubber  122 . A first fluid supply pump SP 01  as energized by a scrubber system control module  142  and/or the control system  118  pumps portions of the aqueous solution  112  from the reaction chamber  124  through substantively chemically inert tubing  144  through one or more aeration fixtures  146 - 150  to enable the aqueous solution  112  to absorb the source ammonia  102 . The ammonia scrubber  122  further comprises a scrubber interface  154  that is bidirectionally communicatively coupled with the control module  118  via the communications and power bus  132 . The scrubber interface  154  is additionally bi-directionally communicatively coupled with, or comprised within, the scrubber system control module  142 . 
         [0068]    The aqueous solution  112  passes through the source ammonia gas  112  and falls by gravity into a scrubber tank  152 . A first aeration fixture  146  releases the aqueous solution  112  within the ammonia scrubber  122  as a sheet of fluid. A second aeration fixture  148  is a showerhead that releases the aqueous solution  112  into the source ammonia gas  102  as a fine water mist. A third aeration fixture  150  is a showerhead that releases the aqueous solution  112  into the source ammonia gas  102  as water droplets. 
         [0069]    A first motorized fluid return pump SP 01  as energized by the scrubber system control module  142  and/or the control system  118  pumps the aqueous solution  112  captured by the scrubber tank  152  through additional tubing  144  and thereby returns the aqueous solution  112  to the reaction chamber  124 . An optional first supply fan SF 01  as energized by the scrubber system control module  142  and/or the control system  118  propels or drives the source ammonia gas  102  and the enclosed atmospheric gas  114  from the enclosure  120  and into the ammonia scrubber  122  through a length of tubing  144 . The scrubber tank  152  may comprise sheets, walls, a bottom wall and/or ceiling wall of polyvinyl chloride or other suitable material known in the art. 
         [0070]    It is understood that the ammonia scrubber  122  may be or comprise a suitable and commercially available gas scrubber known in the art, and that the source fan SF 01 , the first motorized fluid supply pump SP 01  and/or the first motorized fluid return pump RP 01  may be comprised within the ammonia scrubber  122 . It is further understood that the tubing  144  may be or comprise polyvinyl chloride piping or other suitable and preferably substantively chemically inert material known in the art. 
         [0071]    Referring now generally to the Figures and particularly to  FIG. 1E ,  FIG. 1E  is a detailed block diagram of a first preferred embodiment of the sulfur dioxide module  126 . A second motorized fluid supply pump SP 02  as energized by an SO2 module control module  156 , and/or the control system  118 , and thereupon pumps and circulates portions of the aqueous solution  112  from the reaction chamber  124  through substantively chemically inert tubing  144  through a pressure column module  158 . The pressure column module  158  creates a pressure differential that infuses and/or introduces sulfur dioxide gas  110  into the water volume  104  to form and acidify the aqueous solution  112 . An ignition chamber  160  is adapted to maintain the sulfur  106  within the sulfur module  126  before and during of the ignition of the sulfur  106 . The ignition of the sulfur  106  may be accomplished by a user manually applying a flame  161  to the sulfur  106  or by an electronically controlled ignition device  161 B that (a.) issues a flame or an igniting spark to the sulfur  106  when energized, or (b.) receives an ignition command message from the SO2 module controller  156  and/or the control system  118  and is thereby directed to generate a spark, a blue flame and/or another sulfur ignition medium known in the art. Still alternatively, optionally or additionally, the sulfur  106  may be or comprise touch-to-burn sulfur and may be manually ignited. 
         [0072]    An SO2 module interface  162  is disposed between, and bi-directionally communicatively coupled with both of, the control system  118  and the SO2 module controller  156 . Bi-directional communications between the control module  200  and the SO2 module controller  156  are enabled by the communications and power bus  132  and the SO2 module interface  162 , whereby commands and data may be communicated to and from the control module  200  and the SO2 module controller  156 . Electrical power is also provided to the sulfur dioxide module  126  via the communications and power bus  132  and the SO2 module interface  162 . 
         [0073]    Optionally and alternatively electrical power and/or commands are provided electronically controlled ignition device  161 B by a communicative coupling of the electronically controlled ignition device  161 B with the SO2 module controller  156  and/or the power and communications bus  132  of the control system  118 . 
         [0074]    It is understood that the sulfur module  126  may be or comprise a sulfur burner as marketed by Harmon Systems International, LLC of Bakersfield, Calif., or other suitable sulfur burner known in the art. It is further understood that the sulfur burner  126  may be or comprise a suitable and commercially available sulfur burner known in the art, and that the second motorized fluid supply pump SP 02  and/or the second motorized fluid return pump RP 02  may be comprised within the sulfur burner  126 . 
         [0075]      FIG. 1F  is a block diagram of a first preferred embodiment of the RO/ED module  116 . The RO/ED module  116  may include a reverse osmosis module  164 , an electro-dialysis module  166 , a reverse osmosis electro dialysis electronic logic controller module  168  (hereinafter, “RO/ED controller  168 ”), an electronic interface  170  to the reverse osmosis electro dialysis electronic logic controller module (hereinafter, “RO/ED interface  170 ”) and a second motorized fluid output pump OP 02 . It is understood that one or more of the third motorized fluid supply pump SP 03 , the third motorized fluid return pump RP 03 , the fourth motorized fluid return pump RP 04 , the first motorized fluid output pump OP 01 , and the output holding tank  130  may be optionally or additionally comprised within the RO/ED module  116 . Bi-directional communications between the control module  200  and the RO/ED controller  168  is enabled by the communications and power bus  132  and the RO/ED interface  170 , whereby commands and data may be communicated to and from the control module  200  and to the RO/ED controller  168 . Electrical power is also provided to the RO/ED module  116  via the communications and power bus  132  and the RO/ED interface  170 . 
         [0076]    The RO/ED controller  168  is optionally bidirectionally communicatively coupled to the reverse osmosis module  164  and may provide required electrical power and control signals to the reverse osmosis module  164  that direct and enable the reverse osmosis module  164  to substantively extract water volume from the aqueous solution  122  by reverse osmosis. The RO/ED controller  168  is further optionally bidirectionally communicatively coupled to the electro-dialysis module  166  and may provide required electrical power and control signals to the electro-dialysis module  166  that direct and enable the electro-dialysis module  166  to substantively extract additional water volume from the aqueous solution  122  by electro dialysis. The aqueous solution  112  is delivered to the reverse osmosis module  164  by energizing the third motorized fluid supply pump SP 03  via a length of tubing  144 . After some water volume  104  is extracted from the aqueous solution  112  by the reverse osmosis module  164 , the resultant aqueous solution  112  is delivered to the electro dialysis module  166  from the reverse osmosis module  164  by energizing the second motorized fluid output pump OP 02 . The RO/ED controller  168  is additionally optionally electrically coupled to the second motorized fluid output fluid pump OP 02  and selectively provides electrical power to energize the second motorized fluid output fluid pump OP 02  to enable transfer of the aqueous solution  112  from the reverse osmosis module  164  and to the electro dialysis module  166 . 
         [0077]    The RO/ED controller  168  and/or the control module  200  may optionally or additionally be coupled to the third motorized fluid supply pump SP 03  and/or the third motorized fluid return pump RP 03  and selectively energize the third motorized fluid supply pump SP 03  and/or the third motorized fluid return pump RP 03  to enable a delivery of the aqueous solution  112  to the reverse osmosis module  164  and return of water volume  104  from the reverse osmosis module  164  to the reaction chamber  124 . The RO/ED controller  168  and/or the control system  118  may further optionally or additionally be coupled to the fourth motorized fluid return pump RP 04  and selectively energize the fourth motorized fluid return pump RP 04  to enable a return of water volume  104  from the electro dialysis module  166  to the reaction chamber  124 . The RO/ED controller  168  and/or the control system  118  may further optionally or additionally be coupled to the first motorized fluid output pump OP 01  and selectively energize the first motorized fluid output pump OP 01  to enable transfer of the output solution  128  from the electro dialysis module  166  to the holding tank  130 . The holding tank  130  may be or comprise one or more walls, floor wall, and/or ceiling comprising polyvinyl chloride or other suitable material known in the art. 
         [0078]    An optional or additional RO/ED tubing length  172  may couple the reverse osmosis module  164  and the fourth motorized fluid return fluid pump RP 04  and may enable the fourth motorized fluid return fluid pump RP 04  to drive water volume from both the reverse osmosis module  164  and the electro dialysis module  166  and into the reaction chamber  124 . The RO/ED tubing length  172  may be or comprise perforated polyvinyl chloride piping and/or other suitable and substantively chemically inert material known in the art. 
         [0079]    Referring now generally to the Figures and particularly to  FIG. 2 ,  FIG. 6  and  FIG. 7 ,  FIG. 2  is a software flow chart implemented by of the control system  118 . In step  2 . 02  a command is sent from a control module  200  of the control system  118  to the sulfur dioxide module  126  to ignite the sulfur  106 . In optional step  203  the control module  200  directs, and electrically powers, the agitator module  138  to agitate the source material  121  and to thereby sponsor bacterial activity that will generate gaseous ammonia  102  and optionally carbon dioxide within the enclosure  120 . The volume of gaseous ammonia preferably includes molecules of NH3 and molecules of NH4+. 
         [0080]    In step  2 . 02  another command is sent from the control module  200  in step  2 . 04  to (a.) energize motorized fluid pumps SP 02  &amp; RP 02  to circulate water volume  104  and (b.) inject the resultant sulfur dioxide gas  110  via the pressure column  158  into the water volume  104  to generate the aqueous solution  112 . In step  2 . 06  the control module  200  accepts pH sensors SPh. 01 -SPh.N positioned within or proximate to the reaction chamber  124  to determine the pH of aqueous solution  112 , and when the pH of the aqueous solution is not sensed to be greater than 4.0, the control system  118  directs the sulfur dioxide module  126  to simply continue inject sulfur dioxide  110  into the aqueous solution  112  until the aqueous solution  112  is measured by the pH sensors SPh. 01 -SPh.N to have exceeded a magnitude of approximately 4.0. 
         [0081]    When the control module  200  receives a pH reading in step  2 . 06  greater than 4.0 from the pH sensors SPh. 01 -SPh.N, the control module  600  proceeds on to step  2 . 08  and energizes the ammonia scrubber  122  in step  2 . 08 , whereby the ammonia scrubber  122  circulates the aqueous solution  112  through the ammonia scrubber  112  and exposes the aqueous solution  112  to the source ammonia gas  112 . In optional step  2 . 09  the control system  118  directs an optional carbon dioxide module  202 , as further disclosed in reference to  FIG. 11 , to initiate delivery of carbon dioxide into the aqueous solution  112  within the reaction chamber  124 . 
         [0082]    The control module  600  directs the RO/ED module  116  in step  2 . 10  to circulate the aqueous solution  112  through the RO/ED module  116  and to generate an output solution  128  for storage in the output holding tank  130 . 
         [0083]    In step  2 . 12  the control module  600  determines whether to continue the process of step  2 . 04  through  2 . 10 , whereby portions of the aqueous solution are substantively continuously and contemporaneously circulated to and from the reaction chamber  124  and (a.) the sulfur dioxide module  126  to receive sulfur dioxide; (b.) the ammonia scrubber  122  to absorb source ammonia gas  102 ; and (c.) the RO/ED module  116  to filter out components, e.g., ammonium sulfate; and to generate the output solution  128 . It is understood that the output solution contains (a.) a portion of the water volume  104  and (b.) one or more non-aqueous components of the aqueous solution  112  that have been separated from the aqueous solution  112  by the RO/ED module  116 . The control module  200  might, for example, be programmed to proceed to step  2 . 13  and to shut down the first system  100  or the second system  136  when an ammonia gas detector SA 01  sends a measurement that indicates that that the concentration of the source ammonia gas  102  within the atmospheric gas  114  within the enclosure  120  is less than a pre-specified amount, e.g., less than one parts per million per volume unit. 
         [0084]    In the alternative, in step  2 . 12  a human operator may direct the control system via an input module  202  to cease operations and proceed to step  213  and to shut down the first system  100  or the second system  200 . 
         [0085]    The control system  118 , in accordance with its structure, inputs and programming, may proceed from step  2 . 12  and to execute the loop of steps  2 . 14  through  2 . 28 , whereby the control system  118  directs the first system  100  or the second system  136  to maintain a pH of the aqueous solution  112  approximately within a preferred range, such as approximately within the range of from 4.0 to 5.0 plus or minus five percent. 
         [0086]    When the control module  200  determines in step  2 . 14  that the pH of the aqueous solution  112  is measured to be greater than 5.0, the control system  118  proceeds on to step  2 . 16  and pause the activity of the ammonia scrubber  122  in circulating and exposing aqueous solution  112  for absorption of ammonia gas  102  and in step  2 . 18  directs the sulfur dioxide module  126  to increase the rate of introduction of sulfur dioxide  110  into the aqueous solution  110 . An optional wait step  2 . 20  imposes a wait state of a predetermined time, and in step  2 . 22  the control system  118  directs the ammonia scrubber  122  to resume circulating aqueous solution  112  and causing absorption of the source ammonia gas  102  into the aqueous. The control system  118  directs the sulfur dioxide module  126  to resume a preprogrammed or pre-specified standard rate of introduction of sulfur dioxide  110  into the aqueous solution. 
         [0087]    In the alternative, when the control module  200  determines in step  2 . 14  that the pH of the aqueous solution  112  is not measured to be greater than 5.0, the control system  118  proceeds on to step  2 . 26  and to determine if that the pH of the aqueous solution  112  is measured to be less than 4.0. When the control system  118  to determines in step  2 . 26  that the pH of the aqueous solution  112  is measured to be less than 4.0, the control system  118  directs the sulfur dioxide module  126  to decrease the rate of introduction of sulfur dioxide  110  into the aqueous solution  110  to a certain pre-specified or preprogrammed rate of introduction of sulfur dioxide  110  into the aqueous solution  110 . The control module  200  proceeds from either step  2 . 26  or step  2 . 28  to step  2 . 12 . 
         [0088]    It is understood that alternative control methods to implement the invented method are made obvious to one of ordinary skill in the art in light of the present invention. In certain alternate preferred methods of the present invention, manual control, material input and/or material output may be applied, effected or enabled by a human operator to engage, disengage, turn on and/or turn-off one or more modules  116 ,  122  &amp;  126 , the source fan SF 01 , one or more motorized fluid pumps OP 01 , OP 02 , SP 01 -SP 03  &amp; RP 01 -RP 04 . 
         [0089]      FIG. 3  is a cut-away top view of the first system  100  adapted to decontaminate the internal volume of air  300  of a substantively enclosed and contaminated structure  302 , wherein the enclosed volume of air  300  includes the source gaseous ammonia  102 . 
         [0090]      FIG. 4  is a cut-away side view of the first system  100  adapted to remediate an ammonia gas emitting and substantively liquid material  400 , wherein a portable tent source enclosure  402  is placed above and around the substantively liquid material  400  and an optional motorized air pump  404  is placed and positioned to pump air into the liquid spill material  400  through a tubing  406  in order to sponsor an accelerated production of source ammonia  102  from the substantively liquid material  400  by bacterial action. An air pump controller  408  is electrically coupled with both the motorized air pump motor  404  and the power and communications bus  132 , whereby the air pump controller  408  receives electrical power to energize the air pump  404  via the power and communications bus  132 , wherein the control system  118  selectively and controllably delivers electrical power to the air pump controller  408 . 
         [0091]      FIG. 5  is an example of the first system  100  enclosing an accumulation of a substantively solid collection of bird excrement or animal dung  500  (hereinafter, “dung  500 ”) housed within an enclosure  502 . The dung  500  emits the source ammonia gas  102 . The first system  100  is augmented with a tilling blade  504  that is rotatably coupled with an agitator motor  506 . The tilling blade  504  is adapted and applied to mechanically turn over and agitate the dung  500  and thereby accelerate the production and capturing of the gaseous ammonia  102 . The 
         [0092]    An agitator motor controller  508  is electrically coupled with both the agitator motor  506  and the power and communications bus  132  and receives electrical power to energize the agitator motor  506  via the power and communications bus  132 , wherein the control system  118  selectively and controllably delivers electrical power to the agitator motor  506 . Additionally, alternatively or optionally, the agitator motor  506 , the tilling blade  504  and the agitator motor controller  508  may be or be comprised within an automated COMPOST-A-MATIC™ in-vessel composting system as marketed by Farmer Automatic of America, Inc. of Register, Ga. or other suitable motorized or automated tilling system known in the art. It is understood that the agitator module  138  may optionally or alternatively be or comprise an isolated stand-alone system that is not coupled with the power and communications bus  132  and receives an independent feed of electrical power. 
         [0093]      FIG. 6  is a schematic diagram of an optional internal control system  118  of the first system  100  with optional modules that extend control to the second system  136 . The control module  200  includes a real time clock  600  coupled with a logic controller  602 . The logic controller  602  may be coupled with an optional memory  604 . The logic controller  602  may be a programmable logic unit that directs the first system  100  to perform the invented method, to include the aspects of the method of  FIG. 2 , and/or the logic control  602  might be configured or adapted to execute programming of a software program stored within the memory  604 . The control module  200  is bi-directionally communicatively coupled by means of a communication bus  606  with the ammonia scrubber interface  154 , the sulfur dioxide module interface  162 , the RO/ED module  116 , one or more pH sensors SpH. 01 -Sph.N and one or more ammonia gas concentration sensors SA. 01 -SA.N. The communication bus  606  is preferably comprised within the power and communications bus  132 . 
         [0094]    The control module  200  may optionally or additionally be coupled with the agitator motor controller  504  and/or the agitator pump controller  406 . The control module  200  may be further optionally or additionally be coupled with a carbon dioxide valve controller  608  of the carbon dioxide source module  202  of the second system  136 , and as further disclosed in reference to  FIGS. 6, 7 and 11 . 
         [0095]      FIG. 7  is a schematic diagram of a controlled power distribution network  700  of the control system  118  of the first system  100  of  FIG. 1A  and including optional elements of the second system  136 . The power distribution network  700  selectively and as controlled by the control module  200  delivers electric power from an electrical power source  702  to the ammonia scrubber  122 , the sulfur dioxide module  126 , the RO/ED module  116 , one or more pH sensors, one or more ammonia gas concentration sensors, one or more motorized fluid pumps OP 01 , SP 01 -SP- 04  &amp; RP 01 -RP- 03 , and/or the source fan SF 01  of the first system  100 . Additionally or alternatively, power distribution network  700  selectively and as controlled by the control module  200  delivers electric power from the electrical power source  702  to the agitator pump controller  406 , the agitator motor controller  508 , and/or the carbon dioxide source valve controller  608 . 
         [0096]      FIG. 8  is a cut-away view of an ammonia delivery perforated tubing  800  of the first system  100  that is coupled with an output port of the first return pump RP 01  and returns the aqueous solution  112  from the ammonia scrubber  122  and to the reaction chamber  124 . The ammonia delivery perforated tubing  800  is adapted and configured to return aqueous solution  112  from the ammonia scrubber  122  and into the reaction chamber  124 , and may be or comprise perforated polyvinyl chloride piping and/or other suitable and substantively chemically inert material known in the art. 
         [0097]      FIG. 9  is a cut-away view of a sulfur dioxide delivery perforated tubing  900  of the first system  100  that circulates and returns the aqueous solution  112  from the sulfur dioxide module  126  and to the reaction chamber  124 . The sulfur dioxide delivery perforated tubing  900  is adapted and configured to return aqueous solution  112  from the sulfur dioxide module  126  and into the reaction chamber  124 . The sulfur dioxide delivery perforated tubing  900  may be or comprise perforated polyvinyl chloride piping and/or other suitable and substantively chemically inert material known in the art. 
         [0098]    Referring now generally to the Figures and particularly to  FIG. 10  and  FIG. 11 ,  FIG. 10  is a block diagram of a third alternate preferred embodiment of the present invention  1000  (hereinafter, “third system  1000 ”) comprising the carbon dioxide module  202  coupled with the first system  100 . As disclosed in  FIG. 11 , the carbon dioxide module  202  comprises a source of pressurized carbon dioxide  1100  and is adapted to deliver gaseous carbon dioxide into the water volume  104  and within the reaction chamber  124  via a length of the chemically inert tubing  144 . A pressure release valve  1102  is coupled with the source of pressurized carbon dioxide  1100  and a carbon dioxide delivery tubing  1004  via the length of the chemically inert tubing  144 . The carbon dioxide perforated delivery tubing  1004  located within the reaction chamber  124  and is adapted to accept carbon dioxide from source of pressurized carbon dioxide  1100  and via the pressure release valve  1102 . The carbon dioxide valve controller  608  controls opening and closing of the pressure release valve  1102  and receives commands and electrical power from the control module  200  via communications and power bus  132 , whereby the control system  118  directs, starts, stops and controls introduction of carbon dioxide into the aqueous solution  112  from the source of pressurized carbon dioxide  1100 . The carbon dioxide perforated tubing  1004  may be or comprise perforated polyvinyl chloride piping or other suitable and substantively chemically inert material known in the art. 
         [0099]      FIG. 12  is an illustration of a motorized embodiment  1200  of the first system  100 . The motorized embodiment includes a motorized cab  1202  and a wheeled trailer  1204 , wherein the motorized cab  1202  is adapted to detachably engage with the wheeled trailer  1204  and transport portable an ammonia gas scrubber  1206 , an RO/ED module  1208 , a sulfur dioxide module  1210 , a components holding tank  1212  and a resultant components holding tank  1212 . 
         [0100]      FIG. 13  is an illustration of a carbon dioxide generation  1300  module that accepts mammalian exhalation a source of gaseous carbon dioxide. An enclosed animal barn  1300  substantively encloses a plurality of mammalian livestock  1302 - 1306 . An injection module  1308  receives carbon dioxide sourced from the mammalian livestock  1302 - 1306  via a length of the tubing  144 . The injection module  1308  pressurizes the received carbon dioxide and injects the pressurized carbon dioxide into the pressurized carbon dioxide source  1100  via the tubing  144 . 
         [0101]    Referring now generally to the Figures and particularly to  FIGS. 14, 15 and 16 ,  FIG. 14  discloses aspects and steps  14 . 00 - 14 . 22  of a sixth alternate preferred embodiment of the invented method (hereinafter, “the sixth method”),  FIG. 15  discloses material, equipment and equipment modules  15 A- 15 R that may be employed in one or more steps or aspects  14 . 00 - 14 . 22  of the sixth method, and  FIG. 16  discloses inventive materials, aspects and elements  16 A- 16 E that may optionally be applied in an instantiation of the sixth method and various alternate preferred embodiments of the present invention. 
         [0102]    More particularly  FIG. 14  is a process diagram of the sixth method. In step  14 . 00  a biomass  16 A of organic residuals, e.g., chicken litter and/or other ammonia generating and/or comprising organic materials, is positioned, preferably within an enclosure  102  as shown in  FIG. 16 , and enabled to emit a quantity of ammonium gas  15 A into a mixture of atmospheric gases  15 B in step  14 . 02 . The ammonium gas  15 A may be captured in step  14 . 02  as a component of a mixture of atmospheric gases  15 B or optionally selected from the atmospheric gases  15 B. Optional aspects and equipment related to the production of ammonium gas  15 A are elaborated in  FIG. 16 . 
         [0103]    The ammonium gas  15 A and/or atmospheric gases  15 B are optionally passed through an ammonium gas scrubber  15 C in optional step  14 . 06 . The ammonium gas  15 A is delivered in step  14 . 08  into a reaction chamber  15 D, and/or optionally as a component of the mixture of atmospheric gases  15 B of step  14 . 02  and/or as an output from the ammonium gas scrubber  15 C. The ammonium gas  15 A delivered into the reaction chamber  15 D in step  14 . 08  is thereupon brought into contact with, and permitted to react with, the second reactant sulfur dioxide  15 A in step  14 . 09 , whereupon an output mass of ammonium sulfate  15 F is formed. The mass of ammonium sulfate  15 F is then transferred into a storage tank  15 G in step  14 . 10  and made available for immediate use, or alternately collected and made available for later transport and use, 
         [0104]    Referring now to steps  14 . 12  through  14 . 20 , a second reactant sulfur dioxide  15 E is disclosed to be generated from one or a combination of sources. In optional step  14 . 12  a mass of elemental sulfur  15 H is secured and thereupon is combusted in step  14 . 14  by means of a sulfur burning system  15 I. In one optional variation of the present invention, the sulfur burning system  15 I is or comprises an a sulfur dioxide burner system as marketed by Harmon Systems International, LLC of Bakers field, Calif., whereby the second reactant sulfur dioxide  15 E is generated by combustion of the elemental sulfur  15 H in optional step  14 . 16  by burning the elemental sulfur  15 H with a propane torch (not shown) to generate a first mass of sulfur dioxide gas  15 J containing the second reactant sulfur dioxide  15 E. 
         [0105]    Alternatively or additionally, a second mass of gaseous sulfur  15 K may be obtained and delivered in step  14 . 18 . Further alternatively or additionally, a third mass of gaseous sulfur  15 L may be extracted from a liquid mass  15 M of a solution containing sulfur in step  14 . 20  by an extraction system  15 P. 
         [0106]    The second reactant sulfur dioxide  15 E as generated or obtained in steps  14 . 14 - 14 . 20  may optionally be transferred into the scrubber in optional step  14 . 21 . 
         [0107]    The second reactant sulfur dioxide  15 E as generated or obtained in steps  14 . 14 - 14 . 20  is transferred into the reaction chamber  15 D in step  14 . 22  to enable reaction with the mass of ammonium gas  15 A in step  14 . 10 . It is understood that the second reactant sulfur dioxide  15 E may be or comprise, in singularity or combination, the solid sulfur  15 H of step  14 . 12 , the first mass of sulfur dioxide gas  15 J of step  14 . 16 , the second mass of gaseous sulfur  15 K of step  14 . 18 , and/or the third mass of gaseous sulfur  15 L of step  14 . 20 . 
         [0108]    Referring now to the Figures and particularly to  FIG. 15 ,  FIG. 15  is a schematic diagram of an additional optional embodiment of a production facility  15 N wherein aspects of the sixth method, and other alternate preferred embodiments of the invented method, may be instantiated or implemented. 
         [0109]    The source ammonium gas  15 A is emitted from the organic source material biomass  16 A containing ammonium and/or ammonium compounds. A first fan  150 . 1  is adapted to withdraw the source ammonia gas  15 A into an ammonia scrubber module  15 C. The ammonia scrubber module  15 C and the reaction chamber  15 D are connected via a circulation system and are both coupled to the sulfur source enclosure  120 . A sulfur dioxide generation module, either the sulfur gas  15 A &amp;  15 J- 15 L from elemental sulfur combustion of step  14 . 14  of the method of  FIG. 14  or extracted sulfur from sulfur water source  15 M, is also coupled with the reaction chamber  15 D. As the reaction solution circulates through the scrubber  15 C and reaction chamber  15 D, the concentrate output is transferred into the storage tank  15 G. 
         [0110]    It is understood that the ammonia scrubber  15 C may be or comprise a suitable and commercially available gas scrubber known in the art, and that the source fan may be comprised within the ammonia scrubber  15 C. It is further understood that the tubing connecting the source nitrogen gas  15 A and scrubber  15 C may be or comprise polyvinyl chloride piping or other suitable and preferably substantively chemically inert material known in the art. 
         [0111]    The concentrated output solution may thus include ammonium sulfate as a solute or component, whereby ammonium sulfate is produced in a manner that is in conformance one or more governmental, regulatory or organizational standards and the resultant ammonium sulfate may receive a certification of a preferred or particular origin, such as a being certified, graded, trademarked or marked as a special type of organic sulfate. It is understood that the receipt of such certifications or authorizations may increase the market value and perceived quality of the resultant ammonium sulfate of the concentrated output solution. 
         [0112]    It is also understood that the system in  FIG. 15  may include commercially available equipment or their equivalents, wherein the ammonia scrubber  15 C may be or comprise, or be comprised within, a wet flue gas scrubber marketed by Deryck A Gibson Ltd. of Kingston Jamaica. In various alternate preferred embodiments of the present invention, the source ammonia gas  15 A is present as a mist, a spray or a waterfall as it circulates within the ammonia scrubber  15 C. The reaction chamber  15 D may comprise sheets, walls, a bottom wall and or/ceiling wall of polyvinyl chloride or other suitable material known in the art. 
         [0113]    As indicated in  FIGS. 14 and 15 , the ambient air  15 B and/or gases  15  containing the collected NH3 and CO2 gasses are propelled by a first fan  150 . 1  to enter scrubber module  15 C An optional second fan module  150 . 2  propels the ambient air  15 B and/or gases  15 E,  15   j ,  15 K &amp;  15 L into the scrubber module  15 C. An optional airway  15 R enables propels the ambient air  15 B and/or gases  15 E,  15   j ,  15 K &amp;  15 L into the scrubber module  15 C by an alternate route. An optional third fan module  150 . 3  propels the ambient air  15 B and/or gases  15 E,  15   j ,  15 K &amp;  15 L directly into the reaction chamber  15 D. 
         [0114]      FIG. 16  demonstrates a yet additional preferred embodiment of the composting apparatus, wherein ammonia gas  15 A is produced by highly selective aerobic bacteria  16 D action with the biomass  16 A and without adding external heat. The composting building, which may be a barn, a shed, a greenhouse, or a specially constructed dedicated facility, can also serve as the ammonia source chamber that contains and shields the organic residuals biomass  16 A. According to an embodiment of the invention, the floor of the facility is contained of a layer of organic residuals biomass  16 A, as the source of ammonia gas  15 A, and is shielded to prevent noxious gases from escaping. A composting trench is built at the same positions as label  16 . 02  to insulate the biomass from heat loss, and to allow easy aeration and physical movement of the biomass. The composting trench also contains a forced aeration system  16 C, injecting oxygen gases to facilitate the action of a mass of aerobic bacteria  16 D. 
         [0115]    Aerobic bacteria  16 D are provided to highly selectively convert all or substantially all of the waste amino acids, proteins, uric acid and any other available nitrogen compounds in the biomass into NH3 and/or NH4 and CO2. Preferably, the specific strains of aerobic bacteria  16 D used in the present invention include uricolytic bacteria such as  Bacillus pasteurii  and/or  Peptostreptococcus anaerobius, Clostridium sticklandii, Clostridium aminophilum , and  Eubacterium pyruvativorans . Thermophilic bacteria are preferred because their presence reduces the population of harmful bacteria such as  E. coli, Salmonella  and fecal coliform bacteria. 
         [0116]    As the composting process commences, a rototiller  16 B may be used to mix/agitate and aerate the biomass. In a preferred embodiment, a hood may be used to capture rising water vapor and/or NH3 and/or NH4 and CO2 from the biomass  16 A as it generates heat. An intake channel  16 E delivers water vapor and/or NH3 and/or NH4  15 A from the enclosure  120  and into the scrubber  15 C. 
         [0117]    Referring now generally to the Figures and particularly to  FIGS. 17, 18 and 19 ,  FIG. 19  discloses aspects of a seventh alternate preferred embodiment of the invented method (hereinafter, “the seventh method”),  FIGS. 17 and 18  disclose material, equipment and equipment modules  1700 - 1732  that may be employed in one or more steps or aspects of the seventh method, and  FIG. 19  discloses inventive materials, aspects and elements  1900 - 1914  that may optionally be applied in an instantiation of the seventh method and various alternate preferred embodiments of the present invention. 
         [0118]    Referring to  FIGS. 17 through 19 , a preferred embodiment of a composting apparatus  1700  and a method of producing solid and/or concentrated organic ammonium sulfate product by highly selective aerobic bacteria  16 D action without adding external heat, are shown and described. Composting apparatus  1700  is preferably located inside of a composting building  1704 . Composting building  1704  may be a barn, a shed, or a greenhouse. In other embodiments, composting building  1704  may simply be a cover or box covering composting trench  1702 . Composting building  1704  includes an input end  111 , an output end  1713 , and a composting trench  1702 . Preferably, composting trench  1702  is the receptacle used for composting. Preferably, composting building  1704  contains and shields the composting trench  1702  so that noxious gases cannot escape into the environment. Composting trench  1702  preferably contains the heat generated by the aerobic bacteria  16 D action, insulates the biomass from heat loss, and allows easy aeration and physical movement of the biomass. Composting building  1704  preferably contains the means to control the temperature, the moisture, the pH, and the nitrogen content of the biomass in composting apparatus  1700 . Composting building  1704  preferably includes steep eaves or a narrowed roof area to allow a more efficient capture and removal of gasses and water vapors from inside the atmosphere of composting building  1704 . Composting building  1704  may also include a louvered opening  1732  at the input end  1711 . Preferably, louvered opening  1732  may be used for air control. In other embodiments, louvered opening  1732  may be omitted or replaced with another suitable mechanism. 
         [0119]    In a preferred embodiment, composting trench  1702  is from about 1 foot to about 10 feet deep; more preferably from about 2 feet to about 6 feet deep; and most preferably from about 4 feet to 5 feet deep. In a preferred embodiment, composting trench  1702  is from about 50 feet to about 500 feet long; more preferably from about 100 feet to about 350 feet long; and most preferably from about 200 to about 300 feet long. In a preferred embodiment, composting trench  1702  is from about 3 feet to about 25 feet wide; more preferably from about 5 feet to about 20 feet wide; and most preferably from about 8 feet to about 14 feet wide. In a preferred embodiment, the dimensions of composting trench  1702  are as follows: about 4 feet deep, about 250 feet long, and about 10 to about 12 feet wide. In other embodiments, composting trench  1702  may have dimensions greater than, less than, or different from those described above. 
         [0120]    In a preferred embodiment, composting trench  1702  is configured to hold from about 20 days to about 50 days of manure, and more preferably from about 25 days to about 30 days of manure. In other embodiments, composting trench  1702  is configured to hold less than about 20 days of manure or greater than about 50 days worth of manure. In a preferred embodiment, composting trench  1702  is configured such that the last few days of compost, preferably the last three days of compost, are covered. The cover captures gases that will be used for bioburden reduction and/or for killing the bacteria  16 D as the composting process ceases. 
         [0121]    Referring to  FIG. 2 , composting trench  1702  includes airflow ducts  1706  and a heat conducting water system  1712 . Preferably, each of the airflow ducts  1706  and heat conducting water system  1712  is comprised of a plurality of pipes that are perpendicular to a longitudinal axis of composting trench  1702  (i.e., are perpendicular to flow of the compost). The pipes in the airflow ducts  1706  are preferably separate from the pipes in heat conducting water system  1712 . Preferably, each of the pipes in the airflow ducts  1706  and each of the pipes in heat conducting water system  1712  is about 12 feet long and situated every few feet, i.e., about every 5 feet. Preferably, airflow ducts  1706  are used to regulate, provide, and/or supply airflow to various sections of composting trench  1702 . Preferably, heat conducting water system  1712  is used to distribute the heat generated by the aerobic composting process to various sections of composting trench  1702 . A plurality of manifolds and/or valves within these pipes may be used to distribute the gas/heat to the compost. Preferably, the pipes may be perforated to allow for transport of the process gases throughout composting trench  1702 . For example, the pipes may transport gases such as air, oxygen and/or ammonia produced from the composting process of the present invention to various sections of composting trench  1702 . In this manner, the gases may be distributed where needed. Additionally, composting trench  1702  may include vents. In other embodiments, airflow ducts  106  and/or heat conducting water system  1712  may be omitted and/or replaced with another suitable mechanism. In yet other embodiments, the pipes may be situated parallel to the longitudinal axis of composting trench  1702 . In yet other embodiments, the pipes may not be perforated. In yet other embodiments, the pipes for airflow ducts  1706  and the pipes for heat conducting water system  1712  may not be separate. In yet other embodiments, heat may be controlled and/or distributed via electrical means and/or other non water-based means. In other embodiments, other means of distributing heat and/or controlling may be used, in lieu of, or in addition to, the means of distributing and/or controlling heat described above. 
         [0122]    Referring to  FIG. 18 , composting trench  1702  of composting apparatus  1700  includes crawl space  1708  at top of composting trench  1702 . Preferably, crawl space  1708  is used to enable access to the pipes for the purpose of reconfiguring the pipes and/or for maintenance of the pipes. In other embodiments, crawl space  1708  may be omitted or replaced by another suitable mechanism. 
         [0123]    In a preferred embodiment, the temperature of the biomass does not exceed about 70 degree C. during the aerobic composting process according to present invention. Most preferably, the temperature of the biomass is kept between 50 degree C. and 70 degree C. In order to regulate the compost temperature, the heat generated by the aerobic composting process may be distributed as follows. For example, the aerobic composting process heats water in the pipes of heat conducting water system  1712 . These pipes may distribute heat up and down composting trench  1702  by distributing hot water up and down composting trench  1702 . For example, hot water may be sent to any part of composting trench  1702  via these pipes from a high temperature section of composting trench  1702 . 
         [0124]    In a preferred embodiment, a hood may be used to capture rising water vapor and/or NH 3  and/or NH 4  and CO 2  from the biomass as it generates heat. In yet other embodiments, in lieu of, or in addition to, using a hood to capture rising water vapor or NH 3  and/or NH 4  and CO 2  at least a portion of the roof of composting building  1704  may also be used. Preferably, the roof of the composting building  1704  includes steep eaves or a narrowed roof area to allow a more efficient capture and removal of NH 3  and/or NH 4  and CO 2  from inside composting building  1704 . 
         [0125]    The present invention generally operates as follows. Manure is collected from a CAFOs facility on a continuing basis, as soon as feasible. Preferably, manure is collected from a CAFOs facility within 12 hours of production. The collected manure has a moisture content of about 70-80% by weight. A source of carbon is added, preferably at a ratio of manure to carbon source of about 3:2, resulting in a biomass with a moisture content of preferably about 30%-70% by weight. Most preferably, the resulting biomass has a moisture content of about 50% by weight. Preferably, the source of carbon is sawdust. Other sources of carbon may be used in lieu of, or in conjunction with, sawdust. In addition to providing a carbon source during the aerobic composting process, the nature of the carbon source may also provide porosity to the biomass, improving the speed and efficiency of the capture of composting gases. 
         [0126]    According to an embodiment of the invention, the floor of a CAFOs facility containing manure may be washed periodically, and the water and manure may be collected in a containment pool. The containment pool is preferably enclosed or shielded, such that the NH 3  and CO 2  gasses from the manure composting process cannot escape into the environment. The shielding or enclosure of the containment pool preferably contains a suitable air handling system manufactured to withstand the corrosion associated with NH 3  and CO 2  gases, which is used to collect the NH 3  and CO 2  gasses and to transfer the collected NH 3  and CO 2  gasses to one or more collection tank(s)  1801  which contain an aqueous solution. According to an embodiment of the invention, additional CO 2  gasses may be collected from the atmosphere of the CAFOs facility by means of a suitable air handling system manufactured to withstand the corrosion associated with NH 3  and CO 2  gases. The CO 2  gases collected from the atmosphere of the CAFOs facility are transferred via the air handling system to one or more collection tank(s)  1801 . 
         [0127]    In a preferred embodiment, the source of carbon includes carbon to nitrogen in the ratio of at least about 6:1. In other embodiments, the volume/amount of manure and/or carbon source used in the input may vary, depending on, for example, the capacity of composting trench  1702 . In yet other embodiments, the carbon to nitrogen ratio of the source of carbon may be less than about 6:1 or greater than about 6:1. In yet other embodiments, an additional source of carbon may not be added to the manure, and the manure alone may be used in the composting process of the present invention. 
         [0128]    Referring to  FIG. 17 , the input  1710  of the present invention is preferably manure mixed with a source of carbon to form a biomass having a high solids content for aerobic composting. The resulting biomass is spread around composting trench  1702 , and is moved through composting trench  1702  as the composting process progresses. Preferably, the amount of biomass used in input  1710  is a day&#39;s worth of manure. This amount, of course, will vary depending upon, for example, the amount of available manure and/or sawdust and/or the size of composting apparatus  1700 . A day&#39;s worth of biomass is loaded onto composting trench  1702  daily. As such, a new input may be created everyday and identified as “day 1 compost,” “day 2 compost,” “day 3 compost,” etc. For example, the first day&#39;s biomass would be labeled as “day 1 compost.” The next day, at about the same time, the previous day&#39;s biomass would be moved down the length of the composting trench  1702 , making room for the second day&#39;s biomass. Second day&#39;s biomass is loaded onto composting trench  102  and labeled as “day 2 compost,” and so forth. Preferably, the biomass is added at a specified time of day. To make room for the next day&#39;s biomass, the previous day&#39;s biomass is moved down composting trench  1702  using a rototiller (available from, for example Farmer Automatic of America). This leaves an open space for the next day&#39;s biomass in composting trench  1702 . Preferably, each day&#39;s biomass is moved about 5 feet to about 10 feet down composting trench  1702 . 
         [0129]    Temperature, pH and moisture content of the biomass are controlled by aeration of the biomass both by a physical moving and mixing process, and by the addition of O 2  into composting trench  1702 . Within the biomass, the dissolved ammonia gas NH 3  is in a chemical equilibrium with the NH 4 . The ratio of NH 4  to NH 3  in this equilibrium is pH dependent. Preferably, the pH of the biomass is controlled to keep the alkalinity level of the biomass high so that most of the NH 4  in the biomass is converted to NH 3  and released into the air, and not nitrified by the bacteria  16 D present in the biomass. Preferably, the pH of the biomass is also controlled so that the aerobic bacteria  16 D are not killed by the NH 3  production. In a preferred embodiment, the pH of the biomass is between 8.0 and 10.1. 
         [0130]    Each day&#39;s biomass may be moved once during the day, several times during the day, and/or continuously throughout the day. As the composting process commences, a rototiller may be used to mix/agitate and aerate the biomass. In other embodiments, other means of moving and/or aerating the biomass may be used in lieu, or in conjunction with, the rototiller. In yet other embodiments, biomass may not be added to the composting trench  1702  daily, but may be added more often than that, or less often than that, i.e., every other day. In this manner, the next load of biomass may be added the same day as the previous load, or every other day. The amount of biomass and time intervals between each addition may vary. 
         [0131]    In a preferred embodiment, O 2  is added to the biomass during the aerobic composting process to facilitate the composting reaction. Preferably, the form of O 2  addition is air. Preferably, the rate of O 2  addition is determined by the temperature of the biomass  16 A. Preferably, O 2  is added to any one or more of the day 1 to day 15 allotments of biomass. Preferably, the amount of O 2  added over the length of composting trench  1702  decreases. In this manner, preferably, the amount of O 2  added on day 10 is less than the amount of O 2  added on day 1. In other embodiments, other sources of O 2  may be used and/or other means of controlling O 2  addition may be used. Air ducts  1706  may be used to regulate airflow. This may ensure that bacteria  16 D in the biomass receive an adequate supply of O 2  to complete the composting process. In other embodiments, other means of regulating airflow, in lieu of, or in conjunction with air ducts  1706 , may be used. 
         [0132]    Aerobic bacteria  16 D are provided to highly selectively convert all or substantially all of the waste amino acids, proteins, uric acid and any other available nitrogen compounds in the biomass into NH 3  and/or NH 4  and CO 2 . Preferably, the specific strains of aerobic bacteria  16 D used in the present invention include uricolytic bacteria such as  Bacillus pasteurii  and/or  Peptostreptococcus anaerobius, Clostridium sticklandii, Clostridium aminophilum , and  Eubacterium pyruvativorans . Thermophilic bacteria are preferred because their presence reduces the population of harmful bacteria such as  E. coli, Salmonella  and fecal  coli -form bacteria. During the aerobic composting process, the biomass should remain at a temperature of 50 C. to 70 C. to promote the growth of thermophilic bacteria. The heat to maintain this temperature is supplied by the aerobic composting process and is distributed by heat conducting water system  1712 . Regular aeration of the biomass helps to regulate the temperature as well as supplies the oxygen to the bacteria  16 D. It is not necessary to add external heat to the aerobic composting process to manufacture ammonium sulfate according to the present invention. 
         [0133]    As the aerobic process progresses, the aerobic bacteria  16 D highly selectively convert all or substantially all of the waste amino acids, proteins, uric acid and any other available nitrogen compounds in the biomass into NH 3  and/or NH 4  and CO 2 . The resulting NH 3  and CO 2  gasses are collected from the atmosphere of the composting building  1700  by means of hood  1714  and/or air flow ducts  1706 , or another suitable air handling system manufactured to withstand the corrosion associated with NH 3  and CO 2  gases. Preferably, the air handling system should be capable of changing the building volume of air in less than one hour. 
         [0134]    Referring to  FIG. 19 , the air containing the collected NH 3  and CO 2  gasses is delivered to one or more collection tank(s)  1901  which contain an aqueous solution. The air containing the collected NH 3  and CO 2  gasses is forced by the air handling system to enter the collection tank(s)  1901  through an array of diffuser units  1902 . Preferably, the diffuser units  1902  are adapted to release the collected NH 3  and CO 2  gases into the collection tank(s)  1901  as small gas bubbles, preferably 5 microns to 10,000 microns in diameter. Preferably, the number and size of the diffuser units  1902  is sufficient to ensure that substantially all of the collected NH 3  and CO 2  gasses are removed from the air as the air passes through the collection tank(s)  1901 . After the passage through the collection tank(s)  1901 , the air handling system may recycle the air back to the atmosphere of the composting building  1700  so that any unabsorbed NH 3  and CO 2  remaining in the air may be added back into composting trench  1702 , and/or may be collected for future use or commercial purposes. 
         [0135]    The captured NH 3  and/or NH 4  react with the aqueous solution in collection tank(s)  1901 , and are converted to ammonium hydroxide. The ammonium hydroxide reacts with captured CO 2  to form ammonium polycarbonate. Preferably, the process is allowed continued until the pH in the collection tank(s)  1901  reaches 8.5 to 9.35. Preferably, the process is allowed to continue until the concentration of ammonium polycarbonate in the aqueous solution of the collection tank(s)  1901  reaches a concentration of between 1,600 ppm and 4,500 ppm as measured with an electrical conductivity meter. 
         [0136]    In the preferred embodiment, after the concentration of ammonium polycarbonate in the aqueous solution of the collection tank(s)  1901  reaches a concentration of between 1,600 ppm and 4,500 ppm, the aqueous solution containing ammonium polycarbonate, ammonium hydroxide and CO 2 , is removed from the collection tank(s)  1901  through a first piping system  1903 , and is transferred to one or more pre-osmosis holding tank(s)  1904 . In order to increase the concentration of the ammonium polycarbonate in the aqueous solution, the aqueous solution containing ammonium polycarbonate, ammonium hydroxide and CO 2  is transferred from pre-osmosis holding tank(s)  1904  to one or more reverse osmosis devices  206  through a second piping system  1905 . The reverse osmosis devices may include a DOW™ FILMTEC™ XLE-440 reverse osmosis membrane, or a similar reverse osmosis membrane. The reverse osmosis process allows water to be removed from the aqueous solution resulting in a more concentrated ammonium polycarbonate solution. The removed water is transferred from reverse osmosis device(s)  1906  through a third piping system  1907  to a water holding tank  1908 , and may be reused in the process or discarded. The reverse osmosis process may be repeated as necessary to increase the concentration of the ammonium polycarbonate in the aqueous solution. In other embodiments, the reverse osmosis process may be replaced by other processes suitable for increasing the concentration of the ammonium polycarbonate solution in the aqueous solution, or it may be omitted. 
         [0137]    The aqueous solution containing concentrated ammonium polycarbonate is transferred from reverse osmosis device(s)  1906  through a fourth piping system  1909  to one or more reaction tank(s)  1910 . Sulfate  1912  is added to reaction tank(s)  1910  at a ratio of approximately 5 pounds of sulfate for each 1 gallon of ammonia solution. In certain alternate preferred embodiments of the seventh method, the source of sulfate  1912  preferably comprises Organic Materials Review Institute (“OMRI”) certified organic gypsum. According an embodiment of the present invention, in order to improve the yield of ammonium sulfate, excess sulfate  1912  may be added to reaction tank(s)  1910 , at a ratio of approximately 6 pounds of sulfate for each 1 gallon of ammonia solution. 
         [0138]    The temperature of the aqueous solution containing concentrated ammonium polycarbonate and sulfate  1912  in reaction tank(s)  1910  is raised to 50.degree. C. or allowed to rise to 50.degree. C. due to the chemical reaction between the ammonium carbonate and sulfate  1912 . During the initial reaction period (preferably four hours), the aqueous solution containing concentrated ammonium polycarbonate and sulfate  1912  is mixed and circulated inside reaction tank(s)  1910 , resulting in the formation of ammonium sulfate suspension  1915  and calcium carbonate. The pressure may be allowed to increase in the reaction tank(s)  1910  in order to increase the rate and yield of ammonium sulfate. Preferably, the pressure is allowed to increase to two atmospheric pressures or greater. Calcium carbonate is allowed to settle to the bottom of reaction tank(s)  1910  in the form of the calcium carbonate sludge. In a preferred embodiment, the calcium carbonate sludge is removed from reaction tank(s)  1910  through a floor drain and a fifth piping system  1916  to one or more bag filters  1917  which capture the calcium carbonate sludge. The resulting captured calcium carbonate sludge can be recovered and used as a separate product for various agricultural and non-agricultural purposes. 
         [0139]    After the initial reaction period (preferably four hours), the aqueous solution containing concentrated ammonium polycarbonate, sulfate  1912  and ammonium sulfate suspension  1915  is moved from reaction tank(s)  1910  through a sixth piping system  1913  to one or more holding area tank(s)  1914 , where the presence of unreacted sulfate  1912  in said aqueous solution allows the formation of ammonium sulfate suspension  1915  to proceed for an additional period of time, preferably for more than 5 days. Most preferably, the formation of additional ammonium sulfate suspension  1915  in holding area tank(s)  1914  is allowed to proceed for a period of 10 days. 
         [0140]    According to an embodiment of the invention, the resulting ammonium sulfate suspension  1915  may be centrifuged to remove excess water in order to concentrate the ammonium sulfate suspension  1915  to a desired density for use as a liquid fertilizer. In other embodiments, the centrifugation process may be replaced by other processes suitable for increasing the concentration of the ammonium sulfate suspension  1915 . According to an embodiment of the invention, the ammonium sulfate suspension  1915  may be dried to form crystals of dry ammonium sulfate. The resulting liquid or dry ammonium sulfate is certifiable as organic. The term “organic” as used herein, is a labeling certification term that refers to an agriculture product produced in accordance with the Code of Federal Regulations (“CFR”) Title 7 (Subtitle B, Chapter I, Subchapter M, Part 205). 
         [0141]    The foregoing disclosures and statements are illustrative only of the Present Invention, and are not intended to limit or define the scope of the Present Invention. The above description is intended to be illustrative, and not restrictive. Although the examples given include many specificities, they are intended as illustrative of only certain possible configurations or aspects of the Present Invention. The examples given should only be interpreted as illustrations of some of the preferred configurations or aspects of the Present Invention, and the full scope of the Present Invention should be determined by the appended claims and their legal equivalents. Those skilled in the art will appreciate that various adaptations and modifications of the just-described preferred embodiments can be configured without departing from the scope and spirit of the Present Invention. Therefore, it is to be understood that the Present Invention may be practiced other than as specifically described herein. The scope of the present invention as disclosed and claimed should, therefore, be determined with reference to the knowledge of one skilled in the art and in light of the disclosures presented above.