Patent Publication Number: US-2021171412-A1

Title: Processes and systems for producing ammonia products and/or calcium carbonate products

Description:
CROSS REFERENCE TO RELATED APPLICATIONS 
     This application claims the benefit of U.S. Provisional Application No. 62/934,279 filed Nov. 12, 2019, the contents of which are incorporated herein by reference. 
    
    
     BACKGROUND OF THE INVENTION 
     The present invention generally relates to systems and processes capable of producing ammonia products and/or calcium carbonate products, and in particular systems and processes capable of producing organic high sulfur liquid ammonium products and optionally organic calcium carbonate products from an effluent derived from one or more organic feedstocks. 
     High yields and healthy growth in food crops, gardens, and lawns require a high soil nitrogen content. High ammoniacal nitrogen fertilizers are commonly used to meet this need by delivering the necessary nitrogen directly to soil and crops. However, most high ammoniacal nitrogen fertilizers currently available are synthetic fertilizers which precludes them from being used to produce organic crops, one of the fastest-growing sectors of the agricultural economy. In the United States, organic crops are regulated by the National Organic Program (NOP) standards developed under the Organic Foods Production Act of 1990 (7 C.F.R. § 205), and the term “organic crops” is used herein consistent with the NOP standards. By 2031, the demand for organic fertilizer with high nitrogen content is predicted to increase tenfold in the United States. Currently, very few companies offer an organic fertilizer that meets these needs. 
     Animal waste in the form of livestock manure has been a liability for large dairy farms and other Confined Animal Feeding Operations (CAFOs). Nutrients in manure, particularly in the liquid fraction (effluent) of manure, have the potential to leach into nearby bodies of water, producing a source of pollution and creating a major liability for animal feeding operations. Some processes, specifically anaerobic digestion and biogas production, have proved to be effective at removal of pathogens and harmful greenhouse gases from effluent. However, there are many shortcomings of these processes and many CAFOs continue to search for improved means for sustainably processing their effluent. 
     In view of the above, it can be appreciated that it would be desirable if systems and processes were available for producing high nitrogen content organic fertilizer, particularly from effluent derived from livestock manure. 
     BRIEF DESCRIPTION OF THE INVENTION 
     The present invention provides systems and processes capable of producing ammonia products and/or calcium carbonate products, including but not limited to an organic high sulfur liquid ammonium product and an organic calcium carbonate product from an effluent derived from one or more organic feedstocks. 
     According to one aspect of the invention, a process is provided that includes providing an organic feedstock that contains at least one nitrogen compound, removing solids from the organic feedstock to produce an organic liquid effluent that contains at least one of ammonium and ammonia, stripping and concentrating ammonia from the organic liquid effluent to produce a gaseous mixture that contains ammonia, cooling the gaseous mixture to produce a condensed aqueous ammoniacal nitrogen solution comprising one or more of aqueous ammonia, ammonium bicarbonate, and ammonium carbonate, and contacting the condensed aqueous ammoniacal nitrogen solution with a stabilizing agent to cause a reaction therebetween to produce at least a stabilized ammoniacal nitrogen product. 
     According to another aspect of the invention, a process is provided that includes preparing an organic feedstock that contains at least one nitrogen compound by causing organic animal manure and/or organic food waste to undergo anaerobic digestion, removing solids from the organic feedstock to produce an organic liquid effluent that contains at least one of ammonium and ammonia, stripping and concentrating ammonia from the organic liquid effluent to produce a gaseous mixture that contains ammonia, cooling the gaseous mixture to produce a condensed aqueous ammoniacal nitrogen solution comprising one or more of aqueous ammonia, ammonium bicarbonate, and ammonium carbonate, and contacting the condensed aqueous ammoniacal nitrogen solution with gypsum to cause a reaction therebetween and produce calcium carbonate and at least a stabilized ammoniacal nitrogen product that contains ammonium sulfate. 
     According to another aspect of the invention, a system is provided that includes a filtration system configured to remove solids from an organic feedstock that contains at least one nitrogen compound and produce an organic liquid effluent that contains at least one of ammonium and ammonia, means for stripping and concentrating ammonia from the organic liquid effluent to produce a gaseous mixture that contains ammonia, means for cooling the gaseous mixture to produce a condensed aqueous ammoniacal nitrogen solution comprising one or more of aqueous ammonia, ammonium bicarbonate, and ammonium carbonate, and means for reacting a stabilizing agent with the condensed aqueous ammoniacal nitrogen solution to produce a stabilized ammoniacal nitrogen product. 
     Technical effects of the processes and system described above preferably include the ability to produce high nitrogen content organic fertilizers from organic effluents. 
     Other aspects and advantages of this invention will be appreciated from the following detailed description. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         FIG. 1  schematically represents a process of producing stabilized ammoniacal nitrogen products in the forms of a high sulfur liquid ammonia product and a dried high sulfur ammonium product in accordance with certain nonlimiting aspects of the invention. 
         FIG. 2  schematically represents a nonlimiting embodiment of a system for producing an organic stabilized ammoniacal nitrogen product in accordance with certain nonlimiting aspects of the invention. 
         FIG. 3  schematically represents an isolated view of a product section of the system of  FIG. 2 . 
         FIG. 4  schematically represents an isolated view of an alternative embodiment of the product section of the system of  FIG. 2  in accordance with certain nonlimiting aspects of the invention. 
     
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
     The following disclosure describes various aspects of systems and processes that are schematically represented in  FIGS. 1 through 4 . Although the invention will be described hereinafter in reference to particular features/functions schematically identified in the drawings, it should be noted that the teachings of the invention are not limited to these particular features/functions, and the invention does not require all of the features/functions or the interfunctionality represented in the drawings. 
       FIG. 1  schematically represents general steps that may be included in systems and processes for producing one or more stabilized ammoniacal nitrogen products, including but not limited to an organic liquid fertilizer with high ammoniacal nitrogen and sulfur contents. The term “ammoniacal nitrogen” will be used herein to refer to nitrogen that is contained in ammonium and/or ammonia, and preferably can be provided to a plant in a water-soluble form that is readily available to the plant for use as a nutrient. For convenience, the processing steps will be described as being organized into three sections that include a pre-treatment section, a distillation section, and a product section. However, this should not be interpreted as limiting the scope of the invention as the processes could include additional or fewer steps, and/or the represented steps may be characterized differently and/or include additional or fewer components. 
     In  FIG. 1 , the pre-treatment section involves the processing of an organic feedstock, referred to in  FIG. 1  as a liquid organic waste, to yield a liquid organic waste filtrate (sometimes referred to herein as an “organic liquid effluent” or simply “effluent”) that contains ammonium (NH 4   + ), or ammonia (NH 3 ), or both ammonium and ammonia. In the example given, solids are removed from the organic feedstock by filtration to produce the liquid organic waste filtrate. In the distillation section, the liquid organic waste filtrate undergoes a distillation process that includes stripping from the liquid organic waste filtrate a gaseous mixture (“Tops Vapor”) that contains ammonia, water vapor, and may further include hydrogen sulfide, carbon dioxide, and other volatile compounds, which is concentrated and then undergoes condensation to produce a condensed aqueous ammoniacal nitrogen solution that will typically also contain ammonium bicarbonate and/or ammonium carbonate. An ammonium carbonate product produced during the distillation process may be collected and removed in this section. In the product section, the condensed aqueous ammoniacal nitrogen solution is contacted with a stabilizing agent, which in the nonlimiting embodiment of  FIG. 1  is represented as gypsum, to stabilize and concentrate stabilized products resulting from a reaction between the condensed ammonia-containing liquid and the gypsum. The stabilized products are identified in  FIG. 1  as a calcium carbonate product, a stabilized ammoniacal nitrogen product referred to as a high sulfur liquid ammonia product, and a concentrated liquid that contains sulfur and ammoniacal nitrogen. Optionally, the concentrated liquid may be dried to produce a dried high sulfur ammonium product, such as ammonium sulfate fertilizer, and a recovered water vapor. 
     The term “stabilized” as used in reference to stabilized ammoniacal nitrogen products refers to products that are not and do not contain gaseous ammonia, which would be objectionable for safety and environmental reasons, and instead the ammonia and nitrogen are contained in stable compounds. The stabilized products produced in the process of  FIG. 1  are preferably organic products, more particularly certified organic products, which as used herein refer to products that are produced in accordance with the standards of the National Organic Program (NOP) developed under the Organic Foods Production Act of 1990 (7 C.F.R. § 205) such that the products can be approved for use as an input in organic crop production. Organic products can also refer to products and fertilizers approved by third party organic certifying agencies using similar guidelines to the National Organic Program. 
     In view of the desire to produce organic products, it should be understood that the terms “organic feedstock” or “organically derived feedstock” refer to entirely natural source materials having a high ammoniacal nitrogen content from which the liquid organic waste filtrate (effluent) used herein is produced. These natural source materials may include, but are not limited to, animal manure (including cattle manure effluent and hog manure effluent), organic food waste, blood meal, feather meal, guano, bone meal, and wastewater from a variety of food and liquid processing operations. The organic feedstock is preferably anaerobically digested to remove pathogens and convert organic matter into ammoniacal nitrogen. As known in the art, anaerobic digestion is a collection of processes by which microorganisms break down biodegradable material (biomass) within a digester and in the absence of oxygen. Within a digester, various types of bacteria may be used to break down the biomass into byproducts including biogas (e.g., methane, carbon dioxide, etc.) and a liquid effluent, commonly referred to as digestate. Although synthetic substances may not necessarily inhibit or have a significant effect on the processes disclosed herein or their ability to produce high nitrogen fertilizers, to achieve organic certification under the National Organic Program standards, the feedstock is preferably digested while avoiding any contact with any synthetic substances or materials, such as polymers that are commonly used in certain anaerobic digestion processes. Effluents produced from these feedstocks and processed as described herein preferably do not contain any suspended solids greater than 15 microns, and preferably have a total suspended solids (TSS) of about 2.5% or less. 
     Also consistent with the desire to produce organic products, additives used in the process represented in  FIG. 1  are also preferably organic products. As such, the gypsum (a mineral containing calcium, sulfur, oxygen, and water in the form of CaSO 4 .2H 2 O) used in  FIG. 1  is preferably certified as derived from an organic source under relevant organic certifying institutions&#39; standards. 
       FIG. 2  schematically represents a nonlimiting embodiment of a system and process for producing an organic stabilized ammoniacal nitrogen product capable of high ammoniacal nitrogen and sulfur contents. In this embodiment, organic waste material is sourced from an animal feedlot  1  and processed in an anaerobic digester  2  to produce a digestate. The digester  2  may be a component of the system represented in  FIG. 2  or the digestate produced therefrom may be delivered from a remote operation comprising the digester  2 . Alternatively, storage such as a lagoon of liquid manure or a solid mass of manure in which anaerobic digestion can occur may be used instead of the digester  2 . 
     Suspended solids are preferably removed from the digestate, for example, to produce an effluent having the aforementioned maximum suspended solids particles size of not greater than 15 microns and a total suspended solids (TSS) of about 2.5% or less. In  FIG. 2 , the equipment represented for removing solids from the digestate include a centrifuge  3  and filter unit  4 , for example, a fiber press, a screen, or ultrafiltration equipment, though time and gravity in a lagoon may by itself be adequate. A combination of two or more filtration methods is preferred to ensure adequate solids removal. The resulting effluent is likely to be at a temperature of about 100° F. (about 35° C.) and may contain about 1800 ppm of ammonium and/or ammonia, likely nitrogen in forms other than ammoniacal nitrogen, as well as hydrogen sulfide (H 2 S), carbon dioxide (CO 2 ), other volatile organics, and certain levels of calcium, iron, magnesium, sodium, potassium, phosphorus, manganese, etc. 
     The effluent is generally the product of a pre-treatment section of the system of  FIG. 2 , and is transferred with a pump  5  to a means capable of stripping and concentrating ammonia from the effluent. Various means can be used for this purpose, as a nonlimiting example, a distillation tower  15  that forms part of a distillation section of the system. However, other means are foreseeable, as nonlimiting examples, air strippers, thin film evaporators, etc. The effluent is preferably at an elevated temperature when it is enters the distillation tower  15 . For this reason, a heat exchanger  6  may be used to raise the temperature of the effluent over 90° F. (about 30° C.), for example at least 180° F. (about 80° C.), and more preferably in the range of 180° F. to 200° F. (80° C. to 95° C.). 
     The distillation tower  15  is preferably a packed media column, although other distillation methods such as sieve trays or valve trays may be used. Within the distillation tower  15 , the heated effluent enters a stripping section  7  configured to strip and remove ammonia from the effluent. In the nonlimiting embodiment represented in  FIG. 2 , a boiler  31  is used to generate steam for this purpose. The steam is preferably at a pressure of least 15 psi (about 100 kPa) and at least 250° F. (120° C.). The ammonia is removed from the effluent by provoking the effluent to cover the packed media, which increases the surface area of the effluent and accelerates the mass transfer of ammonia from liquid to gas. The gaseous ammonia is concentrated in a concentration section  8  of the distillation tower  15  located above the stripping section  7  before exiting the tower  15  through a conduit  11  at the top of the tower  15 . 
     The gaseous ammonia is entrained in a gaseous mixture (Tops Vapor in  FIG. 1 ) that may further include water vapor, hydrogen sulfide, carbon dioxide, and other volatile compounds. The gaseous mixture is preferably at a temperature of between 150° to 212° F. (35° C. to 100° C.), more preferably 180° to 200° F. (80° C. to 95° C.), most preferably about 190° F. (90° C.). The gaseous mixture preferably has an ammonia concentration above 10%, more preferably above 12%, and most preferably above 15%. 
     The gaseous mixture is conducted to a condenser  12  where the gaseous mixture is condensed to yield a condensed aqueous ammoniacal nitrogen solution that contains aqueous ammonia, ammonium bicarbonate, and/or ammonium carbonate. The condenser  12  is represented in  FIG. 2  as a reflux condensing loop having a cooling coil  13  fed with water, air, or glycol coolant  13   a.  Though represented as external of the tower  15 , condensers incorporated into the top of the tower  15  are also foreseeable. In the embodiment shown, the condenser  12  is configured to recycle a portion of the condensed aqueous ammoniacal nitrogen solution back to the tower  15  through a pump  14  to raise the concentration of ammonia within the concentration section  8  to increase the efficiency of ammonia removal from the effluent. The tower  15  is preferably operated at an ammonia removal efficiency of at least 80%, more preferably 90%, and most preferably 95% or more. 
     The tower  15  also releases a liquid mixture  9  (bottoms liquid in  FIG. 1 ) that includes, without limitation, condensed steam and heated effluent. The heated liquid mixture  9  exits through a tank  10  located at a lower end of the tower  15  and passes through the heat exchanger  6  to transfer heat to the effluent entering the system. After the heat exchanger  6 , the liquid mixture  9  may be removed to a lagoon  39  for storage, for example, if the system is constructed at a Confined Animal Feeding Operation or other operation that has use of the liquid mixture  9 . 
     The distillation tower  15  is preferably constructed to maintain organic process controls as defined by the National Organic Program and/or other relevant institutions. This includes, without limitation, the total absence of synthetic substances in areas that come into contact with the effluent and product as well as precautions to ensure that potential spills or leaks cannot introduce synthetic materials to the system. Additionally, organic process controls are preferably applied to the maintenance, operation, and sanitation of the equipment. Automation may also be used in the system to efficiently regulate the temperature and pressure inside the system. 
     A fraction of the gaseous mixture that enters the condenser  12  and a fraction of the condensed aqueous ammoniacal nitrogen solution condensed within the condenser  12  are shown in  FIG. 2  as being separately transported to a product section of the system, and particularly to a water bath within a tank  17  that contains water and dissolved gypsum, which serves to stabilize the ammonium in the gaseous mixture and allows ammonium in the condensed aqueous ammoniacal nitrogen solution to remain in a liquid form as ammonium carbonate ((NH 4 ) 2 CO 3 ) when mixed with water. The tank  17  facilitates a reaction between the gypsum and the ammonium carbonate, which as shown in Equation 1 produces calcium carbonate (CaCO 3 ) and, as a stabilized ammoniacal nitrogen product, ammonium sulfate ((NH 4 ) 2 SO 4 ). In certain embodiments, the gaseous mixture exiting the condenser  12  may be condensed before entering the water bath. In such an embodiment, the gaseous mixture takes the form of a liquid ammonium carbonate solution when it enters the water bath. 
       CaSO 4 .2H 2 O+(NH 4 ) 2 CO 3 →CaCO 3 +(NH 4 ) 2 SO 4 +2H 2 O   Eq. 1
 
       FIG. 3  represents an isolated view of the product section of the system of  FIG. 2 . As seen in  FIGS. 2 and 3 , the gaseous mixture drawn from the condenser  12  is transported through a conduit  38  and then a heat exchanger  40  into the water bath of the tank  17 . The concentration of ammonia in the gaseous mixture at this point in the system preferably does not exceed 18% by weight. As represented, the system includes at least a second tank  19  connected to the first tank  17 . Each tank  17  and  19  is preferably pressurized and contains a mechanical mixing mechanism  17   a  and  19   a  to mix the gypsum with the dissolved ammonium carbonate of the condensed aqueous ammoniacal nitrogen solution (collectively referenced by  41  and  42  in tanks  17  and  19 , respectively) inside the tanks  17  and  19 . 
     The first tank  17  contains a relatively small amount of gypsum, which quickly reacts with the ammonium carbonate in the condensed aqueous ammoniacal nitrogen solution. The first tank  17  also includes a small amount of ammonium sulfate and a small amount of calcium carbonate as a result of the reaction of Equation 1. The calcium carbonate formed in the tank  17  exits the tank  17  via a circulation stream  29  from which the calcium carbonate is removed with a filter  30 . The resulting filtered calcium carbonate stream  44  may be dried, for example, with a dryer/evaporator  33 , to produce dried cakes thereof to be stored in a storage vessel  34 . A filtrate slurry  32  containing the remaining ammonium carbonate and ammonium sulfate originally in the circulation stream  29  enters the second tank  19 , which contains a higher concentration of gypsum than the tank  17  as a result of gypsum being directly added to the tank  19  from a gypsum source  24 . In addition, excess gases  18  from the first tank  17  may be diverted to the second tank  19 . 
     Within the second tank  19 , the gypsum reacts quickly with the ammonium carbonate, so that the reaction products within the tank  19  are primarily ammonium sulfate and calcium carbonate. The resulting slurry stream  20  containing ammonium sulfate, gypsum, and calcium carbonate exits the tank  19 , and a stabilized ammoniacal nitrogen product  35  (primarily an ammonium sulfate solution) is removed from the slurry stream  20  with a filter  27  before being sent to the concentration stages of the process. In  FIGS. 2 and 3 , the stabilized ammoniacal nitrogen product  35  may be transported to a liquid storage tank  21  or further dried with a dryer/evaporator  36  to produce solid ammonium sulfate crystals and stored in storage vessel  37 . A slurry  28  containing gypsum, calcium carbonate, and ammonium sulfate is also shown as being drawn from the second tank  19  and transported to the first tank  17  to be used in the reactions that occur there. Excess gases  25  such as carbon dioxide (CO 2 )  25   a  and hydrogen sulfide (H 2 S)  25   b  may be removed from the second tank  19 . Optionally, a production system  26  may be included to produce iron sulfide from the excess gases  25 . The stabilized ammoniacal nitrogen product  35  collected in the tank  21  may be packaged as a liquid ammonium sulfate solution fertilizer  22 . Alternatively or in addition, a fraction of the condensed aqueous ammoniacal nitrogen solution produced by the condenser  12  may be collected in a storage tank  16  and packaged as a liquid fertilizer  22 . 
       FIG. 4  represents an isolated view of an alternative embodiment of the product section of the system of  FIG. 2 . In this embodiment, represented as a batch process, the gaseous mixture transported by the conduit  38  is drawn through a compression pump  112  and delivered to a single mixing tank  114 , instead of the series of tanks  17  and  19  shown in  FIGS. 2 and 3 . The mixing tank  114  is preferably a pressurized tank and contains a mechanical mixing mechanism  115  to mix the gaseous mixture with gypsum from a gypsum source  111  and dissolved ammonium carbonate of the condensed aqueous ammoniacal nitrogen solution drawn from the condenser  12 . The condensed aqueous ammoniacal nitrogen solution and gypsum are respectively represented by  117  and  118  in the tank  114 . The temperature in the tank  114  is preferably 90° F. to 130° F. (about 30° C. to 55° C.), more preferably 100° F. to 120° F. (about 35° C. to 50° C.), and most preferably about 105° F. (about 40° C.). The mechanical mixing in the tank  114  is preferably maintained at about 200 RPM, preferably for a duration of 4 to 12 hours, more preferably 6 to 10 hours, and most preferably about 8 hours. The batch process is not necessarily limited to a single tank  114  and additional embodiments can include multiple vessels with mechanical mixing in each. Optionally, a water-cooled condenser  116  may be coupled to the tank  114 . A stabilized ammoniacal nitrogen product (primarily an ammonium sulfate solution) produced in the tank  114  may be removed and stored in a liquid storage tank  120 , from which it may undergo further processing such as drying as described in reference to  FIGS. 2 and 3 . 
     In all embodiments of the water bath (tanks  17 , 19 , and  114 ), the resulting liquid is removed and heated to increase the concentration of ammonia and sulfur in the liquid. Although not shown, the ammonium sulfate solution can be diverted to a mechanical dryer to evaporate all the water off the product to create solid ammonium sulfate crystals using components similar to those represented in  FIG. 3 , which can be used as a solid ammonium sulfate fertilizer. The drying process preferably creates water vapor, which can be diverted for use in the earlier stages of the process, preferably the distillation section. 
     The systems and processes described above produce a liquid or solid organic fertilizer containing soluble ammoniacal nitrogen. The majority of organic fertilizers currently commercially available contain relatively low levels of nitrogen in forms that are slowly released over the course of weeks or even months. In contrast, the ammoniacal nitrogen in the products produced by the processes described herein is immediately available to plants/crops upon contact with the fertilizer. 
     The liquid fertilizer produced preferably has a pH between 4.5 and 7.5, most preferably about 5 to about 6. The pH of the liquid fertilizer can additionally be stabilized with citric acid in a further embodiment, a natural additive that does not disqualify the fertilizer from qualifying as certified organic. The ammoniacal nitrogen in the liquid fertilizer is preferably in concentrations between 4 and 9%, more preferably 6 to 8% and, most preferably about 7%. The sulfur in the liquid fertilizer is preferably in a concentration of 4.5 to 10%, more preferably 7 to 9%, and most preferably about 8%. 
     The dry fertilizer produced in the embodiments containing a dryer may contain up to about 21% nitrogen and up to about 24% sulfur, and possibly more. The higher nitrogen content in the dry fertilizer may lead organic certifying agents to require the fertilizer to be mixed with compost or only be used to supply 20% of a crop&#39;s nitrogen needs during a single harvest. 
     The fertilizer produced is not necessarily an ammonium sulfate solution. When the nitrogen and sulfur contents are outside of a ratio of about 7:8, the solution can be considered ammoniacal nitrogen with a high sulfur content. Using gypsum to produce ammonium sulfate is similar to the use of gypsum in a composting operation to prevent nitrogen loss. The increase in sulfur in the solution is an added bonus, providing an additional nutrient to the nitrogen solution that is widely sought after in organic farming. Currently, very few fertilizers commercially available offer significant sulfur content. 
     The fertilizer produced is preferably produced in accordance with the standards of the National Organic Program and other relevant organic certifying institutions in order for the fertilizer to be approved as an input in organic crop production. The fertilizer produced is concentrated and easy to transport compared to other organic fertilizers on the market including compost, feather meal, urea, and other products, reducing the carbon footprint of organic crop production. The dry fertilizer can also be mixed with current composts and other fertilizers on the market, necessitating smaller amounts of compost and other fertilizers to be transported. 
     The fertilizer produced also sequesters carbon dioxide in the form of calcium carbonate during the ammonium sulfate production process. The carbon dioxide sequestered would otherwise be released into the atmosphere if the effluent used in the system was disposed of otherwise. The carbon dioxide sequestered amounts to roughly 1.5 pounds (about 0.7 kg) of carbon per pound (about 0.5 kg) of nitrogen in the fertilizer. This equates to roughly 1.5 carbon credits per 880 gallons (about 10,900 L) of fertilizer applied. 
     In investigations leading to aspects of the present invention, the above-noted process was used in the production of dry ammonium sulfate using an automated 24 foot (about 7.3 m) tall distillation tower connected to a 110,000 BTU (about 116,056 kJ) boiler. Specifically, 0.3 gallons (about 1.14 L) per minute of digested dairy cow manure effluent containing 1800 ppm ammonia filtered to 15 microns was preheated to 150° F. (about 65° C.) using a heat exchanger and then further heated to 180° F. (about 80° C.) using another heat exchanger before entering the tower. The second heat exchanger used heat captured from the Bottoms exiting the distillation tower at approximately 210° F. (about 100° C.). 
     The 180° F. (80° C.) effluent was pumped to the distillation tower to a point 16 feet (about 4.9 m) high on the tower. The tower was a packed media distillation column with a six inch (about 15 cm) diameter in the ammonia stripping portion. Live steam from the boiler was injected into the tower at 12 to 15 psi (about 82 to about 104 kPa) above the bottoms collection tank at the base of the tower. The ammonia from the effluent was stripped in the lower 16 feet (about 4.9 m) of the tower and then concentrated in the upper 8 feet (about 2.5 m) of the tower. The concentration portion had a diameter of 6 inches (about 15 cm) at the feed line to 2 inches (about 5 cm) at the top. CO 2  and H 2 S was also stripped from the manure in the column. A mixture of ammonia, CO 2 , H 2 S, and water vapor exited the top of the tower as a gaseous mixture at approximately 180° F. (about 80° C.). 
     The concentration of the ammonia occurred using internal reflux condensation in jacketed cooling cans in the tower. Cold groundwater was run through the jacketed portions and the flow of the water was managed by control valves. The distilled gaseous mixture was piped into a multi-staged gypsum slurry bath resulting in the production of ammonium sulfate and calcium carbonate slurry. The gypsum bath was maintained at approximately 110° F. (about 43° C.). The calcium carbonate was filtered out of the slurry resulting in an ammonium sulfate liquid. The calcium carbonate was dried resulting in a calcium carbonate cake. 
     Analysis of the liquid ammonium sulfate product concluded that the product contained at least 3% ammoniacal nitrogen and at least 3.4% sulfur. A portion of the liquid ammonium sulfate product was evaporated and dried to produce dry ammonium sulfate crystals. Lab analysis showed that there was more than an 80% ammonia removal efficiency from the effluent. 
     While the invention has been described in terms of specific embodiments, it is apparent that other forms could be adopted by one skilled in the art. For example, the physical configuration of the system could differ from that shown, and materials and processes/methods other than those noted could be used. Therefore, the scope of the invention is to be limited only by the following claims.