Manufacturing process for producing ammonia from anaerobic digestate liquid

Abstract

The present invention relates to organic nitrogen fertilizers and methods for producing organic nitrogen fertilizers, including retrieving high concentration organic ammonia from discarded organic material.

Claims

1. A method of producing organic ammonia, comprising: a. heating a nitrogen-containing organic substrate in an anaerobic digester device to drive a biological anaerobic digestion of the substrate to yield a digestate; b. collecting an effluent of the digestate; c. mixing the effluent with air, and heating said effluent in a first chamber separate from said digester to evolve CO.sub.2-laden gas from the effluent and collecting said CO.sub.2-laden gas from said first chamber to yield a decarbonized effluent in the first chamber; d. aerating said decarbonized effluent with air and heating the decarbonized effluent-air mixture to evolve NH.sub.3 from said decarbonized effluent in a second chamber and removing NH.sub.3 vapor; and e. cooling the NH.sub.3 vapor to yield an aqueous NH.sub.3 product derived from said nitrogen-containing organic substrate without chemical reactions.

2. The method of claim 1, wherein mixing the effluent with air comprises injecting air into the effluent by passing the effluent through a first Venturi injector tube and injecting air into the effluent through an injection port.

3. The method of claim 2, wherein said aerating the decarbonized effluent to evolve said NH.sub.3 from the decarbonized effluent includes passing the decarbonized effluent through a second Venturi injector tube and injecting air into the decarbonized effluent through a second injection port.

4. The method of claim 1, further comprising injecting said NH.sub.3 vapor into a cooled aqueous NH.sub.3 solution to resorb NH.sub.3 from the NH.sub.3 vapor during said step of cooling the NH.sub.3 vapor, wherein injecting said NH.sub.3 vapor into a cooled aqueous NH.sub.3 solution includes passing the cooled aqueous NH.sub.3 solution through a third Venturi injector tube and injecting the NH.sub.3 vapor into the cooled aqueous NH.sub.3 solution through a third injection port.

5. The method of claim 1, further comprising transferring the decarbonized effluent to a filtering apparatus and filtering the decarbonized effluent to yield water, and supplying said water to a collection chamber.

6. A method of producing organic ammonia, comprising: a. heating a nitrogen-containing organic substrate in a digestion chamber to yield a nitrogen-rich digestate; b. collecting an effluent of the digestate; c. heating said effluent to evolve CO.sub.2-laden gas from the effluent in a first chamber to lower a pH of said effluent and to produce a decarbonized effluent; d. passing the decarbonized effluent through Venturi injector tube and injecting air into the decarbonized effluent to cause degassing of NH.sub.3 vapor within a second chamber; and e. collecting and cooling the NH.sub.3 vapor in a third chamber to yield an aqueous NH.sub.3 solution.

7. The method of claim 6, wherein said step of heating said effluent drives the chemical equilibrium of ammonium bicarbonate toward the production of NH.sub.3 and CO.sub.2.

8. The method of claim 6, further comprising injecting air into the effluent during the step of heating said effluent to produce said decarbonized effluent, wherein injecting air into the effluent includes passing the effluent through a second Venturi injector tube and injecting air into the effluent through the Venturi injection port.

9. The method of claim 6, further comprising injecting said NH.sub.3 vapor into said aqueous NH.sub.3 solution to resorb NH.sub.3 from the NH.sub.3 vapor, wherein injecting said NH.sub.3 vapor into said aqueous NH.sub.3 solution includes passing the aqueous NH.sub.3 solution through a third Venturi injector tube and injecting the NH.sub.3 vapor into the aqueous NH.sub.3 solution through the Venturi injection port of the third Venturi injector tube.

10. The method of claim 6, further comprising adding a basic chemical agent to the decarbonized effluent before or during the step of extracting NH.sub.3 from said decarbonized effluent.

11. The method of claim 6, further comprising transferring the decarbonized effluent to a filtering apparatus and filtering the decarbonized effluent to yield water, and supplying said water to a collection chamber.

12. The method of claim 6, further comprising injecting CO.sub.2 into said aqueous NH.sub.3 solution to lower the pH of the aqueous NH.sub.3 solution to aid in resorbing NH.sub.3 from the NH.sub.3 vapor, wherein injecting said CO.sub.2 into said aqueous NH.sub.3 solution includes passing the aqueous NH.sub.3 solution through a third Venturi injector tube and injecting the CO.sub.2 into the aqueous NH.sub.3 solution through the Venturi injection port of the third Venturi injector tube.

13. A method of producing organic ammonia, comprising: a. collecting a nitrogen-containing effluent from an anaerobic digestion process; b. mixing the effluent with air, and heating said effluent in a first chamber separate from an anaerobic digester to evolve CO.sub.2-laden gas from the effluent to yield a decarbonized effluent in the first chamber; c. aerating said decarbonized effluent with air and heating the decarbonized effluent-air mixture to evolve NH.sub.3 from said decarbonized effluent in a second chamber and removing NH.sub.3 vapor; and d. cooling the NH.sub.3 vapor to yield an aqueous NH.sub.3 product derived from said effluent.

14. The method of claim 13, wherein mixing the effluent with air comprises injecting air into the effluent by passing the effluent through a first Venturi injector tube and injecting air into the effluent through an injection port.

15. The method of claim 14, wherein said aerating the decarbonized effluent to evolve said NH.sub.3 from the decarbonized effluent includes passing the decarbonized effluent through a second Venturi injector tube and injecting air into the decarbonized effluent through a second injection port.

16. The method of claim 13, further comprising injecting said NH.sub.3 vapor into a cooled aqueous NH.sub.3 solution to resorb NH.sub.3 from the NH.sub.3 vapor during said step of cooling the NH.sub.3 vapor, wherein injecting said NH.sub.3 vapor into a cooled aqueous NH.sub.3 solution includes passing the cooled aqueous NH.sub.3 solution through a third Venturi injector tube and injecting the NH.sub.3 vapor into the cooled aqueous NH.sub.3 solution through a third injection port.

17. The method of claim 16, further comprising concentrating said aqueous NH.sub.3 solution to a concentration of NH.sub.3 and other ammoniacal species in a range of about 3% to about 30% by weight.

18. The method of claim 13, wherein said heating said effluent drives the chemical equilibrium of ammonium bicarbonate toward the production of NH.sub.3 and CO.sub.2.

19. The method of claim 13, further comprising transferring the decarbonized effluent to a filtering apparatus and filtering the decarbonized effluent to yield water, and supplying said water to a collection chamber.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 provides a schematic view of an ammonia capture system, according to an embodiment of the present invention.

(2) FIG. 2 provides a schematic view of collection apparatus of an ammonia capture system, according to an embodiment of the present invention.

DETAILED DESCRIPTION

(3) Reference will now be made in detail to certain embodiments of the invention, examples of which are illustrated in the accompanying drawings. While the invention will be described in reference to these embodiments, it will be understood that they are not intended to limit the invention. To the contrary, the invention is intended to cover alternatives, modifications, and equivalents that are included within the spirit and scope of the invention. In the following disclosure, specific details are given to provide a thorough understanding of the invention. However, it will be apparent to one skilled in the art that the present invention may be practiced without all of the specific details provided.

(4) Reference will be made to the exemplary illustrations in the accompanying drawings, and like reference characters may be used to designate like or corresponding parts throughout the several views of the drawings.

(5) The present invention concerns systems and methods of extracting ammonia, ammonium, and derivatives thereof from digestate liquids produced through anaerobic digestion processes. The extracted ammonia and related compounds can then be incorporated into organic fertilizer compositions. The ammonia and other nitrogenous compounds may be recovered from the digestate generated by an anaerobic digestion process using a digester and ammonia recovery system, as described herein.

(6) FIG. 1 of the present invention provides a system view of an exemplary system for extracting ammonia and related compounds and derivatives from organic wastes, which may be mixed with various feedstocks. The organic wastes may be processed through a non-chemical microbe-mediated digestion process to produce a liquid byproduct rich in ammonia and ammonium compounds. The system 1000 may include several separation stages to generate and separate ammonia and related compounds and derivatives, and, optionally, other useful byproducts, such as methane.

(7) In some implementations, the organic waste may be added into the digester 1001 from a reservoir 1003 for each digestion process. One or more organic substrate sources, including plant biomass, manure, other animal waste, municipal and food wastes may be stored in and supplied from the reservoir 1003. Other co-substrates for purposes of balancing the chemistry of co-digestion and to facilitate the generation of ammonia and ammonium compounds in the biodigestion process may be fed from separate reservoirs 1004a-1004n. For example, a high protein supplement feedstock may be provided from 1004a, such as for providing non-synthetic high-protein supplements such as blood meal, blood, soy meal, soy derived proteins, meat meal (slaughter house waste), feather meal, fish and fish by-products, whey, milk, dairy by-products, alfalfa, corn, and sweet clover. Fermentation of high levels of proteins from animal derived co-substrates result in increased formation of ammonia. Thus, high protein co-substrates increase the amount of ammonia produced and extracted from the digestate. Other supplements providing sugars and/or other nutrients may be stored in and provided from other reservoirs, such as reservoirs 1004b and 1004c. For example, molasses and/or vinasse may be supplied from reservoir 1004b. Co-digestion utilizing such co-substrates improves nutrient balance and digestion, equalization of solids by dilution, biogas production, and increases the potential for production of ammonia and ammonium compounds produced by natural means without chemical reactions, while producing higher yields of ammonia and ammonium compounds.

(8) The digester 1001 may have a large volume capacity in a range of about 10,000 gallons to about 500,000 gallons, for example, about 50,000 gallons to about 450,000 gallons, about 100,000 gallons to about 400,000 gallons, about 150,000 gallons to about 350,000 gallons, or any value therein. In other examples, the digester may have a smaller volume range for small output to supply relatively small operations or lab research operations. For example, the digester may have a capacity of about 250 gallons to about 10,000 gallons, or any value therein. The digester may be of various types, such as a fixed dome biogas digester, tube digester, or thin film digester.

(9) The environment in the digester 1001 may be conditioned to promote the metabolism and growth of anaerobic (e.g., methanogenic) bacteria. The production of large concentrations of ammonia in the biodigestion process can raise pH and inhibit other desirable digestion processes, such as contemporaneous methanogenesis. Thus, co-digestion with high protein substrates that result in reduced production of inhibitory chemicals (e.g., hydrogen sulfide) can improve ammonia production. Such co-digestion feedstocks include blood meal, blood, soy meal, soy derived proteins, meat meal (slaughter house waste), feather meal, fish and fish by-products, whey, milk, dairy by-products, alfalfa, corn, and sweet clover. Such proteinaceous co-substrates provide nutrients missing from biodigestion of low-protein materials and help to prevent inhibiting substances from affecting methanogenesis. Additional nutrient supplements that supply sodium, calcium, magnesium, and trace amounts of nickel, cobalt, molybdenum, and/or selenium can aid in counteracting the effects of increased ammonia production by the anaerobic digestion. In some embodiments, bacterial strains that are able to thrive and produce ammonia at higher pH levels may be selected for use in the biodigestor (e.g., Methanolobus strains such as Methanolobus bombayensis, Methanolobus taylorii, and Methanohalophilus zhilinaeae) to allow the pH of the digester to be higher without impairing ammonia production.

(10) In some embodiments, the temperature of the biodigestor 1001 may be maintained in a range of about 30° C. and about 60° C. (e.g., between about 40° C. and about 50° C.). The temperature of the digestor may be maintained by a combination of the heat generated by the anaerobic metabolism of the anaerobic bacteria in the digestor 1001 and one or more heating mechanisms 1007 (e.g., a heat exchanger) through which the digestate may be passed and heated and then returned to the digestor 1001 to maintain a target temperature in the digestor 1001. The system may include a boiler 1008 that provides steam for a heat exchanger 1007. In some examples, the boiler 1008 may be fueled by methane gas that is generated in the digestor 1001 and then extracted by a methane/CO.sub.2 separation system 1010.

(11) The pH of the biodigestor 1001 may be maintained in a pH range of about 6.5 to about 9 (e.g., in a range of about 6.8 to about 7.5, about 7 to about 9.5 or any value therein). In some examples, the pH of the digestor 1001 may be maintained at the pre-determined range by the combination of the degassing and removal of CO.sub.2 from the digestate liquid and the addition of a basic agent into digestor as needed. For example, the digestor 1001 may include one or more pH meters that are in communication with an electronic controller (not shown) that is operable to control a valve and pump for releasing a basic agent of predetermined concentration and known basicity from a storage container 1051 housing the basic agent. The basic agent may be NaOH, Ca(OH).sub.2, KOH, or other basic agent.

(12) The ammonia-rich liquid effluent generated in the digestor 1001 may subsequently be used in the ammonia extraction process performed in a series of desorption and absorption stages in which the physical conditions of the effluent (e.g., temperature and pH) are varied to facilitate removal and reabsorption of ammonia in aqueous solution. Digestate liquid in the digestor may decarbonized (dissolved carbon dioxide and carbonic acid may be removed), removing a significant amount of CO.sub.2. The removal of carbon dioxide from the digestate fluid raises the pH of the digestate which drives the equilibrium of ammonium carbonate towards dissociation. Methane may also be produced in the digestor by the anaerobic bacteria. The methane and CO.sub.2 gas that evolves in the digestor 1001 and may be collected via ducting and transferred to the methane/CO.sub.2 separation system 1010. The separated methane may be utilized as a fuel for the boiler 1008 for providing heated water or other fluid to the heat exchanger 1007 and/or in other heating elements in the system 1000 for heating fluids at various stages of the ammonia recovery process. The methane may additionally or alternatively used as a fuel for an electric generator 1011. The recovered CO.sub.2 may be vented out of the system 1000 and/or routed to mix with a recovered ammonia vapor in one or more of the desorption and absorption stages.

(13) The decarbonized digestate fluid from the digestor 1001 may be collected and passed through a heating mechanism, such as the heat exchanger 1007, to further heat the digestate fluid and drive additional carbon dioxide out of solution. The temperature of the digestate fluid may be raised to a temperature of about 50° C. to about 100° C., and preferably greater than 60° C. The heated digestate fluid may subsequently passed from the heat exchanger 1007 to a sequence of mixing chambers in which the digestate fluid may manipulated to extract an ammonia solution.

(14) FIG. 2 provides a view of an exemplary sequence of mixing units 1020, 1030, and 1040 through which substrates of the system may be transferred sequentially. Each of the mixing chambers may include an air nozzle or Venturi injector tube utilized to mix the fluid passed from one chamber to another with air or another gas. The temperature and pH conditions of each mixing chamber may be different in order to perform different absorption and desorption steps, which include decarbonization of the digestate (e.g., in mixing unit 1020), desorption of ammonia from the decarbonized digestate (e.g., in mixing unit 1030), and ammonia reabsorption in an aqueous solution (e.g., in mixing unit 1040).

(15) The first mixing unit 1020 may include a nozzle or a Venturi-style injector tube 1021, and a collection chamber 1022. The digestate is mixed with air by the Venturi tube 1021 as the digestate passes therethrough. The Venturi tube 1021 includes a conduit 1021a through which the digestate is passed to a low-pressure choke point where an injection duct 1021b is located. Air (e.g., ambient air, air drawn from a pressurized tank, etc.) is injected through the injection duct 1021b to mix with the heated digestate. The air is mixed thoroughly with the digestate in the turbulent flow of the Venturi tube 1021, which provides a high degree of surface area interface between the digestate fluid and the injected air. This results in an enhanced degassing of CO.sub.2 from the digestate. Once the digestate/air mixture passes into the mixing chamber 1022 in which the digestate/air mixture settles, and the CO.sub.2-rich air bubbles out of the digestate fluid. The digestate that pools in the mixing chamber 1022 may also be heated to a temperature in a range of about 85° C. to about 100° C. The resulting decarbonized digestate may have a pH of about 6.8 to about 9 (e.g., about 7.5 to about 8.5, or any value in such range). The CO.sub.2-rich air may be removed from the chamber for use in a later stage of the ammonia recovery process. The removal of the CO.sub.2-rich air may be aided by a pump, a partial vacuum, or may be allowed to flow naturally from the chamber. The decarbonization process of the present invention may remove up to about 90% of the CO.sub.2 from the effluent, thereby pushing the chemical equilibrium of ammonium bicarbonate and ammonia significantly toward free ammonia and increase the pH of the digestate fluid, thereby facilitating an extraction of a greater quantity of ammonia from the effluent.

(16) Carbon dioxide and digestate may be collected from the first mixing unit 1020 and transferred to further mixing chambers in a sequential absorption and desorption stages. The carbon dioxide and/or digestate may also be transferred to other structures and uses in the system 1000. The decarbonized digestate fluid from the first mixing unit 1022 may be transferred from the mixing chamber 1022 to the input conduit 1031a of the Venturi tube 1031, and the decarbonized digestate is passed to a low-pressure choke point where an injection duct 1031b is located. Air (e.g., ambient air, air drawn from a pressurized tank, etc.) is injected through the injection duct 1031b to mix with the heated decarbonized digestate. The air is mixed thoroughly with the digestate in the turbulent flow of the Venturi tube 1031, resulting in a large volume of air mixing into the decarbonized digestate which enhances volatilization of NH.sub.3 from the decarbonized digestate. The increased pH of the decarbonized digestate fluid pushes ammonium equilibrium toward dissociation of ammonium into aqueous ammonia and hydrogen ions, making more ammonia available in the digestate fluid and facilitating volatilization of ammonia from the digestate fluid. The decarbonized digestate at a high temperature and an increased pH allows a large majority of the ammonium in the digestate fluid being dissociated into ammonia and hydrogen ions, allowing a proportion of the ammonia in solution that is in the uncharged (non-ionized) ammonia state of about 0.6 or greater. The solubility of NH.sub.3 in an aqueous solution is low, and thus most of the NH.sub.3 volatilizes from the digestate fluid, and can be collected.

(17) In some examples, the decarbonized digestate fluid may be routed to a heat exchanger or other heating apparatus 1027 to further raise the temperature of the decarbonized digestate fluid to a temperature in a range of about 70° C. to about 90° C. (e.g., about 75° C. to about 80° C., or any value or range of values therein) prior to passing through the Venturi tube 1031. The proportion of ammonia that is in the NH.sub.3 form in a aqueous solution (1) at a temperature in a range of 70° C. to about 80° C. and (2) a pH of about 8 to about 10 (e.g., in a range of about 8.5 to about 9.5) is in a range of about 0.6 to about 0.95. In some embodiments, the air drawn into the mixing chamber 1032 may be warmed using a heat exchanger, heating coil or other heating mechanism to raise the temperature of the incoming air to a temperature in a range, e.g., of 70° C. to about 90° C. to aid in raising the temperature of the decarbonized digestate. An ammonia-rich air mixture is collected from the chamber through a collection conduit 1033 to transfer the NH.sub.3 rich mixture to a later stage of the ammonia recovery process. The removal of the ammonia-rich vapor may be aided by a pump, applied partial vacuum, or may be allowed to flow naturally from the chamber.

(18) In some embodiments, one or more basic chemical agents may be used to raise the pH of the digestate fluid pooled in the second mixing chamber 1032. In some examples, the basic agent may be NaOH, Ca(OH).sub.2, KOH, or other basic agent, which may be added in sufficient amounts to raise the pH of the pooled digestate to a pH in the range of about 9 to about 11 (e.g., about pH 9.5 to about pH 10.5) to further shift the ammonia equilibrium toward de-ionized ammonia. The basic agent may be supplied from the storage container 1051 housing the basic agent.

(19) In some embodiments, some or all of the digestate fluid remaining in the second mixing chamber 1032 may be removed from the chamber and routed either back to the digester 1001 or delivered into a filtering apparatus 1052 (e.g., a filter press) for purification. The filtering apparatus may be any of various known filtering apparatus. Once the recovered fluid is filtered, yielding a water filtrate, the water may be conditioned to a target temperature and routed to one or more subsequent uses. The recovered digestate fluid may be conditioned in a heating system (e.g., a heat exchanger electrical heating system, etc.) to a temperature in a range of about 35° C. to about 45° C. and routed in a tank 1053 for storage. The fluid may be added back to the digester to be mixed with the biodigestion medium as needed. After filtering, the fluid may also or alternatively be conditioned to a temperature of about 70° C. to about 90° C. (e.g., about 75° C. to about 80° C., or any value or range of values therein) using a heat exchanger or other heating mechanism and may be added back to the fluid of the second mixing chamber 1032 as needed. The filtered fluid may also be conditioned with a pH agent (e.g., sodium hydroxide or hydrated lime, etc.) to raise the pH before it is added back to the second tank. Keeping the digestate pooled in the second mixing tank 1032 allows for a building NH.sub.3 concentration in the fluid in the second mixing tank 1032 to increase the amount of NH.sub.3 that volatilized from the fluid in the second mixing tank 1032.

(20) The significant amounts of NH.sub.3 that volatilize from the digestate fluid in the second mixing chamber 1032 and may be collected via an outlet 1034 that leads to a third air nozzle or Venturi injector 1041 and third mixing chamber 1042. The NH.sub.3-rich air collected from the second mixing chamber 1032 may be passed through the injector duct 1041b of the third Venturi injector 1041 and mixed at the throat of the Venturi tube with the cooled aqueous NH.sub.3 solution (less than about 20° C.), which has a pH of less than about 8.5 that is passed through the input passage 1041a of the Venturi mixer 1041. Thus, the relatively warm NH.sub.3 vapor from the second mixing chamber 1032 is mixed with a cooled NH.sub.3 solution to reduce the temperature to allow the gaseous NH.sub.3 vapor to be reabsorbed into the cooled NH.sub.3 solution. The lower pH of the cooled NH.sub.3 solution also allows for reabsorption of the NH.sub.3 vapor. In some embodiments, CO.sub.2 gas captured evolved and collected from the digestate fluid in the first mixing chamber 1022 may be routed from outlet 1024 to the injector duct 1041b of the third mixing unit 1040 and mixed with the NH.sub.3-rich air collected from the second mixing chamber 1032. The added CO.sub.2 gas may be used as the means by which the pH of the third mixing chamber 1042 is reduced in order to increase the amount of dissolved NH.sub.4.sup.+ in the fluid collected in the third mixing chamber 1042. In some embodiments, the CO.sub.2 gas may be cooled in a heat exchanger or other mechanism prior to it being delivered to the injector duct 1041b of the third Venturi mixer 1041. In other embodiments, the cooled fluid may be a pH treated solution comprising a weak acid and/or buffering agents to maintain the pH below about 8.5. A substantial amount of the NH.sub.3 in the air mixture is able to be dissolved into the cooled, lower pH aqueous solution in the third mixing chamber 1032 because ammonia solubility in aqueous solutions increases as temperature and pH drop. The proportion of ammonia that is in the NH.sub.4.sup.+ form in an aqueous solution (1) at a temperature in a range of 20° C. or less and (2) a pH of less than about 8.5 to greater or equal to about 0.8. Thus, the solubility of NH.sub.3 in aqueous solution is also high, and thus a significant proportion of the NH.sub.3 in the NH.sub.3-rich air dissolves into the ammonia solution.

(21) In some embodiments, the cooled fluid passed through the Venturi mixer may be fluid taken from the third mixing chamber 1042 and either routed to the intake 1041a of the Venturi mixer 1041 or routed to a cooling tank 1053 (e.g., including a heat exchanger, refrigeration unit, or other cooling mechanism) to lower the temperature to a temperature in a range of about 10° C. to about 20° C. before being passed to the intake 1041a to mix with the NH.sub.3-rich air from the second mixing chamber 1032. The fluid from the third mixing chamber 1042 may be delivered to the intake 1041a at a pre-determined rate.

(22) The ammonia-rich aqueous solution collected in the third mixing chamber 1042 may be transported through outlet 1043 incrementally to a collection tank 1054 for the clean aqueous ammonia product. The ammonia-rich aqueous solution may be used in a number of applications including making organic nitrogen fertilizers. Because the ammonia is organically derived from biowastes and natural sources, the concentration of the stable .sup.15N isotope in the resulting ammonia composition is much higher than in ammonia products that are made from chemical syntheses and concentration techniques. The .sup.15N isotope is present in the environment and in ammonia products produced by chemical reactions in an amount of about 0.3% per mole of naturally occurring nitrogen. The amount of .sup.15N isotope in the ammonia and related species produced by the process of the present invention is in the range of about 1% to about 20% per mole of nitrogen (e.g., in a range of about 5% to about 15%). The high concentration of .sup.15N isotope reflects the process of concentrating ammonia from natural biowastes and nutrient stocks through organic processes.

(23) The ammonia produced by this process is an organic ammonium hydroxide solution that is usable in organic farming. The ammonia is produced at a concentration in a range of about 3-30% w/w ammonia solution (e.g., about 10% to about 25% w/w ammonia). The organic ammonia solution may be used to create fertilizer compositions that are compliant with the Organic Foods Production Act of 1990, USDA Organic Regulations, (generally referred to as the National Organic Program or NOP) and other agency standards for use in organic farming and can be used in organic farming operations.

(24) In some embodiments, and without limitation, a fertilizer composition may include a liquid composition that includes about 3% to about 30% ammonia w/w (e.g., 10% w/w to about 25% w/w, or any value or range of values therein), and/or one or more additional ingredients. The fertilizers may further include organic acids that may serve to balance the pH effects of the concentrated ammonia in the fertilizer. The pH may be maintained in a range around neutral pH, such as between about pH 6 and pH 8 (e.g., from about pH 6.5 to about pH 7.5). To balance the pH of the liquid fertilizer, the liquid fertilizer may include one or more organic acids.

(25) The resulting high concentration ammonia composition may be further processed into fertilizer products. In some embodiments, the fluid product captured from the third mixing chamber may be utilized as a fertilizer composition. Such fertilizer composition may be an aqueous solution comprising ammonia and ammonium species (e.g., NH.sub.4.sup.+, ammonium hydroxide, and ammonium carbonate) in a concentration of about 3% to about 30% w/w (e.g., 10% w/w to about 25% w/w, or any value or range of values therein), and carbonic acid in various soluble forms in an amount of about 5% to about 15% w/w. In some embodiments, the ammonia-rich aqueous solution may be mixed with other plant and soil nutrient compounds that are compatible with organic farming to create a nitrogen-rich organic fertilizer composition.

(26) The high concentration ammonia composition may be mixed with alternative acids, including organic acids. In some embodiments, the fertilizer composition may be an aqueous solution comprising ammonia and ammonium species (e.g., NH.sub.4.sup.+, ammonium hydroxide, and ammonium carbonate) in a concentration of about 3% to about 30% w/w (e.g., 10% w/w to about 25% w/w, or any value or range of values therein), and citric acid in various soluble forms in an amount of about 5% to about 15% w/w, to yield a combination of these species with ammonium citrate (see FIG. 1). A reservoir of citric acid may be included in the system 1000, and at least a portion of the high concentration ammonia composition produced by the system may be mixed with the citric acid from the citric acid reservoir to produce a separately collected and stored product comprising organic ammonia, ammonium species (including ammonium citrate), and citric acid.

(27) In other embodiments, the organic fertilizers may include ammonia in various ionic forms in a concentration of about 3% to about 30% w/w (e.g., 10% w/w to about 25% w/w, or any value or range of values therein) and one or more weak organic acids or salts thereof (e.g., polyprotic organic acids or salts thereof), such as citric acid, malic acid, fumaric acid, salts of such organic acids, and combinations thereof. Other simpler organic acids, such as acetic acid salts of such organic acids may be used as well. The organic acids must be from organically-compliant sources (e.g., NOP compliant). Citric acid may be preferred due to its tri-protic chemistry and superior buffering capabilities. The organic acid(s) may be present in a concentration in the liquid fertilizer in a range of about 5% to about 50% w/w, depending on the concentration of ammonia in the liquid fertilizer. For example, the concentration of citric acid in the liquid fertilizer by weight may be about twice the amount of ammonia present in the solution by weight. Simpler monoprotic acids may be present in higher concentrations, due to their lower buffering capacity.

(28) The organic fertilizers of the present invention may also include humic acids which help with nitrogen fixation in the organic fertilizers. Liquid ammonia fertilizers suffer from nitrogen loss through evaporation or other pathways of loss. Planting soils are typically acidic to optimize conditions for the growth of plants, which exhibit optimal germination and growth in a pH range of about pH 5.0 to about pH 7.0. The acidic pH of the soil can increase ammonia volatilization. This particularly significant where the fertilizer composition has a relatively high nitrogen concentration (e.g., greater than 10% w/w), since the higher concentration results in a higher rate of volatilization. Humic acids are able to retain NH.sub.4 as well as aid in NH.sub.3 ammonia volatilization reduction. Humic acids have high cation exchange capacity (CEC) that allows it to retain soil cations and can significantly reduce NH.sub.3 volatilization upon addition to an acidic soil (e.g., through the addition of peat). The addition of humic acids to the organic NH.sub.3 fertilizer of the present invention significantly reduces NH.sub.3 volatilization and lead to effective accumulation of NH.sub.4 in the planting soil, despite having an acidic pH (e.g., about pH 5.5 to about 7.0). The humic acids may provide the additional benefit of providing short carbon-chain molecules.

(29) Humic acids may be included in the organic fertilizer composition of the present invention in a concentration in a range of about 3% w/w to about 8% w/w. The amount of humic acids included in the organic fertilizer may vary with the concentration of ammonia provided therein. For example, in compositions comprising about 10% to about 15% NH.sub.3 w/w, the fertilizer composition may include about 3% to about 4% w/w of humic acids. In compositions comprising about 15% to about 25% organic NH.sub.3 w/w, the fertilizer composition may include about 5% to about 8% w/w of humic acids.

(30) The organic fertilizer composition of the present invention may also include additional components routinely used in the art, for example, humectants, adjuvants, antioxidants, stabilizers, plant macronutrients, plant micronutrients, and combinations thereof.

(31) The organic fertilizer composition of the present invention may also include a solid fertilizer composition comprising about 3% to about 30% ammonia w/w (e.g., 10% w/w to about 25% w/w, or any value or range of values therein), and/or one or more additional ingredients. The fertilizers may further include organic acids that may serve to balance the pH effects of the concentrated ammonia in the fertilizer. The pH may be maintained in a range around neutral pH, such as between about pH 6 and pH 8 (e.g., from about pH 6.5 to about pH 7.5). The solid fertilizer composition may additionally include humectants, adjuvants, antioxidants, stabilizers, plant macronutrients, plant micronutrients, and combinations thereof. The fertilizer composition may include further nutrients, such as gypsum as a calcium sulfate source, and dolomitic lime as a calcium carbonate and magnesium carbonate source.

CONCLUSION/SUMMARY

(32) The present invention provides organic ammonia fertilizer compositions and methods of making the same. It is to be understood that variations, modifications, and permutations of embodiments of the present invention, and uses thereof, may be made without departing from the scope of the invention. It is also to be understood that the present invention is not limited by the specific embodiments, descriptions, or illustrations or combinations of either components or steps disclosed herein. The embodiments were chosen and described in order to best explain the principles of the invention and its practical application, to thereby enable others skilled in the art to best utilize the invention and various embodiments with various modifications as are suited to the particular use contemplated. Although reference has been made to the accompanying figures, it is to be appreciated that these figures are exemplary and are not meant to limit the scope of the invention. It is intended that the scope of the invention be defined by the claims appended hereto and their equivalents.