WO2020131116A1 - Procédé de récupération de bicarbonate d'ammonium à partir d'eaux usées - Google Patents

Procédé de récupération de bicarbonate d'ammonium à partir d'eaux usées Download PDF

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Publication number
WO2020131116A1
WO2020131116A1 PCT/US2018/067247 US2018067247W WO2020131116A1 WO 2020131116 A1 WO2020131116 A1 WO 2020131116A1 US 2018067247 W US2018067247 W US 2018067247W WO 2020131116 A1 WO2020131116 A1 WO 2020131116A1
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Prior art keywords
ammonia
gas
carbon dioxide
ammonium bicarbonate
temperature
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PCT/US2018/067247
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English (en)
Inventor
Dominic Bassani
Morton ORENTLICHER
Mark Simon
Stephen Pagano
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Bion Environmental Technologies, Inc.
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Publication date
Application filed by Bion Environmental Technologies, Inc. filed Critical Bion Environmental Technologies, Inc.
Priority to CA3123802A priority Critical patent/CA3123802A1/fr
Priority to PCT/US2018/067247 priority patent/WO2020131116A1/fr
Priority to EP18943551.4A priority patent/EP3898515A4/fr
Priority to MX2021007358A priority patent/MX2021007358A/es
Publication of WO2020131116A1 publication Critical patent/WO2020131116A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05C—NITROGENOUS FERTILISERS
    • C05C3/00—Fertilisers containing other salts of ammonia or ammonia itself, e.g. gas liquor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
    • B01D5/0066—Dome shaped condensation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/26—Carbonates or bicarbonates of ammonium
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
    • C05F17/00—Preparation of fertilisers characterised by biological or biochemical treatment steps, e.g. composting or fermentation
    • C05F17/10—Addition or removal of substances other than water or air to or from the material during the treatment
    • C05F17/15—Addition or removal of substances other than water or air to or from the material during the treatment the material being gas
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
    • C05F17/00—Preparation of fertilisers characterised by biological or biochemical treatment steps, e.g. composting or fermentation
    • C05F17/50—Treatments combining two or more different biological or biochemical treatments, e.g. anaerobic and aerobic treatment or vermicomposting and aerobic treatment
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
    • C05F3/00—Fertilisers from human or animal excrements, e.g. manure
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/048—Purification of waste water by evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/02—Biological treatment
    • C02F11/04—Anaerobic treatment; Production of methane by such processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F2001/5218—Crystallization
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/20—Nature of the water, waste water, sewage or sludge to be treated from animal husbandry
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
    • Y02A40/10—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in agriculture
    • Y02A40/20—Fertilizers of biological origin, e.g. guano or fertilizers made from animal corpses
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/40—Bio-organic fraction processing; Production of fertilisers from the organic fraction of waste or refuse

Definitions

  • the present invention relates generally to a process, a method, and a system for the recovery and concentration of dissolved ammonium bicarbonate from a wastewater containing ammonia (NH3) using gas separation, condensation, and fdtration, each at controlled operating temperatures.
  • the present Invention also relates generally to a process, a method, and a system for the recovery and concentration of dissolved ammonium bicarbonate from a wastewater containing ammonia (NH3) using gas separation, condensation, and crystallization, each at controlled operating temperatures.
  • Wastewaters may contain dissolved ammonia as ammonium ion and as dissolved ammonia gas; as well as dissolved carbon dioxide as bicarbonate and carbonate ions and as dissolved carbon dioxide gas.
  • the word“ammonia” will be used generally to refer to any dissolved form of ammonia.
  • the present invention also relates to a process, a method, and a system for the production of a nitrogen rich fertilizer from an ammonia (NH3) containing wastewater using a process, method and/or system comprising the concentration of dissolved ammonium bicarbonate using gas separation and condensation, followed by crystallization of concentrated ammonium bicarbonate, all at controlled operating temperatures. More specifically, the present invention relates to a process, method, and system to produce, from a wastewater containing ammonia (NH3), an organic solid containing high concentrations of nitrogen which could be utilized as a component ingredient in a nitrogen rich, organic fertilizer product.
  • the process, method and system of the present invention is a useful improvement over existing technologies for the removal of ammonia from wastewaters because the present invention: converts NH3-N into ammonia gas but does not utilize any chemicals to increase pH, captures the ammonia gas in the form of a stable salt but does not utilize industrial acids to react with the ammonia, and produces a solid-fertilizer product with minimal use of energy.
  • the present invention allows for the production/synthesis of organic N-fertilizer, ammonium bicarbonate (AB) derived from wastewaters, sludges and solids containing ammonia (NH3) or ammonia and carbon dioxide (C02), without the use of chemical additives.
  • AB ammonium bicarbonate
  • NH3 ammonia
  • C02 ammonia and carbon dioxide
  • Anaerobic digestion is a common unit operation employed in the treatment of wastewaters containing organics and nitrogenous compounds including industrial, municipal and agricultural wastewaters.
  • the resulting solid/liquid slurry from an anaerobic digester has a high- solids portion and a low-solids portion.
  • the digestate produced from dairy wastewater contains a high-solids portion comprising largely cellulosic solids and a low-solids portion containing concentrations of dissolved carbon dioxide and dissolved ammonia nitrogen as well as salts and both suspended and dissolved organics.
  • the dissolved ammonia nitrogen in the digestate presents significant environmental issues if left untreated, such as, when the digestate is land applied, discharged to a body of water, or sent to a holding pond or lagoon.
  • Potential adverse air and water impacts include: ammonia (toxic to fish, irritating to human eyes and lungs) will be lost both to the air and water; ammonia will be biologically oxidized either in water or soil and chemically oxidized in the air, in either case forming gases that are irritants and can form ozone or greenhouse gases, etc.
  • Most often regulations for ammonia release are designed to prevent excess nutrient input to surface waters which may cause eutrophication.
  • One well-established technology for treatment of digestate is air stripping which uses hot air and/or steam to strip ammonia from the wastewater creating a liquid stream comprising substantially less dissolved ammonia and a heated gas containing the stripped ammonia.
  • Formation of a solid precipitate containing ammonia, ammonium bicarbonate, and ammonium carbonate, during the air stripping process may foul the air stripping substrates causing operational and maintenance issues and thus is not desired.
  • An increase of the pH of the wastewater shifts the equilibrium for ammonia away from dissolved ionized ammonium and more to ammonia gas. Accordingly, increased removal of the ammonia from digestate using air stripping is commonly achieved with chemical addition. Examples of chemicals used to increase pH include calcium, sodium or magnesium hydroxide.
  • the stripped ammonia is absorbed into an acid solution. The use of acids is highly effective for ammonia recovery and could also be effective in producing a concentrated ammonium salt product using subsequent unit operations.
  • treatment utilizing industrial chemicals to raise pH with a stripping process and for absorption of ammonia such as, for example, for a treatment system for a dairy waste which produces a nutrient rich solid for use as a fertilizer, has the unavoidable consequence stemming from the use of such chemicals that any reusable end product cannot be certified as an “organic” product.
  • Stripper exhaust gas containing ammonia is sometimes released to the atmosphere although regulations typically require that it is further processed to capture the nitrogen.
  • U.S. Patent No. 7,811,455 (Burke) describes a process for use of biogas rather than air and reclaiming ammonia from stripper exhaust gases in the form of ammonium bicarbonate by blending the C02 in the digester biogas with the stripper gas and then precipitating and recovering ammonium bicarbonate with the added benefit of lowering C02 in the biogas.
  • One of the main drawbacks with that process is that the use of chemicals to raise the pH in the stripper precludes certification of the ammonium bicarbonate solids and any solids created from the ammonium bicarbonate solids as“organic” fertilizer.
  • Another drawback is the inefficiency associated with processing large volumes of gas, including precipitation of ammonium bicarbonate in the gas phase.
  • High-ammonia and ammonium containing wastewaters are produced in many industrial and municipal processes. Agriculture is one of the largest sources of these wastewaters, in particular in the form of products from the anaerobic digestion of organic waste. Examples of sources of this waste are animal manure, meat processing, dairy processing, and silage.
  • Ammonia (NH3) that is not captured in a stable chemical form is a potential source of air and water pollution.
  • the present invention provides a way to remove a substantial portion of the ammonia nitrogen within a liquid wastewater and capture the nitrogen in the form of crystallized ammonium bicarbonate using a series of unit operations operated under specified temperatures and without the use of chemicals to raise pH.
  • the resulting ammonium bicarbonate solid is high in nitrogen content and could be used in combination with other materials to create a nitrogen rich organic fertilizer product.
  • the present invention includes at least three components: 1) removal of the ammonia from the waste (including without limitation sludges, semi solids, and solids and liquids) without the use of chemicals at a temperature of at least 80 degrees Celsius thereby converting the ammonia to gaseous form;
  • bicarbonate at a temperature below 35 degrees Celsius such that the reverse osmosis concentrate becomes saturated with dissolved ammonium bicarbonate and ammonium carbonate which depends upon the concentrations of ammonium carbonate and ammonium bicarbonate to form solid ammonium bicarbonate and ammonium carbonate.
  • the present invention includes at least three components:
  • the present invention is not limited to any one specific method or process to remove ammonia nitrogen from the waste but rather includes numerous alternatives provided the operating temperatures for the components are followed. Stripping animal manure digestate at a temperature of at least 60 degrees Celsius and preferably at a temperature of at least 80 degrees Celsius, for example, is one way to remove ammonia nitrogen from animal waste creating an exhaust gas containing ammonia gas. Examples of other ways to remove ammonia nitrogen from wastewaters and create an ammonia-containing gas include dryers, and filtration devices with membrane modules and heat sources.
  • the present invention includes two paths for the creation of a concentrated solution of ammonium carbonate and ammonium bicarbonate, the first using condensation to convert gaseous ammonia, C02 and water vapor to a liquid solution containing ammonium carbonate and ammonium bicarbonate followed by filtration, the second using staged condensation to remove a significant amount of water vapor from the gas by partial condensation causing formation of a concentrated gas, followed by the formation of a concentrated dissolved ammonium bicarbonate liquid solution using absorption of ammonia from said gas.
  • the present invention then uses crystallization to form solid ammonium bicarbonate and ammonium carbonate.
  • the present invention includes condensing the gaseous ammonia with carbon dioxide and water vapor at a temperature of between about 35 and 50 degrees Celsius causing the formation of dissolved ammonium carbonate and ammonium bicarbonate in a liquid condensate.
  • the amount of carbon dioxide within the ammonia-containing gas may be enough to convert substantially all of the ammonia into ammonium carbonate and ammonium bicarbonate without addition of carbon dioxide.
  • Digested dairy manure put through a stripping process operated at greater than 80 degrees Celsius should create an exhaust gas containing enough carbon dioxide for the conversion of substantially all of the gaseous ammonia to dissolved ammonium carbonate and ammonium bicarbonate.
  • the net result of the process is to recover ammonium bicarbonate and ammonium carbonate from the mixture of materials constituting the digestate as a high purity solution of ammonium
  • bicarbonate and ammonium carbonate in the condensate permits organic certification of the eventually created nitrogen rich solids. If additional carbon dioxide is required, the organic certification can still be used if the carbon dioxide is from non-synthetic sources. While organic fertilizers have a significant financial advantage over non-organic fertilizers, the present invention is not limited solely to a process, method, or system resulting in organic products. The present invention also includes addition of carbon dioxide from outside sources resulting in products unable to be certified as organic.
  • the dissolved ammonium carbonate and ammonium bicarbonate in the resulting condensate liquid is then concentrated.
  • a two-stage reverse osmosis unit operating between about 20 and 50 degrees Celsius for example concentrates dissolved ammonium carbonate and ammonium bicarbonate to about 10 times the ammonium concentration of the condensate, but the increase could be anywhere from 1.5 to 20 times the concentration of the ammonium concentration in the condensate. More preferably, a two-stage reverse osmosis unit operating between about 35 and 50 degrees Celsius, concentrates dissolved ammonium carbonate and ammonium bicarbonate more efficiently.
  • the present invention includes condensing the gaseous ammonia is a staged manner at a temperature of at least 80 degrees Celsius in the first stage to remove a significant amount of water vapor in liquid condensate form causing formation of a concentrated ammonia and carbon dioxide gas. Removing the water vapor and
  • the concentrated ammonia and carbon dioxide gas is then treated using absorption (an absorption column, for example) operating at a temperature of between about 20 and 50 degrees Celsius to form a concentrated dissolved ammonium bicarbonate liquid solution.
  • absorption an absorption column, for example
  • the liquid containing concentrated dissolved ammonium carbonate and ammonium bicarbonate is then cooled to less than about 35 degrees Celsius to saturate the reverse osmosis or absorption concentrate and form solid ammonium bicarbonate and ammonium carbonate which is stable and high in nitrogen content. Moreover, resulting solids are substantially free of phosphorous.
  • the solid ammonium bicarbonate can be stored and/or combined with other materials to create nitrogen rich fertilizer.
  • ammonium bicarbonate Although the detailed chemistry for the formation of ammonium bicarbonate from ammonia and carbon dioxide is complex, the reactions provide predictable behaviors at temperatures and pressures accessible under normal industrial and agricultural conditions. At biological pH about 8, ammonium bicarbonate is stable in solutions below about 50 degrees Celsius and rapidly decomposes in solutions above about 80 degrees Celsius, as displayed in Table 2 below.
  • the present invention utilizes the varying stability and solubility of ammonium bicarbonate at different temperatures and pressures a) to drive substantially all of the dissolved ammonium out of the wastewater and into gaseous form (which occurs at a temperature of about 80 degrees Celsius (Table 2) and is complete at a temperature of about 90 degrees Celsius (Table 1)), b) so that it can be condensed with carbon dioxide and water vapor and concentrated at a lower temperature (at a temperature of between about 35 and 50 degrees Celsius) where ammonium bicarbonate is stable, thereby converting the ammonia to dissolved ammonium bicarbonate in a concentrated liquid form, and c) so that the concentrated dissolved ammonium bicarbonate can be solidified at a lower temperate (less than about 20 degrees Celsius).
  • FIG. l is a schematic drawing of one embodiment of the invention for the treatment of cattle manure (e.g., from a CAFO) comprising solids separation, anaerobic digestion, stripping, condensation, concentration using reverse osmosis, and crystallization.
  • cattle manure e.g., from a CAFO
  • FIG. 2 is a schematic drawing of another embodiment of the invention for the treatment of dairy manure (e.g., from a CAFO) comprising solids separation, anaerobic digestion, ultra filtration with heating and membrane filtration, condensation, concentration using reverse osmosis, crystallization, and storage.
  • dairy manure e.g., from a CAFO
  • FIG 3 is a schematic drawing of another embodiment of the invention for the treatment of an ammonia-containing wastewater (e.g., from layer manure) comprising heat drying, condensation of ammonia water, dissolution of carbon dioxide into the ammonia water using membrane filters, concentration of ammonium bicarbonate, crystallization, and storage.
  • an ammonia-containing wastewater e.g., from layer manure
  • FIG 4 is a schematic drawing of another embodiment of the invention for the treatment of cattle manure (e.g., from a CAFO) comprising solids separation, anaerobic digestion, stripping, absorption, concentration using reverse osmosis, and crystallization.
  • cattle manure e.g., from a CAFO
  • FIG. 5 is a schematic drawing of another embodiment of the invention for the treatment of livestock manure (e.g., from a CAFO) comprising solids separation, anaerobic digestion, stripping, condensation, absorption, and crystallization.
  • livestock manure e.g., from a CAFO
  • FIG. 1 is a process flow schematic drawing of one embodiment of the invention for the treatment of cattle manure (e.g., from a CAFO) comprising solids separation, anaerobic digestion, stripping, condensation, concentration, and crystallization.
  • cattle manure e.g., from a CAFO
  • the present invention excludes the use of pH adjustment chemicals.
  • raw manure 10 with or without associated dairy waste generated at the CAFO is transported to a solids separation unit/process 20 (it being understood that a mixing or holding tank/vessel could be used prior to solids separation and/or can be used for solids separation).
  • the solids separation unit/process may be a single stage or chamber unit or it could be a series of stages or chambers for coarse solids separation and intermediate solids separation.
  • the slurry/effluent 24 from the solids separation unit 20 is input into an anaerobic digester 30 which digests much, preferably most, of the dissolved organics and small organic particulates to produce biogas 32 and an effluent digestate 34
  • the effluent digestate 34 from the anaerobic digester 30 contains residual solids, dissolved salts and organics, and concentrations of dissolved ammonia and carbon dioxide.
  • the present invention collects the ammonia and carbon dioxide and captures them in a subsequent multistage process to re-form solid ammonium bicarbonate. Each stage of the subsequent multistage process operates at different temperatures to take advantage of the solubility properties of ammonium bicarbonate for its concentration in dissolved form and then its formation as a nitrogen rich solid.
  • the temperature of digestate 34 out of a typical anaerobic digester treating cattle manure is about 35 degrees Celsius.
  • the digestate needs to be heated to greater than about 80 degrees Celsius for treatment in the stripper 40
  • the stripper operating at a temperature of greater than about 80 degrees Celsius, without any chemical addition to increase pH, removes dissolved ammonia and dissolved carbon dioxide from the digestate 34 creating exhaust vapor 42 containing water vapor, gaseous carbon dioxide, and gaseous ammonia. Vapor 42 will also contain traces of organic volatiles and semi-volatiles.
  • footnote 1 denotes the vapor is constant composition for continuous operation and varies during a batch process - H20, C02, and NH3 evolve with traces of organic volatiles and semi volatiles.
  • the treated water and solids 44 out of the stripper can be further treated for application to land or water using current treatment technologies.
  • the temperature of the stripper 40 can be maintained using a heat exchanger 46
  • the vapor 42 created by stripping the digestate 34 in that first stage, the separation stage, is then treated in a second condensation and concentration stage to create a concentrated dissolved ammonium bicarbonate solution.
  • Condenser 50 and reverse osmosis filter 60 are then used to treat vapor 42 at a temperature of between about 35 degrees Celsius and 50 degrees Celsius.
  • a pressure control valve 48 can be used between the stripper 40 and the condenser 50 to maintain a differential between the two.
  • footnote 2 denotes pressure control valve is set to maintain differential between distillation unit and condenser - Condenser temperature, T, must be less than 50 degrees Celsius to keep NH4 and HC03 in solution, while distillation temperature must be greater than 80 degrees Celsius to convert to NH3 and C02.
  • Operating the condenser 50 between about 35 and 50 degrees Celsius allows the water vapor, ammonia, and carbon dioxide to form dissolved ammonium bicarbonate.
  • the effluent ammonium bicarbonate solution 54 is treated in a reverse osmosis filter 60.
  • Reverse osmosis filter 60 removes water thereby concentrating the ammonium bicarbonate in the solution.
  • the resulting concentrated effluent 64 out of the reverse osmosis filter 60 contains about 50-100 times the concentration of dissolved ammonium bicarbonate in the digestate 34.
  • footnote 5 denotes AB concentrate is supersaturated relative to temperature of crystallizer. Control of the reverse osmosis temperature avoids precipitation of the ammonium bicarbonate on the membrane while achieving a concentration sufficient for saturation at the temperature in the crystallizer.
  • the permeate 62 is a clean water than can be reused or discharged.
  • the concentrated effluent 64 out of the reverse osmosis filter 60 is then treated at a temperature of less than about 35 degrees Celsius in stage three using a crystallizer 70. It is understood that lower temperatures, e.g., 20 degrees Celsius, could be used in the crystallizer depending upon the concentrations of dissolved ammonium carbonate and ammonium
  • bicarbonate in the reverse osmosis concentrate Solid crystals of ammonium bicarbonate are grown in the crystallizer 70 under controlled conditions, separated from the liquid fraction to produce an ammonium-salt 74 which may be dried, pelletized or granulated to form a final product.
  • a portion of the saturated ammonium bicarbonate supernatant is recycled 72 to the reverse osmosis filter 60, after it is heated to the required temperature in a heat exchanger 56.
  • footnote 4 denotes heat exchange on recirculation liquid to minimize size of heat exchanger 56 to match temperature of reactor liquid.
  • the resulting ammonium salt may be dried and packaged for commercial distribution as a specialized nitrogen fertilizer, that is high-purity, phosphorus free, and certified USDA organic.
  • the resulting product is high-purity and phosphorous free due to the two purification operations, namely, 1) the distillation process which removes ammonia and separates it from salts that are left behind in the distillation unit’s liquid effluent, and 2) the crystallization process which removes solid ammonium bicarbonate from other contaminants including traces of phosphorous containing salts. If synthetic chemicals are not used in obtaining the solids or liquid digestate, the ammonium bicarbonate product will have the potential for designation as organic (USDA 2012) fertilizer.
  • the USDA designation is of economic importance as the price of organic fertilizer expressed as dollars per pound ammonia nitrogen, is materially higher than that of chemical (non-organic) fertilizers that are equally uniform, high purity, and concentrated sources of NH3-N. As with synthetic fertilizer, the material is nearly odorless, and has low transport and application costs relative to manure and digestate. If the ammonia is captured with an industrial acid or is derived from application of caustic or other industrial alkali - it will not qualify as organic fertilizer.
  • the ammonium salt according to the invention resolves this conflict by (1) producing ammonia gas thermally with no chemical addition, and (2) using the carbon dioxide found in the digestate to recover the ammonia from the digestate to form an organic fertilizer, ammonium bicarbonate.
  • the ammonium salt 74 can be stored 80 for use on or off site.
  • stage 1 of the foregoing described process can be modified to remove solids (effluent suspended solids of 0.1% or less) so that a membrane separation device could be employed to separate the gases water vapor, carbon dioxide, and ammonia from the digestate liquid.
  • raw manure 110 with or without associated dairy waste generated at the CAFO is transported to a solids separation unit/process 120 (it being understood that a mixing or holding tank/vessel could be used prior to solids separation or for the separation).
  • the solids separation unit/process 120 may be a single stage or chamber unit or it could be a series of stages or chambers.
  • the footnotes 1-4 denote the following:
  • ammonia nitrogen 1000 ppm
  • - NH3-N is 60% NH3 at 80 C, 34% NH3 at 60 C, and 4% NH3 at 20
  • the output/effluent from the solids separation unit 124 is input into an anaerobic digester 130 which digests much, preferably most, of the dissolved organics and small organic particulates to produce biogas 132 and an effluent digestate 134.
  • the temperature of digestate 134 is heated to greater than about 80 degrees Celsius for treatment in stage 1, as described in detail below.
  • the invention excludes the addition of chemicals to increase pH and also excludes the addition of carbon dioxide from a non-organic source (preferably, the carbon dioxide used in the process comes directly from the waste being treated).
  • a non-organic source preferably, the carbon dioxide used in the process comes directly from the waste being treated.
  • an input vapor similar to that created in the foregoing embodiment shown in Figure 1 containing water vapor, gaseous carbon dioxide, and gaseous ammonia is created using a different unit process than shown in Figure 1.
  • the separation of the gaseous ammonia and gaseous carbon dioxide from the digestate 134 is accomplished using a membrane device 143 instead of a stripper.
  • the membrane passes gases, such as water vapor, ammonia, and carbon dioxide, but not liquid water. It therefore performs the same gas-separation function as the separation device shown in stage 1 of Figure 1.
  • the digestate 134 is treated for solids removal prior to stage 1, the ultrafilter 136, and prior to gas separation in the membrane device 143.
  • An ultra filter 136 is shown in Figure 2 for the solids removal it being understood that other solids removal methods producing the equivalent result of fine solids removal, for example passing only solids of less than 0.5 micron, are included within the scope of the invention.
  • the concentrated solids 138 from the ultra filter 136 can be mixed with the solids from the initial solids separation step, or processed as a high phosphorus solid product.
  • the ultra filter 136 removes a substantial portion of the total suspended solids in the digestate.
  • the low suspended-solids (0.1% or less) digestate 137 is then treated in the gas-separation process of the invention which in this embodiment includes use of membrane device 143.
  • the temperature of the low-solids digestate 137 is raised to at least about 80 degrees Celsius using a heat exchanger 146.
  • Membrane device 143 includes a hydrophobic membrane that allows gas molecules to pass, such as water vapor, ammonia, and carbon dioxide, but not the liquid and its contaminants. The preceding uF is required to remove solids and organic material that might otherwise foul the hydrophobic membrane. Vapor 142 will also contain traces of organic volatiles and semi-volatiles.
  • the treated water and solids 149 out of the membrane device 143 can be further treated for application to land or water using current treatment technologies.
  • Condenser 150 and reverse osmosis filter 160 are used to condense vapor 142 and concentrate its condensate 154 at a temperature of between about 35 and 50 degrees Celsius, to hold stable ammonium bicarbonate in solution.
  • the effluent ammonium bicarbonate solution 154 out of the condenser 150 contains the dissolved ammonium bicarbonate from the ammonia and carbon dioxide of the digestate 134.
  • the non-condensed water and gases 152 exiting the condenser 150 can be discharged to the atmosphere.
  • the effluent ammonium bicarbonate solution 154 is treated in a reverse osmosis filter 160.
  • Reverse osmosis filter 160 removes water thereby concentrating the ammonium bicarbonate in the solution.
  • the resulting concentrated effluent 164 out of the reverse osmosis filter 160 contains about 10 times the concentration of dissolved ammonium bicarbonate in the condenser effluent 154.
  • the permeate 162 is a clean water than can be reused or discharged.
  • the concentrated effluent 164 out of the reverse osmosis filter 160 is then treated at a temperature of less than about 35 degrees Celsius, preferably less than 20 degrees Celsius, in stage 3 using a crystallizer 170.
  • Solid crystals of ammonium bicarbonate are grown in the crystallizer 170 under controlled conditions, separated from the liquid fraction to produce an ammonium-salt 174 which may be dried, pelletized or granulated to form a final product.
  • a portion of the saturated ammonium bicarbonate supernatant is recycled
  • ammonium salt 174 solid, having physical and chemical properties as stated above for the first embodiment will result.
  • the ammonium salt can be stored 180 for use on or off site.
  • FIG. 3 Yet another embodiment of the invention using an external source for carbon dioxide is shown in Figure 3. Such an embodiment could be used for wastes that do not contain the carbon dioxide needed to convert the ammonia to ammonium bicarbonate. Examples of such wastes include waste not processed using anaerobic digestion, such as high-solids manure or other organic waste.
  • stage 1 and stage 2 are modified.
  • stage 1 comprises a dryer 247 in place of a stripper and stage 2 includes the addition of membrane modules 253 with a source of carbon dioxide 255 along with a condenser 250 and a reverse osmosis filter 260
  • the footnotes 1-4 denote the following:
  • [4] inject compressed vent gas (C02, H20, NH3) into ammonia water feed line.
  • the invention excludes the addition of chemicals to increase pH.
  • a solution of ammonium bicarbonate is created and crystallized as in the foregoing embodiments shown in Figure 1 and 2.
  • the separation of the gaseous ammonia from the waste 234 is performed using a dryer 247, an ammonia water is created using condensers 250, and gaseous carbon dioxide is contacted with the ammonia water solution using membrane device 253 to create a solution of ammonium bicarbonate.
  • the waste (such as layer manure) 234 is treated in stage 1 of the process of the invention which in this embodiment includes use of dryer 247.
  • the temperature of the dryer is at least about 80 degrees Celsius.
  • Dryer 247 operates at a sufficiently high temperature that the ammonia in the waste is converted to gas and removed with the water vapor.
  • the dryer functions as a separation device in a manner analogous to the distillation process 40 in Figure 1.
  • the exhaust vapor 242 from the dryer 247 contains water vapor and gaseous ammonia and lower than desired concentrations of carbon dioxide.
  • Figure 3 shows an example of a two-step condenser 250 to create an ammonia water 258 from the dryer exhaust gas 242.
  • the first step removes about one half of the water and nearly no ammonia (NH3) and the second step is complete condensation producing ammonia water at about 50 degrees Celsius or less.
  • the concentration of the dissolved ammonia in the condensate will be about twice that in the dryer vapor, for example about 0.5% by weight.
  • the non- condensed water and gases 252 exiting the condenser 250 can be discharged to the atmosphere.
  • ammonia water 258 is then treated in a membrane device 253 where an external source of gaseous carbon dioxide 255 is added.
  • the gaseous carbon dioxide passes through the membrane, dissolves into the ammonia water, and reacts to create a solution of ammonium bicarbonate 254.
  • the solution of ammonium bicarbonate may be 2.3% by weight ammonium bicarbonate at about pH 6.5 - 8.5, depending on the amount of C02 added and the temperature.
  • the ammonium bicarbonate 254 is then treated in a reverse osmosis filter 260.
  • Reverse osmosis filter 260 removes water thereby concentrating the ammonium bicarbonate in the solution.
  • the resulting concentrated effluent 264 out of the reverse osmosis filter 260 contains about 20 times the concentration of ammonia in the dryer gas.
  • the permeate 262 is a clean water than can be reused or discharged.
  • Stage 2 which includes the condenser 250, the membrane device 253 and the reverse osmosis filter 260 operate at a temperature of between about 35 degrees Celsius and 50 degrees Celsius.
  • the dissolved ammonium bicarbonate solution 264 is then treated in stage 3 using crystallization, similar to the embodiments shown in Figures 1 and 2.
  • the concentrated effluent 264 out of the reverse osmosis filter 260 is cooled to a temperature of less than about 35 degrees Celsius in stage 3 using a crystallizer 270.
  • Solid crystals of ammonium bicarbonate are grown in the crystallizer 270 under controlled conditions, separated from the liquid fraction to produce an ammonium-salt 274 which may be dried (such as using dryer 285), pelletized or granulated to form a final product.
  • a resulting ammonium salt solid having physical and chemical properties as stated above for the first and second embodiments will result. However, the certification as an organic product is contingent upon use of carbon dioxide produced organically. If synthetic carbon dioxide is used, the ammonium bicarbonate product cannot be designated as an organic fertilizer.
  • Carbon dioxide produced by fermentation of either animal waste or agricultural material is certifiably organic; and is readily available from agricultural sources to assure that the carbon dioxide is neither synthetic nor contaminated with synthetic carbon dioxide.
  • Figure 4 is a process flow schematic drawing of a variation on the embodiment of the invention shown in Figure 1 for the treatment of cattle manure (e.g., from a CAFO) comprising solids separation, anaerobic digestion, stripping, absorption, concentration, and crystallization.
  • cattle manure e.g., from a CAFO
  • the device could be a pressure swing adsorption device which is commonly used to separate gases, such as CH4 and C02, with materially different properties.
  • footnotes 1-5 denote the following: [1] - vapor is constant composition for continuous operation and varies during a batch process. H20, C02, and NH3 evolve with traces of organic volatiles and semi volatiles.
  • [2] - pressure control valve is set to maintain differential between stripper unit and absorber.
  • Absorber temperature, T must be less than 50 C to keep NH4 and HC03 in solution, while stripper temperature must be greater than 80 C to convert to NH3 and C02.
  • raw manure 10 with or without associated dairy waste generated at the CAFO is transported to a solids separation unit/process 20 (it being understood that a mixing or holding tank/vessel could be used prior to solids separation and/or can be used for solids separation).
  • the solids separation unit/process may be a single stage or chamber unit or it could be a series of stages or chambers for coarse solids separation and intermediate solids separation.
  • the slurry/effluent 24 from the solids separation unit 20 is input into an anaerobic digester 30 which digests much, preferably most, of the dissolved organics and small organic particulates to produce biogas 32 and an effluent digestate 34
  • the effluent digestate 34 from the anaerobic digester 30 contains residual solids, dissolved salts and organics, and concentrations of dissolved ammonia and carbon dioxide.
  • the present invention collects the ammonia and carbon dioxide and captures them in a subsequent multistage process to form solid ammonium bicarbonate. Each stage of the subsequent multistage process operates at different temperatures to take advantage of the solubility properties of ammonium bicarbonate for its concentration in dissolved form and then its formation as a nitrogen rich solid.
  • the temperature of digestate 34 out of a typical anaerobic digester treating cattle manure is about 35 degrees Celsius.
  • the digestate needs to be heated to greater than about 80 degrees Celsius for treatment in the stripper 40.
  • the stripper operating at a temperature of greater than about 80 degrees Celsius, without any chemical addition to increase pH, uses gas (biogas, CH4, C02, air, etc) to remove dissolved ammonia and dissolved carbon dioxide from the digestate 34 creating exhaust vapor 42
  • Vapor 42 containing water vapor, gaseous carbon dioxide, and gaseous ammonia. Vapor 42 will also contain traces of organic volatiles and semi-volatiles.
  • the treated water and solids 44 out of the stripper can be further treated for application to land or water using current treatment
  • the temperature of the stripper 40 can be maintained using a heat exchanger 46 to heat the recycled stripper gas 45 from the absorber.
  • the vapor 42 created by stripping the digestate 34 in that first stage, the separation stage, is then treated with a cold water stream 53 saturated with C02, in an absorption stage 50 to create a dissolved ammonium bicarbonate solution. Ammonia is removed from the vapor distillate, producing recycled stripper gas 45 which is heated in heat exchanger 46 prior to entry at the bottom of stripper 40.
  • Absorber 50 and reverse osmosis filter 60 are used to treat vapor 42 at a temperature of between about 35 degrees Celsius and 50 degrees Celsius.
  • a pressure control valve 48 can be used between the stripper 40 and the absorber 50 to maintain a differential between the two. Operating the absorber 50 between about 35 and 50 degrees Celsius allows the water vapor, ammonia, and carbon dioxide to form dissolved ammonium bicarbonate. Maintaining between about 35 and 50 degrees Celsius in the absorber 50, and a pH less than 9, prevents precipitation of dissolved ammonium bicarbonate or ammonium carbonate and keeps it in dissolved form. Temperature of the absorber 50 can be maintained by control of the flow and temperature of the cold water 53.
  • the effluent ammonium bicarbonate solution 54 is treated in a reverse osmosis filter 60.
  • Reverse osmosis filter 60 removes water thereby concentrating the ammonium bicarbonate in the solution.
  • the resulting concentrated effluent 64 out of the reverse osmosis filter 60 contains about 50-100 times the concentration of dissolved ammonium bicarbonate in the digestate 34.
  • Control of the reverse osmosis temperature is critical to avoid precipitation of the ammonium bicarbonate on the membrane while achieving a concentration sufficient for saturation at the temperature in the crystallizer.
  • the permeate 62 is a clean water than can be reused or discharged.
  • the concentrated effluent 64 out of the reverse osmosis filter 60 is then treated at a temperature of less than about 20 degrees Celsius in stage three using a crystallizer 70.
  • Solid crystals of ammonium bicarbonate are grown in the crystallizer 70 under controlled conditions, separated from the liquid fraction to produce an ammonium-salt 74 which may be dried, pelletized or granulated to form a final product.
  • a portion of the saturated ammonium bicarbonate supernatant is recycled 72 to the reverse osmosis filter 60, after it is heated to the required temperature in heat exchanger 56.
  • the resulting ammonium salt may be dried and packaged for commercial distribution as a specialized nitrogen fertilizer, that is high-purity, phosphorus free, and certified USDA organic.
  • the ammonia recovery step is the equivalent of distillation. This allows nearly no salt (including phosphorus salts) carry over to the input to reverse osmosis. Crystallization is another purification step, so that“high-purity, phosphorus free” product is achieved. If synthetic chemicals are not used in obtaining the solid AB or liquid digestate, the ammonium bicarbonate product will have the potential for designation as organic (USD A 2012) fertilizer.
  • the USD A designation is of economic importance as the price of organic fertilizer expressed as dollars per pound ammonia nitrogen, is materially higher than that of chemical (non-organic) fertilizers that are equally uniform, high purity, and concentrated sources of NH3-N. As with synthetic fertilizer, the material is nearly odorless, and has low transport and application costs relative to manure and digestate. If the ammonia is captured with an industrial acid or is derived from application of caustic or other industrial alkali - it will not qualify as organic fertilizer.
  • the ammonium salt according to the invention resolves this conflict by (1) producing ammonia gas thermally with no chemical addition, and (2) using the carbon dioxide found in the digestate to recover the ammonia from the digestate to form an organic fertilizer, ammonium bicarbonate.
  • the ammonium salt 74 can be stored 80 for use on or off site.
  • FIG. 5 is a process flow schematic drawing of a variation on the embodiment of the invention shown in Figure 1 for the treatment of livestock manure (e.g., from a Controlled Animal Feeding Operation, CAFO) comprising solids separation, physical influent conditioning, anaerobic digestion, stripping, condensation (concentration), absorption, and crystallization.
  • livestock manure e.g., from a Controlled Animal Feeding Operation, CAFO
  • CAFO Controlled Animal Feeding Operation
  • the present invention excludes the use of pH adjustment chemicals.
  • the carbon dioxide which derives directly from the livestock manure waste, is supplemented by carbon dioxide from the biogas to assure maintenance of C02 in the water to stabilize the ammonia in the absorber column.
  • Figure 5 shows the biogas 32 processed in a C02 removal device 35 to provide C02 to for capture of ammonia as ammonium bicarbonate.
  • the device could be a pressure swing adsorption device which is commonly used to separate gases, such as CH4 and C02, with materially different properties.
  • footnotes 1-4 denote the following:
  • [1] - vapor is constant composition for continuous operation and varies during a batch process. H20, C02, and NH3 evolve with traces of organic volatiles and semi volatiles.
  • [2] - pressure control valve(s) is set to maintain differentials between a) the stripper unit and the condenser, and b) the condenser and the absorber.
  • Absorber temperature, T must be less than 50 C to keep NH4 and HC03 in solution, while stripper temperature must be greater than 80 C to convert to NH3 and C02.
  • raw livestock manure 10 is transported to a solids separation and physical conditioning unit/process 20 (it being understood that a mixing or holding tank/vessel could be used prior to solids separation and/or can be used for solids separation).
  • the solids separation unit/process may be a single stage or chamber unit or it could be a series of stages or chambers for coarse solids separation, intermediate solids separation, and physical mixing and conditioning.
  • Physical conditioning may include dilution, grinding, mixing, heating etc., depending on the specific livestock manure processed; dilution may be necessary for some manure to provide the appropriate consistency and concentration for the AD, grinding and mixing may be needed to help solubilize and make more available the organic content for digestion, heating may be needed for the anaerobic digester influent but may also be used to sterilize and prevent biological competition during digestion.
  • the slurry/effluent 24 from the solids separation unit 20 is input into an anaerobic digester 30 which digests much, preferably most, of the dissolved organics and small organic particulates to produce biogas 32 and an effluent digestate 34.
  • the effluent digestate 34 from the anaerobic digester 30 contains residual solids, dissolved salts and organics, and concentrations of dissolved ammonia and carbon dioxide.
  • the present invention collects the ammonia and carbon dioxide and captures them in a subsequent multistage process to form solid ammonium bicarbonate. Each stage of the subsequent multistage process operates at different temperatures to take advantage of the solubility properties of ammonium bicarbonate for its concentration in dissolved form and then its formation as a nitrogen rich solid.
  • the temperature of digestate 34 out of a typical anaerobic digester treating livestock manure is about 35 degrees Celsius.
  • the digestate needs to be heated to greater than about 80 degrees Celsius for treatment in the stripper 40.
  • the stripper operating at a temperature of greater than about 80 degrees Celsius, without any chemical addition to increase pH, creates exhaust vapor 42 containing water vapor, gaseous carbon dioxide, and gaseous ammonia. Vapor 42 will also contain traces of organic volatiles and semi-volatiles.
  • the treated water and solids 44 out of the stripper can be further treated for application to land or water using current treatment technologies.
  • the water vapor 42 created by stripping the digestate 34 in that first stage, the separation stage, is then condensed in the condenser.
  • the condenser is operated as a single or multistage unit to condense the water vapor at a high temperature, to separate water from the gaseous ammonia and C02 effectively concentrating them in the gas.
  • the amount of ammonium carbonate and ammonium bicarbonate concentration in the concentrated gas is at least 2 times greater than in the gas before treatment with condensation and could be as high as 100 times to 1000 times higher.
  • the high temperature condensed water 55 is removed from the condenser and may be channeled back to the stripper to reclaim any re-dissolved ammonia and carbon dioxide, may be discharged from the process, may be used as seed liquid in the absorber, or may be recycled to combine with the fresh livestock manure entering the digester.
  • Absorber 50 is used to treat vapor 142 at a temperature of between about 20 degrees Celsius and 50 degrees Celsius.
  • Pressure control valves 48 can be used between the stripper 40, the condenser, and the absorber 50 to maintain proper differential pressure between the unit processes.
  • Operating the absorber 50 between about 20 and 50 degrees Celsius allows the water vapor, ammonia, and carbon dioxide to form dissolved ammonium bicarbonate. Maintaining between about 20 and 50 degrees Celsius in the absorber 50, and a pH less than 9, prevents precipitation of dissolved ammonium bicarbonate or ammonium carbonate and keeps it in dissolved form.
  • Temperature of the absorber 50 can be controlled with a heat exchanger 56 and by regulating the temperature of the carbon dioxide.
  • the amount of water used to generate the concentrated AB solution is minimized and controlled.
  • the ammonia and carbon dioxide gasses continue to absorb and form an AB solution in the controlled volume of water until they reach close to saturation at the selected temperature between 20 and 50 degrees Celsius.
  • the concentrated effluent 64 out of the absorber is then treated at a temperature of less than about 20 degrees Celsius in stage four using a crystallizer 70.
  • Solid crystals of ammonium bicarbonate are grown in the crystallizer 70 under controlled conditions, separated from the liquid fraction to produce an ammonium-salt 74 which may be dried, pelletized or granulated to form a final product.
  • the more dilute AB solution, following this crystallization process, is returned to the absorber as seed liquid to dissolve more ammonia and carbon dioxide as AB under the higher temperature conditions, between 20 and 50 degrees Celsius.
  • the embodiment of the invention shown in Figure 5 may increase the overall efficiency by potentially eliminating the need for any other concentrating unit process, specifically the RO, instead performing the concentration through removal of water vapor. Substantial reductions in capital cost, energy costs, operating costs, and maintenance costs could all be realized with that embodiment of the invention.
  • the potential for product losses may also be reduced by eliminating or reducing the reverse osmosis, especially since reverse osmosis operates at relatively high pressures.
  • a safer process may also created by eliminating or reducing the high pressure reverse osmosis, it being understood that the present invention also includes variations with the addition of a reverse osmosis step.
  • the embodiment of the invention shown in Figure 5 may eliminate the need for any other concentrating unit process, specifically the RO, instead performing the concentration through removal of water vapor in the partial condenser and capturing the dissolved AB in the absorber. Substantial reductions in capital cost, energy costs, operating costs, and maintenance costs may be realized with that embodiment of the invention. While the present invention has been illustrated by description of various embodiments and while those embodiments have been described in considerable detail, it is not the intention of applicant to restrict or in any way limit the scope of the appended claims to such details. Additional advantages and modifications will readily appear to those skilled in the art. The invention in its broader aspects is therefore not limited to the specific details and illustrative examples shown and described. Accordingly, departures may be made from such details without departing from the spirit or scope of applicants’ invention.

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Abstract

La présente invention concerne un procédé, une méthode et un système de récupération et de concentration de bicarbonate d'ammonium dissous à partir d'eaux usées contenant de l'ammoniac (NH3) utilisant une séparation de gaz, une condensation, et une cristallisation, chacune à des températures de fonctionnement contrôlées. La présente invention comprend 1) l'élimination de l'ammoniac à partir de déchets (boues, semi-solides, et solides et liquides) sans l'utilisation de produits chimiques à une température d'au moins 80 degrés Celsius, 2) la condensation du gaz contenant de l'ammoniac, du dioxyde de carbone et de la vapeur d'eau pour éliminer la vapeur d'eau concentrant la quantité d'ammoniac et de dioxyde de carbone gazeux, 3) la concentration de l'ammoniac et du dioxyde de carbone dans l'eau par des moyens établis, tels que la concentration du gaz à l'aide d'une condensation partielle suivie par le passage du gaz concentré à travers une colonne d'absorption à une température comprise entre environ 20 et 50 degrés Celsius pour former du carbonate d'ammonium et du bicarbonate d'ammonium dissous, ou la condensation totale suivie d'une déshydratation à l'aide d'une osmose inverse, et 4) la cristallisation du carbonate d'ammonium et du bicarbonate d'ammonium dissous concentrés à une température inférieure à environ 35 degrés Celsius pour former du bicarbonate d'ammonium et du carbonate d'ammonium solides.
PCT/US2018/067247 2018-12-21 2018-12-21 Procédé de récupération de bicarbonate d'ammonium à partir d'eaux usées WO2020131116A1 (fr)

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CA3123802A CA3123802A1 (fr) 2018-12-21 2018-12-21 Procede de recuperation de bicarbonate d'ammonium a partir d'eaux usees
PCT/US2018/067247 WO2020131116A1 (fr) 2018-12-21 2018-12-21 Procédé de récupération de bicarbonate d'ammonium à partir d'eaux usées
EP18943551.4A EP3898515A4 (fr) 2018-12-21 2018-12-21 Procédé de récupération de bicarbonate d'ammonium à partir d'eaux usées
MX2021007358A MX2021007358A (es) 2018-12-21 2018-12-21 Proceso para recuperar bicarbonato de amonio de aguas residuales.

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023057022A1 (fr) * 2021-10-06 2023-04-13 Comferm Holding Aps Récupération d'ammoniac par exemple à partir du compostage

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US3970739A (en) * 1974-04-11 1976-07-20 Sumitomo Chemical Company, Limited Process for concurrently treating process waste waters and flue gases from ammonia synthesis process plants
US6368849B1 (en) * 1998-02-20 2002-04-09 Bioscan A/S Method and plant for the treatment of liquid organic waste
US20160200613A1 (en) * 2015-01-14 2016-07-14 Morton Orentlicher Process to recover ammonium bicarbonate from wastewater

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Publication number Priority date Publication date Assignee Title
CS254717B1 (en) * 1985-02-06 1988-01-15 Jan Cervenka Process for working excrements of utility animals

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Publication number Priority date Publication date Assignee Title
US3970739A (en) * 1974-04-11 1976-07-20 Sumitomo Chemical Company, Limited Process for concurrently treating process waste waters and flue gases from ammonia synthesis process plants
US6368849B1 (en) * 1998-02-20 2002-04-09 Bioscan A/S Method and plant for the treatment of liquid organic waste
US20160200613A1 (en) * 2015-01-14 2016-07-14 Morton Orentlicher Process to recover ammonium bicarbonate from wastewater

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023057022A1 (fr) * 2021-10-06 2023-04-13 Comferm Holding Aps Récupération d'ammoniac par exemple à partir du compostage

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