# US 11,305,233 B2 · System, device and method for production of high-nitrogen organic liquid fertilizer from ammonia rich wastewaters and digester effluents > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 11,305,233 B2 - Document ID: US11305233B2 - Status: Granted - Kind: B2 - Application number: 16/431,579 - Filed: 2019-06-04 - Published: 2019-12-05 - Granted: 2022-04-19 - Earliest claimed: 2018-06-04 - Assignees: CleanWorld - Applicants: CleanWorld - Inventors: Joshua L. Rapport; Caleb Adams - Web page: https://patentgrep.com/patent/US11305233B2 ## CPC - B01D 61/147: {Microfiltration} - B01D 61/16: Feed pretreatment - B01D 61/58: Multistep processes - B01D 65/02: Membrane cleaning or sterilisation {; Membrane regeneration} - C02F 1/004: {using large scale industrial sized filters} - C02F 1/041: {by means of vapour compression} - C02F 1/444: {by ultrafiltration or microfiltration} - C02F 9/00: Multistage treatment of water, waste water or sewage - B01D 61/025: {Reverse osmosis; Hyperfiltration} - B01D 2311/04: Specific process operations in the feed stream; Feed pretreatment - B01D 2311/06: Specific process operations in the permeate stream - B01D 2311/18: pH control - B01D 2311/2649: Filtration - B01D 2321/02: Forward flushing - B01D 2321/08: Use of hot water or water vapor - B01D 2321/164: Use of bases - C02F 1/20: by degassing, i.e. liberation of dissolved gases (degasification of liquids in general B01D19/00; arrangement of degassing apparatus in boiler feed supply F22D) - C02F 1/441: {by reverse osmosis} - C02F 1/66: by neutralisation; pH adjustment (for degassing C02F1/20; using ion-exchange C02F1/42; for flocculation or precipitation of suspended impurities C02F1/52; for removing dissolved compounds C02F1/58) - C02F 11/04: Anaerobic treatment; Production of methane by such processes - C02F 11/122: using filter presses (C02F11/123 takes precedence) - C02F 11/125: using screw filters - C02F 11/13: by heating - C02F 2101/16: Nitrogen compounds, e.g. ammonia - C02F 2103/32: from the food or foodstuff industry, e.g. brewery waste waters - C02F 2201/002: Construction details of the apparatus - C02F 2209/003: Downstream control, i.e. outlet monitoring, e.g. to check the treating agents, such as halogens or ozone, leaving the process - C02F 2209/06: pH - C02F 2303/16: Regeneration of sorbents, filters - C02F 2303/22: Eliminating or preventing deposits, scale removal, scale prevention (C02F1/042, C02F1/4602, C02F5/00 take precedence) - C05F 7/005: {Waste water from industrial processing material neither of agricultural nor of animal origin} - Y02W 10/20: Sludge processing - B01D: SEPARATION (separating solids from solids by wet methods B03B, B03D; by pneumatic jigs or tables B03B; by other dry methods B07; magnetic or electrostatic separation of solid materials from solid materials or fluids, separation by high-voltage electric fields B03C; centrifuges, vortex apparatus B04; presses per se for squeezing-out liquid from liquid-containing material B30B9/02; treatment of water C02F, e.g. softening by ion-exchange C02F1/42; {arrangements of air intake cleaners in gas turbine plants F02C7/05} ; arrangements or mounting of filters in air-conditioning, air-humidification or ventilation F24F13/28) - C02F: TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE (separation in general B01D; special arrangements on waterborne vessels of installations for treating water, waste water or sewage, e.g. for producing fresh water, B63J; adding materials to water to prevent corrosion C23F; treating radioactively-contaminated liquids G21F9/04; regeneration of reactants for recirculation into processes, see the relevant places for the processes) - C05F: ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE - Y02W: CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT ## Abstract A method, system and device for recovering a desired nutrient from wastewater or digester effluents while separating the remaining components into various side streams which may have additional value or be suitable for inexpensive disposal due to the processing. ## Claims ### Claim 1 A method of recovering ammonia from wastewater, the method comprising: filtering a first set of solids from an input slurry medium including ammonia by pressing the slurry medium through a plurality of screens of a screw press, wherein each subsequent one of the screens through which the slurry medium is forced has smaller apertures than the previous one of the screens; filtering a second set of solids from the input slurry medium as output by the screw press with a static bag filter and pumping resulting filtrate to one or more storage tanks; for each of a plurality of batches of the filtrate: filtering a third set of solids from the batch of the filtrate without using coagulating or flocculating polymers by forcing the batch through at least one ultra-fine membrane producing a remaining permeate; and cleaning the membrane after the batch has been completely filtered by flushing water through the membrane before a next one of the batches is forced through the membrane, wherein the water is between 80 and 140 degrees Fahrenheit; adjusting a pH level of the remaining permeate by mixing the remaining permeate with a bicarbonate medium when the pH level is below a threshold value forming an adjusted permeate and pumping the adjusted permeate to one or more stripping columns via a permeate pipeline; and thermo-physically recovering the ammonia from the adjusted permeate by steam stripping the adjusted permeate in the one or more stripping columns thereby producing vaporized ammonia, channeling the vaporized ammonia to one or more condensing columns and condensing the vaporized ammonia in the condensing columns without acid scrubbing the vaporized ammonia. ### Claim 2 (depends on 1) The method of claim 1, wherein adjusting the pH level of the remaining permeate comprises dynamically injecting the bicarbonate medium into the permeate pipeline at an injection rate, wherein the injection rate is dynamically adjusted based on a measured pH level of the adjusted permeate within the permeate pipeline after the bicarbonate medium has been injected such that the measured pH level remains above a target value. ### Claim 3 (depends on 1) The method of claim 1, further comprising cleaning the membrane by adjusting a pH level of the water to 12 with sodium hydroxide and flushing the pH adjusted water through the membrane. ### Claim 4 (depends on 3) The method of claim 3, wherein the membrane is a part of a membrane system positioned within a skid and has an inlet for receiving the batches and a plurality of outputs for outputting the permeate. ### Claim 5 (depends on 4) The method of claim 4, further comprising additional ultra-fine membranes that are a part of the membrane system, wherein the additional ultra-fine membranes are composed of pores having diameters between 0.01 and 0.1 microns. ### Claim 6 (depends on 1) The method of claim 1, wherein a first screen of the screens has apertures between 0.5 to 2 millimeters in diameter and a second screen of the screens has apertures between 100 to 250 microns in diameter. ### Claim 7 (depends on 1) The method of claim 1, wherein the static bag filter includes pores having diameters between 400 to 500 microns. ### Claim 8 (depends on 1) The method of claim 1, wherein filtering the first set of solids further comprises running the slurry medium through a shaker deck having one or more shaker screens. ### Claim 9 (depends on 1) The method of claim 1, further comprising refluxing a portion of the ammonia resulting from at least one of the one or more condensing columns back into the one or more stripping columns in order to increase the concentration of the vaporized ammonia. ### Claim 10 (depends on 1) The method of claim 1, wherein the steam stripping comprises generating steam from the adjusted permeate by heating the adjusted permeate with a heat exchanger coupled to the one or more stripping columns. ### Claim 11 (depends on 1) The method of claim 1, further comprising pumping wastewater exiting the one or more stripping columns after the ammonia has been recovered into a reverse osmosis system that separates salt from the wastewater. ### Claim 12 (depends on 1) The method of claim 1, further comprising cleaning the one or more stripping columns and associated piping with acidic and/or basic solutions to remove organic and/or inorganic precipitates. ### Claim 13 An ammonia wastewater recovery system, the system comprising: a first filtering apparatus including a screw press that filters a first set of solids from an input slurry medium including ammonia by pressing the slurry medium through a plurality of screens of the screw press, wherein each subsequent one of the screens through which the slurry medium is forced has smaller apertures than the previous one of the screens; a second filtering apparatus coupled with an output of the first filtering apparatus and including a sump, one or more storage tanks and a static bag filter, wherein the sump pumps the input slurry medium as output by the first filtering apparatus through the static bag filter thereby removing a second set of solids from the input slurry medium and pumps resulting filtrate output by the static bag filter into the one or more storage tanks; a third filtering apparatus coupled with an output of the storage tanks via one or more input valves and including one or more output valves and at least one ultra-fine membrane, wherein for each of a plurality of batches of the filtrate received from the storage tanks the third filtering apparatus: filters a third set of solids from the batch of the filtrate without using coagulating or flocculating polymers by forcing the batch through the at least one ultra-fine membrane producing a remaining permeate; and cleans the membrane after the batch has been completely filtered by the at least one ultra-fine membrane by flushing water through the at least one ultra-fine membrane before a next one of the batches is forced through the at least one ultra-fine membrane, wherein the water is between 80 and 140 degrees Fahrenheit; a pH adjustment apparatus coupled with the third filtering apparatus and including an adjustment tank and an adjustment pump, wherein the pH adjustment apparatus adjusts a pH level of the remaining permeate by mixing the remaining permeate with a bicarbonate medium when the pH level is below a threshold value forming an adjusted permeate and pumping the adjusted permeate to one or more stripping columns via a permeate pipeline; and thermo-physical ammonia recovery apparatus including the one or more stripping columns coupled with one or more condensing columns, wherein the recovery apparatus recovers the ammonia from the adjusted permeate by steam stripping the adjusted permeate in the one or more stripping columns thereby producing vaporized ammonia, channeling the vaporized ammonia to the one or more condensing columns and condensing the vaporized ammonia in the one or more condensing columns without acid scrubbing the vaporized ammonia. ### Claim 14 (depends on 13) The system of claim 13, wherein the adjustment apparatus comprises an injection line coupled with the permeate pipeline and a pH sensor, and further wherein adjusting the pH level of the remaining permeate comprises dynamically injecting the bicarbonate medium into the permeate pipeline at an injection rate with the adjustment pump, wherein the injection rate is dynamically adjusted based on a measured pH level of the adjusted permeate as measured by the pH sensor within the permeate pipeline after the bicarbonate medium has been injected such that the measured pH level remains above a target value. ### Claim 15 (depends on 13) The system of claim 13, wherein the third filtering apparatus cleans the membrane by adjusting a pH level of the water to 12 with sodium hydroxide and flushing the pH adjusted water through the membranes. ### Claim 16 (depends on 15) The system of claim 15, wherein the membrane is coupled together with an input and a plurality of outputs within a self-contained skid. ### Claim 17 (depends on 16) The system of claim 16, further comprising additional membranes, wherein the membranes are composed of material that filters suspended solids having diameters greater than between 0.01 and 0.1 microns. ### Claim 18 (depends on 13) The system of claim 13, wherein a first screen of the screens has apertures between 0.5 to 2 millimeters in diameter and a second screen of the screens has apertures between 100 to 250 microns in diameter. ### Claim 19 (depends on 13) The system of claim 13, wherein the static bag filter includes pores having diameters between 400 to 500 microns. ### Claim 20 (depends on 13) The system of claim 13, wherein filtering the first set of solids further comprises running the slurry medium through a shaker deck having one or more shaker screens. ### Claim 21 (depends on 13) The system of claim 13, wherein the recovery apparatus refluxes a portion of the ammonia resulting from at least one of the one or more condenser columns back into the one or more stripping columns through a feedback channel in order to increase the concentration of the recovered ammonia. ### Claim 22 (depends on 13) The system of claim 13, wherein the recovery apparatus includes a heat exchanger and the steam stripping comprises generating steam from the adjusted permeate by heating the adjusted permeate with a heat exchanger coupled to the one or more stripping columns. ### Claim 23 (depends on 13) The system of claim 13, further comprising a reverse osmosis system that receives wastewater exiting the one or more stripping columns after the ammonia has been recovered and separates salt from the wastewater. ### Claim 24 (depends on 13) The system of claim 13, further comprising a cleaning system that cleans the one or more stripping columns and associated piping with acidic and/or basic solutions to remove organic and/or inorganic precipitates. ### Claim 25 A method of recovering ammonia from wastewater, the method comprising: filtering a first set of solids from an input slurry medium including ammonia by pressing the slurry medium through a plurality of screens of a screw press, wherein each subsequent one of the screens through which the slurry medium is forced has smaller apertures than the previous one of the screens, wherein filtering the first set of solids further comprises running the slurry medium through a shaker deck having one or more shaker screens; filtering a second set of solids from the input slurry medium as output by the screw press with a static bag filter and pumping resulting filtrate to one or more storage tanks; for each of a plurality of batches of the filtrate: filtering a third set of solids from the batch of the filtrate without using coagulating or flocculating polymers by forcing the batch through a plurality of ultra-fine membranes producing a remaining permeate, wherein each subsequent one of the membranes through which the batch is forced has smaller pores than the previous one of the membranes; and cleaning the membranes after the batch has been completely filtered by the membranes by preparing an alkaline wash by adjusting a pH level of wash water to 12 with sodium hydroxide, flushing the alkaline wash through the membranes, and then flushing rinse water through the membranes before a next one of the batches is forced through the membranes, wherein the rinse water is between 80 and 140 degrees Fahrenheit; adjusting a pH level of the remaining permeate by mixing the remaining permeate with a bicarbonate medium when the pH level is below a threshold value forming an adjusted permeate and pumping the adjusted permeate to one or more stripping columns via a permeate pipeline, wherein adjusting the pH level of the remaining permeate comprises dynamically injecting the bicarbonate medium into the permeate pipeline at an injection rate, wherein the injection rate is dynamically adjusted based on a measured pH level of the adjusted permeate within the permeate pipeline after the bicarbonate medium has been injected such that the measured pH level remains above a target value; thermo-physically recovering the ammonia from the adjusted permeate by steam stripping the adjusted permeate in the one or more stripping columns thereby producing vaporized ammonia, channeling the vaporized ammonia to one or more condensing columns and condensing the vaporized ammonia in the condensing columns without acid scrubbing the vaporized ammonia, wherein the steam stripping comprises generating steam from the adjusted permeate by heating the adjusted permeate with a heat exchanger coupled to the one or more stripping columns; and pumping wastewater exiting the one or more stripping columns after the ammonia has been recovered into a reverse osmosis system that separates salt from the wastewater. ### Claim 26 (depends on 25) The method of claim 25, further comprising cleaning the one or more stripping columns and associated piping with acidic and/or basic solutions to remove organic and/or inorganic precipitates.