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WO2024086525A1 - Procédé d'infusion de gaz pour traitement des eaux usées - Google Patents

Procédé d'infusion de gaz pour traitement des eaux usées Download PDF

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Publication number
WO2024086525A1
WO2024086525A1 PCT/US2023/076980 US2023076980W WO2024086525A1 WO 2024086525 A1 WO2024086525 A1 WO 2024086525A1 US 2023076980 W US2023076980 W US 2023076980W WO 2024086525 A1 WO2024086525 A1 WO 2024086525A1
Authority
WO
WIPO (PCT)
Prior art keywords
wastewater
saturator
inline
mixed liquor
biological reactor
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/US2023/076980
Other languages
English (en)
Other versions
WO2024086525A9 (fr
Inventor
Andre Luis MONUTTI
Giancarlo Marcus RONCONI
Mark Max MACKENZIE
Henrique Gozzo ZOADELLI
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Brk Ambiental Participacoes SA
Prosper Technologies LLC
Original Assignee
Brk Ambiental Participacoes SA
Prosper Technologies LLC
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Brk Ambiental Participacoes SA, Prosper Technologies LLC filed Critical Brk Ambiental Participacoes SA
Publication of WO2024086525A1 publication Critical patent/WO2024086525A1/fr
Publication of WO2024086525A9 publication Critical patent/WO2024086525A9/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/20—Mixing gases with liquids
    • B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/20—Mixing gases with liquids
    • B01F23/29—Mixing systems, i.e. flow charts or diagrams
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/40—Mixing liquids with liquids; Emulsifying
    • B01F23/45—Mixing liquids with liquids; Emulsifying using flow mixing
    • B01F23/454—Mixing liquids with liquids; Emulsifying using flow mixing by injecting a mixture of liquid and gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/50—Circulation mixers, e.g. wherein at least part of the mixture is discharged from and reintroduced into a receptacle
    • B01F25/53—Circulation mixers, e.g. wherein at least part of the mixture is discharged from and reintroduced into a receptacle in which the mixture is discharged from and reintroduced into a receptacle through a recirculation tube, into which an additional component is introduced
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1278—Provisions for mixing or aeration of the mixed liquor
    • C02F3/1289—Aeration by saturation under super-atmospheric pressure
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/03—Pressure
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/22—O2
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/40—Liquid flow rate
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/04—Flow arrangements
    • C02F2301/046—Recirculation with an external loop
    • 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
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • the invention is directed to a method of treating wastewater, and more particularly to a method of treating wastewater using gas infusion.
  • Wastewater treatment and in particular municipal sewage treatment usually requires aerobic steps and processes. In these stages the microorganisms present in the effluent (organic matter) when in contact with the presence of oxygen, promote reaction in which there is the conversion of the organic matter into carbon dioxide (CO2), water and inert compounds, eliminating the undesirable load. For this to occur, large volumes of oxygen are typically required, which need to be placed in contact with the effluent, in order to guarantee an adequate and stable aerobic environment to achieve the process.
  • CO2 carbon dioxide
  • a method of oxygenating wastewater for use aerobic wastewater treatment includes the step of recirculating a mixed liquor flow of wastewater from a biological reactor into an inlet of an inline saturator.
  • the method also includes the step of operating the inline saturator to saturate the mixed liquor flow with oxygen to form a supersaturated mixed liquor flow having a level of dissolved oxygen concentration of between 30 ppm and 70 ppm.
  • the method also includes the step of returning the supersaturated mixed liquor flow from an outlet of the inline saturator to the biological reactor.
  • Figure 1 is a schematic view of a wastewater treatment system and method using gas infusion.
  • Figure 2 is a schematic view of a wastewater treatment system and method using gas infusion.
  • Figure 3 is a schematic view of a connection to the aeration tank in the wastewater treatment system of FIGS. 1-2.
  • Figure 4 is a chart showing improvement in BOD removal using gas infusion system of FIGS. 1 and 2.
  • This application relates to methods for wastewater treatment (e.g., industrial and/or municipal wastewater treatment )and more specifically to improved methods for facilitating biological processes in wastewater treatment.
  • wastewater treatment e.g., industrial and/or municipal wastewater treatment
  • the methods described herein facilitate infuse wastewater with oxygen rather than air, and the infusion of wastewater with oxygen in a manner free of bubbles to supersaturate the wastewater with oxygen.
  • FIG. 1 shows a schematic diagram of a wastewater treatment system 1800 utilizing gas infusion modules to infuse the wastewater with oxygen.
  • the system 1800 includes a first gas infusion unit or first inline saturator (ILS #1) 1810 and a second gas infusion unit or second inline saturator (ILS #2) 1820.
  • the first inline saturator 1810 and the second inline saturator 1820 can infuse wastewater with oxygen as further described below
  • the first inline saturator 1810 receives wastewater from two locations: via a first feed pump 1860 from a pipe between an aeration tank and a clarifier tank, and from a pipe downstream of the clarifier tank of the wastewater treatment plant; and from a pipe between an anaerobic treatment tank or Upflow Anaerobic Sludge Blanket (UASB) and an aeration tank of the wastewater treatment plant via a second feed pump 1870.
  • UASB Upflow Anaerobic Sludge Blanket
  • the first inline saturator 1810 infuses the wastewater with oxygen and delivers the oxygen saturated wastewater to a biological reactor 1830, which thereafter tank 1840 is directed to the biological reactor 1830 via a RAS pump 1850.
  • Wastewater is recirculated from the clarifier tank 1840 via a third feed pump 1880 to the second inline saturator 1820.
  • the second inline saturator 1820 infuses the recirculated wastewater with oxygen (e.g., in the same manner as the first inline saturator 1810), and delivers the oxygen saturated wastewater to the biological reactor 1830.
  • Wastewater is thereafter transferred from the biological reactor 1830 to a clarifier tank 1840.
  • a portion of the wastewater flow is recirculated from the clarifier tank 1840 to the aeration tank of the existing wastewater treatment plant, and thereafter passes through the clarifier of the existing wastewater treatment plant, as shown in FIG. 1.
  • FIG. 2 shows a schematic diagram of a wastewater treatment system 1800’ (hereafter “the system 1800’ ”).
  • the system 1800 Some of the features of the system 1800’ are similar to features of the system 1800 in FIG. 2.
  • reference numerals used to designate the various components of the system 1800’ are identical to those used for identifying the corresponding components of the system 1800 in FIG. 1, except that a “ ’ ” has been added to the numerical identifier. Therefore, the structure and description for the various features of the system 1800 and how it’s operated and controlled in FIG. 1 are understood to also apply to the corresponding features of the system 1800’ in FIG. 2, except as described below.
  • the system 1800’ differs from the system 1800 in that the second inline saturator 1820’ receives wastewater (e.g., mixed liquor) recirculated by the third feed pump 1880’ from the biological reactor 1830’, not from the output of the clarifier tank 1840’.
  • wastewater e.g., mixed liquor
  • this arrangement did not impact the surface overflow rate (SOR) and solids load rate (SLR) in the clarifier tank 1840’ (as operation of the system 1800 did) and resulted in improved solids and BOD removal.
  • both the first inline saturator 1810’ and the second inline saturator 1820’ were operated.
  • only the second inline saturator 1820’ was operated. That is, the first inline saturator 1810’ was not operated (e.g., the pump I860’ was closed.
  • the pipe 1835, 1835’ between (e.g., connecting) the biological reactor 1830, 1830’ and the clarifier tank 1840, 1840’ was moved toward the bottom of the biological reactor 1830, 1830’ and the clarifier tank 1840, 1840’, which advantageously reduced the amount of lighter solids sent to the clarifier tank 1840, 1840’ (which are more difficult to decant and separate), as compared with having the pipe 1835, 1835’ toward the top of the biological reactor 1830, 1830’ and the clarifier tank 1840, 1840’.
  • pipe 1835, 1835’ between (e.g., connecting) the biological reactor 1830, 1830’ and the clarifier tank 1840, 1840’ at the bottom allowed for scum generated in the biological reactor 1830, 1830’ to be retained therein. Further a drainage pipe 1837, 1837’ was added at the top of the biological reactor 1830, 1830’, which facilitated the removal of scum formed therein. Additionally, deflectors (not shown) were installed before the clarifier launders, which improved the removal of solids and BOD.
  • the first inline saturator 1810’ supplied oxygen saturated wastewater at a flowrate of between 20 LPM and 60 LPM, such as 30 LPM (on average) and with dissolved oxygen of between 30 ppm and 70 ppm, such as 62 ppm to the biological reactor 1830’.
  • the pump 1880’ recirculated wastewater from the biological reactor 1830’ to the second inline saturator 1820’ at a flowrate of between 90 LPM and 150 LPM, such 150 LPM (or an average of 120 LPM), and the second inline saturator 1820’ supplied oxygen saturated waste water at a flowrate of 90 LPM and 150 LPM, such as 150 LPM (or an average of 120 LPM) and with dissolved oxygen of between 30 ppm and 70 ppm, such as 62 ppm, to the biological reactor 1830’.
  • the biological reactor 1830’ operated at a hydraulic retention time (HRT) of 7.2 hours (e.g., the amount of time the wastewater remained in the biological reactor 1830’ before being discharged therefrom).
  • first inline saturator 1810’ and the second inline saturator 1820’ operated at pressures of between 20 psi and 30 psi (e.g., an average of 25 psi).
  • the second inline saturator 1820’ supplied oxygen saturated wastewater at a flowrate of between 90 LPM and 150 LPM, such as 120 LPM (on average) and with dissolved oxygen between 30 ppm and 70 ppm, such as 62 ppm, to the biological reactor 1830’.
  • the pump 1880’ recirculated wastewater from the biological reactor 1830’ to the second inline saturator 1820’ at a flowrate of between 90 LPM and 150 LPM.
  • the biological reactor 1830’ operated at a hydraulic retention time (HRT) of 7.2 hours (e.g., the amount of time the wastewater remained in the biological reactor 1830’ before being discharged therefrom).
  • the clarifier tank 1840’ also operated at a hydraulic retention time (HRT) of 7.2 hours.
  • the second inline saturator 1820’ operated at pressures of between 20 psi and 30 psi (e.g., an average of 25 psi).
  • the system 1800’ operated at a temperature between 15°C and 30°C, such as 25°C on average, and a raw sewage BOD of between 100 and 240 mg/1.
  • the system 1800’ advantageously achieved a 95% reduction in BOD in the effluent flow, exceeding the required 80% removal target.
  • the system 1800’ achieved steady state of operation, it achieved an 87% reduction in BOD in the effluent flow (exceeding the required 80% removal target), up from an initial 44% reduction when the system 1800 was initially put into operation.
  • the improved 95% reduction in BOD in the effluent flow was achieved following, among other modification, an increase in the hydraulic retention time (HRT) to that described above, and the increase in recirculation flowrate to the second inline saturator 1820’ described above.
  • the first inline saturator 1810’ can be excluded and only the second inline saturator 1820’ can be operated in the system 1800’ to provide oxygen saturated wastewater to the biological reactor 1830’.
  • the gas infusion system and method (e.g., oxygen infusion system and method) described herein provide various advantages in the treatment of wastewater. For example, because infusion of wastewater with oxygen occurs in a bubble-free gas transfer thc aeration tank, allowing the saturation of wastewater with oxygen to improve the biological process in the aeration tank (e.g., biological reactor), such as by more efficient oxygenation and use of available oxygen. As a result, a significant reduction in power (e.g., by as much as 50%, 60% or more) is achieved as air blowers and other equipment typically uses in wastewater treatment plants for the aeration process can be replaced and/or augmented with inline gas infusion as described herein.
  • aeration tank e.g., biological reactor
  • gas infusion systems described herein advantageously achieve a reduction of biochemical oxygen demand (BOD) (e.g., up to 95%, as shown in FIG. 4), allow for a reduced footprint for blower requirements, thereby reducing plant size and capital expenditures.
  • BOD biochemical oxygen demand
  • an augment system for an acetabular cup may be in accordance with any of the following clauses:
  • a method of oxygenating wastewater for use aerobic wastewater treatment comprising: recirculating a mixed liquor flow of wastewater from a biological reactor into an inlet of an inline saturator; operating the inline saturator to saturate the mixed liquor flow with oxygen to form a supersaturated mixed liquor flow having a level of dissolved oxygen concentration of between 30 ppm and 70 ppm; and returning the supersaturated mixed liquor flow from an outlet of the inline saturator to the biological reactor.
  • Clause 2 The method of Clause 1, wherein the level of dissolved oxygen concentration is about 62 ppm.
  • Clause 3 The method of Clause 1, wherein recirculating the mixed liquor flow from the biological reactor includes flowing the mixed liquor flow at a rate of between 90 LPM and 150 LPM.
  • Clause 4 The method of Clause 3, wherein recirculating the mixed liquor flow from the biological reactor includes flowing the mixed liquor flow at a rate of 150 LPM.
  • thc biological reactor includes recirculating flow from a pipe between the biological reactor and a clarifier tank, the pipe extending between bottom portions of the biological reactor and the clarifier tank.
  • Clause 6 The method of Clause 1, wherein operating the inline saturator includes operating the inline saturator at a pressure of between 20 psi and 30 psi.
  • Clause 7 The method of Clause 6, wherein operating the inline saturator includes operating the inline saturator at a pressure of 25 psi.
  • Clause 8 The method of Clause 1, further comprising flowing wastewater through a second inline saturator and operating the second inline saturator to saturate the wastewater with oxygen to form a supersaturated wastewater flow having a level of dissolved oxygen concentration of between 30 ppm and 70 ppm, and flowing the supersaturated wastewater flow to the biological reactor.
  • Clause 9 The method of Clause 8, wherein flowing the wastewater through the second inline saturator includes flowing the wastewater at a rate of between 20 LPM and 60 LPM.
  • Clause 10 The method of Clause 9, wherein flowing the wastewater through the second inline saturator includes flowing the wastewater at a rate of 30 LPM.
  • Clause 11 The method of Clause 8, wherein operating the second inline saturator includes operating the inline saturator at a pressure of between 20 psi and 30 psi.
  • Clause 12 The method of Clause 11, wherein operating the second inline saturator includes operating the inline saturator at a pressure of 25 psi.
  • Clause 13 The method of Clause 1, wherein the supersaturated mixed liquor flow achieves BOD removal in the wastewater of at least 80%.
  • Conditional language such as “can,” “could,” “might,” or “may,” unless specifically stated otherwise, or otherwise understood within the context as used, is generally intended to convey that certain embodiments include, while other embodiments do not include, certain features, elements, and/or steps. Thus, such conditional language is not generally intended to imply that features, elements, and/or steps are in any way required for one or more embodiments or that one or more embodiments necessarily include logic for deciding, with or without user input or prompting, whether these features, elements, and/or steps are included or are to be performed in any particular embodiment.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Activated Sludge Processes (AREA)

Abstract

L'invention concerne un procédé de traitement des eaux usées comprenant la recirculation d'une liqueur mixte provenant d'un réacteur biologique ou d'un réservoir d'aération au travers d'un saturateur de gaz en ligne où la liqueur mixte est saturée en oxygène. L'oxygène est transféré aux eaux usées sans bulles d'oxygène et permet une réduction de la demande en énergie pour le processus d'aération des eaux usées.
PCT/US2023/076980 2022-10-20 2023-10-16 Procédé d'infusion de gaz pour traitement des eaux usées Ceased WO2024086525A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US202263380377P 2022-10-20 2022-10-20
US63/380,377 2022-10-20

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WO2024086525A1 true WO2024086525A1 (fr) 2024-04-25
WO2024086525A9 WO2024086525A9 (fr) 2024-06-06

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4141823A (en) * 1975-08-05 1979-02-27 The British Oxygen Company Limited Treatment of waste water
US20010040134A1 (en) * 2000-01-20 2001-11-15 Mg Industries System and method for oxygenation of waste water
US20020070163A1 (en) * 2000-12-13 2002-06-13 Lambert Russell E. Wastewater treatment apparatus and method
US7163632B1 (en) * 2006-01-30 2007-01-16 Speece Richard E System and method for oxygenation for wastewater treatment
US20120325741A1 (en) * 2004-05-25 2012-12-27 Gregory Scott Osborn Systems and Methods for Wastewater Treatment
US20220355256A1 (en) * 2021-05-06 2022-11-10 Prosper Technologies, Llc Oxygen infusion module for wastewater treatment

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4141823A (en) * 1975-08-05 1979-02-27 The British Oxygen Company Limited Treatment of waste water
US20010040134A1 (en) * 2000-01-20 2001-11-15 Mg Industries System and method for oxygenation of waste water
US20020070163A1 (en) * 2000-12-13 2002-06-13 Lambert Russell E. Wastewater treatment apparatus and method
US20120325741A1 (en) * 2004-05-25 2012-12-27 Gregory Scott Osborn Systems and Methods for Wastewater Treatment
US7163632B1 (en) * 2006-01-30 2007-01-16 Speece Richard E System and method for oxygenation for wastewater treatment
US20220355256A1 (en) * 2021-05-06 2022-11-10 Prosper Technologies, Llc Oxygen infusion module for wastewater treatment
US20220356097A1 (en) * 2021-05-06 2022-11-10 Prosper Technologies, Llc Methods of gas infusion for wastewater treatment
US20220356096A1 (en) * 2021-05-06 2022-11-10 Prosper Technologies, Llc Systems of gas infusion for wastewater treatment

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
TUMPA MONDAL: "Aerobic wastewater treatment technologies: A mini review", INTJ ENV TECH SCI, vol. 4, 30 December 2017 (2017-12-30), pages 135 - 140, XP093166859 *

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