WO2014178711A1 - Processus d'épuration anaérobie des eaux usées - Google Patents

Processus d'épuration anaérobie des eaux usées Download PDF

Info

Publication number
WO2014178711A1
WO2014178711A1 PCT/NL2014/050266 NL2014050266W WO2014178711A1 WO 2014178711 A1 WO2014178711 A1 WO 2014178711A1 NL 2014050266 W NL2014050266 W NL 2014050266W WO 2014178711 A1 WO2014178711 A1 WO 2014178711A1
Authority
WO
WIPO (PCT)
Prior art keywords
sludge
liquid
reactor vessel
granular
process according
Prior art date
Application number
PCT/NL2014/050266
Other languages
English (en)
Inventor
René Alexander ROZENDAL
Rienk Prins
Petrus Cornelis Van Der Heijden
Original Assignee
Paques I.P. B.V.
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 Paques I.P. B.V. filed Critical Paques I.P. B.V.
Publication of WO2014178711A1 publication Critical patent/WO2014178711A1/fr

Links

Classifications

    • 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
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
    • 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
    • C02F1/48—Treatment of water, waste water, or sewage with magnetic or electric fields
    • 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

Definitions

  • the present invention relates to a process for anaerobic wastewater treatment wherein granular and non-granular sludge are formed.
  • a sludge granule is an aggregate of microorganisms that is often formed during wastewater treatment in the absence of any support matrix, such as for example in a constant upflow hydraulic regime. Under these conditions, the microorganisms present survive and proliferate by attaching to each other.
  • the aggregates of microorganisms eventually form dense granules, typically with a diameter in the range of from 0.5 to 5 mm, often referred to as granular sludge. Due to their high density and therewith high settling rates, granular sludge resists washing out from a wastewater treatment reactor, even at high hydraulic loads.
  • the high density allows for a high concentration of granular sludge and thus of active microorganisms and therewith a high conversion of organic material contained in the wastewater can be achieved.
  • One gram of granular sludge is typically able to convert in the range of from 0.1 to 1.0 grams of Chemical Oxygen Demand (COD) per day into methane.
  • COD Chemical Oxygen Demand
  • Granular sludge is typically formed in upflow anaerobic wastewater reactors such as an Upflow Anaerobic Sludge Bed (UASB) reactor or an Expanded Granular Sludge Bed (EGSB). Whether sludge will be formed in a wastewater treatment reactor and whether the sludge formed will be dense granular sludge or non-dense nongranular sludge, such as dispersed or flocculent sludge, will depend on the process conditions applied, in particular the hydraulic retention time. In L. W. Hulshoff Pol et al. Water Research 38 (2004), p. 1376-1389 details on the sludge granulation process in anaerobic wastewater treatment are given.
  • UASB Upflow Anaerobic Sludge Bed
  • EVSB Expanded Granular Sludge Bed
  • granular sludge Since granular sludge has a high density, it has a high settling velocity, typically in the order of 60 m/h. In an upflow reactor, such as for example an UASB reactor, the granular sludge is therefore retained in the reactor. Non-granular sludge has a much lower density and settling velocity. In many reactor regimes, the upflow velocity is larger than the settling velocity of any non-granular sludge formed and nongranular sludge is typically discharged from the reactor with the effluent of treated wastewater. Since UASB reactors are typically operated with a dilution rate, i.e.
  • Reference herein to the maximum specific growth rate ( ⁇ ⁇ ⁇ ) of sludge is to the rate of sludge production (weight increase per time unit) per weight of sludge present in a certain reaction volume under ideal growth conditions.
  • Wastewater streams, in particular industrial wastewater streams tend to become more concentrated in organic waste material, usually expressed as Chemical Oxygen Demand (COD).
  • COD is the amount of oxygen that would be needed to oxidize the organic material in a litre of wastewater.
  • Conventional upflow anaerobic wastewater treatment reactors are typically able to treat wastewater streams with a COD up to approximately 20 g/L.
  • much larger hydraulic residence times would be needed than are typically applied in anaerobic wastewater treatment reactors wherein organic material is converted into methane using granular sludge.
  • the dilution rate When applying large hydraulic retention times (the hydraulic retention time being the inverse of the dilution rate), the dilution rate will be lower than the maximum specific growth rate of the non-granular sludge. As a result, the amount of non-granular sludge in the reactor will increase at the detriment of the concentration of granular sludge. It has been acknowledged in L. W. HulshoffPol et al. Water Research 38 (2004), p. 1376-1389 that selective washout of dispersed sludge results in increased growth of heavier sludge agglomeration. Also the reverse is true: less washout of dispersed sludge results in decreased growth of heavier sludge agglomeration.
  • an anaerobic wastewater treatment process wherein granular sludge is formed can be operated in such way that concentrated wastewater can be treated without the need for very large reactor volumes.
  • removing or inactivating at least part of any non-granular sludge present in the treated wastewater stream and recycling a stream of treated waste water depleted in active non-granular sludge to the reactor or, in case the removal or inactivation takes place inside the reactor, maintaining such stream in the reactor, a large retention time of the wastewater to be treated is achieved, whilst the retention time of any non-granular sludge is kept low.
  • the present invention relates to a process for anaerobic wastewater treatment wherein granular and non-granular sludge are formed, the process comprising:
  • step c) obtaining a liquid comprising treated wastewater and dispersed nongranular sludge that is essentially free of granular sludge; d) supplying at least part of the liquid obtained in step c) to a device for removal and/or inactivation of sludge and removing or inactivating at least part of the non-granular sludge to obtain a liquid depleted in active sludge; and
  • reactor vessel or, in case the device for removal and/or inactivation of sludge is located in the reactor vessel, maintaining at least part of the liquid depleted in active sludge in the reactor vessel.
  • An important advantage of the present invention is that the contact time of wastewater with active sludge is increased, whilst the formation of non-granular sludge is minimised.
  • a high load of dense granular sludge can be maintained in the reactor vessel, resulting in a high volumetric biological conversion rate (g COD/ m 3 reactor/day) of the process.
  • the increased contact time of wastewater with active sludge is preferably achieved by means of an effluent recycle.
  • Recycles of effluent are known in the art, in particular for maintaining a sufficient high upflow velocity.
  • effluent recycles known in the art, however, effluent comprising non-granular sludge is recycled.
  • the present inventors have, however, realised that recycling too much non-granular active sludge with the effluent will result in a diminished selection pressure for granular sludge and an undesired increase of bulky non-granular sludge.
  • granular sludge formation is favoured over non-granular sludge formation.
  • the present process may result in some costs for sludge disposal in early stages of the process, the process will finally reach a stage wherein minimal non-granular sludge is formed due to a favourable selection pressure for granular sludge.
  • Figure 1 is schematically shown a process according to the invention wherein non-granular sludge is separated from liquid reactor effluent.
  • Figure 2 is schematically shown a process according to the invention wherein non-granular sludge in the reactor effluent is inactivated.
  • the process according to the invention is a process for anaerobic wastewater treatment wherein granular and non-granular sludge are formed.
  • the process is thus carried out under sludge granulation conditions.
  • Such process conditions are known in the art.
  • the process may be any anaerobic wastewater treatment process of which it is known in the art that sludge granulation may take place.
  • the process may be a process wherein organic material (expressed as COD) is converted into methane.
  • the process may be a process wherein organic material is converted into one or more carboxylic acids, such as for example acetic acid and/or lactic acid.
  • the anaerobic wastewater treatment process according to the invention may be carried out in any suitable reactor, preferably in an UASB reactor or an EGSB reactor, more preferably in an UASB reactor.
  • a wastewater influent is supplied to a reactor vessel containing granular active sludge in step a).
  • the wastewater influent is supplied to a reactor vessel that already contains active granular sludge. It will be appreciated that during start-up of the process, the reactor vessel may not yet contain active granular sludge. Since the process is operated under conditions where sludge granulation takes place, granular sludge will be formed and contained in the vessel once the process is on stream. Under sludge granulation conditions, typically also some non-granular sludge will be formed.
  • the wastewater influent may be any suitable wastewater influent, for example industrial, agricultural or municipal wastewater.
  • step b the wastewater influent is subjected, in the reactor vessel, to anaerobic treatment conditions. Under these conditions, organic material in the wastewater influent will be converted into for example methane or carboxylic acids. It will be appreciated that the type of conversion will inter alia depend on the microorganisms present in the granular sludge and the reaction conditions applied. Microorganisms involved in each type of conversion and reaction conditions for each conversion are known in the art. Suitable conditions known in the art may be applied in step b).
  • a liquid comprising treated wastewater and dispersed non-granular sludge and essentially no granular sludge is obtained.
  • such liquid is obtained in the upper part of the reactor vessel.
  • the reactor vessel preferably comprises a three phase separator in the upper part of the vessel that separates any gas and solid granular sludge from the treated wastewater.
  • step d) at least part of the liquid obtained in step c) is supplied to a device for removal and/or inactivation of sludge to obtain a liquid depleted in active sludge.
  • the device for removal and/or inactivation of sludge may be located inside or outside the reactor vessel, preferably outside the reactor vessel.
  • a liquid comprising treated wastewater and dispersed non-granular sludge and essentially no granular sludge stream is discharged from the reactor vessel and supplied to the device for removal and/or inactivation of sludge.
  • Discharging liquid effluent from the reactor vessel without discharging granular sludge with the effluent is typically done by discharging liquid effluent at or near the top of the reactor vessel.
  • the wastewater influent is supplied at or near the bottom of the reactor vessel and liquid effluent is discharged at or near the top of the reactor vessel.
  • granular sludge will typically stay in the reactor vessel, since it has a settling velocity that far exceeds typically influent velocities for upflow wastewater treatment processes.
  • a separator that separates solids from the treated wastewater may be placed in the reactor vessel just upstream of any outlet for liquid effluent.
  • the reactor vessel comprises a three phase separator near the top of the reactor that separates any gas and solid granular sludge from the treated wastewater before discharge of treated wastewater from the reactor vessel.
  • An inclined plate settler In a reactor that is not operated in upflow mode, a settler will typically be needed in order to avoid the presence of granular sludge in liquid reactor effluent.
  • An inclined plate settler may suitably be used.
  • An inclined plate settler comprises a multitude of parallel inclined plates between which a liquid is flowed upwardly. The granular solids in the liquid are allowed to settle on the inclined, parallel plates.
  • Such settler is preferably placed in the reactor vessel just upstream of any outlet(s) for reactor effluent.
  • the device for removal and/or inactivation of sludge may be located inside the reactor vessel, for example in the upper part of the reactor vessel where a liquid comprising treated wastewater and dispersed non-granular sludge and essentially no granular sludge is typically present.
  • a liquid comprising treated wastewater and dispersed non-granular sludge and essentially no granular sludge is typically present.
  • the device is located in the reactor vessel, at least part of the liquid depleted in active sludge is maintained in the reactor vessel.
  • Reference to a liquid essentially free of granular sludge is to a liquid that comprises less than 1 vol % of granular sludge, preferably less than 0.5 vol %, more preferably less than 0.1 vol %, even more preferably is free of any granular sludge, based on the total volume of the liquid.
  • liquid in the reactor vessel and liquid effluent discharged from the reactor vessel will typically comprise non-granular sludge. If a settler is used to separate granular sludge from the reactor liquid, the settler is operated such that non- granular sludge is retained in the liquid. In an inclined plate settler this is for example done by controlling the upflow velocity in the settler.
  • step d) at least part of the non-granular sludge in the liquid obtained in step c) is removed from the liquid or inactivated.
  • this may be done by any means for solid/liquid separation known in the art, for example by means of filtration and/or sedimentation.
  • the non-granular sludge removed from the liquid in such solid/liquid separator is subsequently withdrawn from the process in order to keep the retention time of non-granular sludge low.
  • the liquid depleted in active sludge thus obtained is at least partly recycled to the reactor vessel or, in case of an separation device located in the reactor vessel, maintained in the in the vessel, as described herein below.
  • Inactivation of active non-granular sludge may be done by any means known to be suitable for inactivation of micro-organisms such as for example thermal, mechanical, chemical or electrical inactivation or inactivation by means of
  • electromagnetic radiation such as UV treatment, microwave treatment or sonification, for example ultrasound sonification.
  • the device is a separator that separates non-granular sludge from the liquid to obtain a liquid depleted in sludge (sludge-depleted liquid) and a fraction enriched in sludge.
  • the fraction enriched in sludge is withdrawn from the process.
  • Separators suitable for separating dispersed solids from a liquid are known in the art and any suitable separators known in the may be used.
  • the separator may for example be a filtration device, such as an ultrafiltration, microfiltration or nanofiltration device, or a settler. More preferably, the separator is a settler such as for example an inclined plate settler.
  • the device is a device for inactivating sludge, for example a heating device, a device for applying a pulsed electrical field over the liquid obtained in step c), an UV disinfection device, or a device for producing high power ultrasound.
  • the device is inactivating sludge by applying a pulsed electrical field over the liquid.
  • the liquid depleted in active sludge that is obtained in step d) is at least partly recycled to the reactor vessel or, in case the sludge removal/inactivation device is located in the reactor vessel, maintained in the reactor vessel in step e).
  • inactivated sludge may be kept in the liquid recycled to or maintained in the reactor vessel.
  • the process has a dilution rate (in h "1 ) which is defined as the quotient of the sum of the flow of wastewater influent and any liquid depleted in active sludge recycled in step e) (in m 3 /h) and liquid volume in the reactor vessel (in m 3 ).
  • the dilution rate is larger than the maximum specific growth rate of any non-granular sludge formed in the process. Under these conditions, formation of granular sludge is favoured over the formation of non-granular sludge.
  • the process according to the invention is particularly suitable for anaerobic conversion of COD into methane in wastewater streams with a relatively high
  • Chemical Oxygen Demand preferably a COD of at least 20 g/1, more preferably in the range of from 20 to 200 g/1, even more preferably in the range of from 25 to 100 g/1, still more preferably of from 30 to 80 g/1.
  • the dilution rate is preferably in the range of from 0.033 to 2.0 h "1
  • the dilution rate is preferably in the range of from 0.2 to 20 h "1 (equivalent to a hydraulic retention time in the range of from 0.05 to 5 h), more preferably of from 0.33 to 10 h "1 (equivalent to a hydraulic retention time in the range of from 0.1 to 3 h).
  • the process conditions can be controlled such that the dilution rate exceeds the maximum specific growth rate of the non-granular sludge.
  • the amount of active sludge that needs to be removed or inactivated in order to control the dilution rate of the hydraulic retention time will inter alia depend on the COD concentration in the wastewater influent and the reactor volume.
  • step d) at least part of the liquid obtained in step c) is supplied to the device for removing or inactivating sludge. Given the influent flow and COD concentration of the wastewater to be treated, it will inter alia depend on the desired minimum dilution rate how much liquid depleted in active sludge needs to be recycled or maintained in the reactor vessel.
  • step d) is a separator
  • a liquid depleted in active sludge and a fraction enriched in sludge is obtained.
  • the liquid depleted in active sludge may be entirely or partly recycled to or maintained in the reactor vessel.
  • Part of the liquid depleted in active sludge may be recovered as treated wastewater, optionally after a further treatment step, for example an aerobic treatment step.
  • treated waste water is recovered from the fraction enriched in sludge.
  • This fraction typically is a liquid phase comprising non-granular sludge.
  • the concentration of sludge in this fraction may be low, for example below 1 wt% or even below 0.1 wt%, since the process conditions in dilution rate in the reactor vessel are unfavourable for non-granular sludge formation.
  • Treated wastewater is preferably recovered from the fraction enriched in sludge, optionally after a further treatment step, for example an aerobic treatment step.
  • treated wastewater may be recovered from the liquid depleted in active sludge, optionally after a further treatment step, for example an aerobic treatment step.
  • treated wastewater may be recovered from a part of the liquid comprising treated wastewater and dispersed non-granular sludge obtained in step c) that is not supplied to the device for removal and/or inactivation of sludge.
  • such liquid is first subjected to one or more further treatment steps, for example an aerobic treatment step, before recovering treated wastewater from it.
  • FIG. 1 a process according to the invention wherein a wastewater influent is supplied to reactor vessel 1 via line 2.
  • Reactor vessel 1 is a UASB reactor comprising a bed of granular sludge (not shown). The influent is supplied to the vessel 1 below the granular sludge bed. The wastewater is treated in vessel 1.
  • Vessel 1 comprises a three-phase separator 3 in which gas and solid granular sludge are separated from the treated wastewater before treated wastewater is discharged as liquid effluent via line 4.
  • Liquid effluent discharged via line 4 is supplied to settler 5 to separate any non-granular sludge from the liquid. Liquid depleted in sludge is recycled to vessel 1 via line 7.
  • a fraction enriched in non-granular sludge is discharged from the process via line 8.
  • part of the liquid effluent discharged from vessel 1 may be directly recycled to vessel 1 (indicated by dotted line 9).
  • Treated wastewater is recovered from the fraction enriched in non-granular sludge that is discharged via line 8 after a further aerobic treatment step (not shown).
  • FIG. 2 is shown a second embodiment of the process according to the invention.
  • liquid effluent discharged via line 4 is supplied to sludge inactivation device 10 wherein a pulsed electrical field is applied over the liquid effluent.
  • sludge inactivation device 10 wherein a pulsed electrical field is applied over the liquid effluent.
  • a liquid comprising inactivated sludge is obtained. Part of this liquid is recycled to vessel 1 via line 7.
  • Treated wastewater is recovered from the part of the liquid comprising inactivated sludge that is withdrawn via line 11.

Landscapes

  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

L'invention concerne un processus d'épuration anaérobie des eaux usées, des boues granuleuses et non granuleuses étant formées. Le processus comprend les opérations consistant à : a) alimenter une cuve de réacteur contenant de la boue granulaire active en affluent d'eaux usées contenant de la DCO ; b) soumettre l'affluent d'eaux usées dans la cuve du réacteur aux conditions d'épuration anaérobie ; c) obtenir un liquide comprenant des eaux usées traitées et des boues non granuleuses dispersées, qui sont essentiellement exemptes de boues granuleuses ; d) fournir au moins une partie du liquide obtenu à l'étape c) à un dispositif d'élimination et/ou d'inactivation des boues et éliminer ou inactiver au moins une partie des boues non granuleuses pour obtenir un liquide appauvri en boues actives ; et e) recycler au moins une partie du liquide appauvri en boues actives vers la cuve du réacteur ou, dans le cas où le dispositif d'élimination et/ou d'inactivation des boues se trouve dans la cuve du réacteur, conserver au moins une partie du liquide appauvri en boues actives dans la cuve du réacteur.
PCT/NL2014/050266 2013-05-03 2014-04-24 Processus d'épuration anaérobie des eaux usées WO2014178711A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP13166355.1 2013-05-03
EP13166355 2013-05-03

Publications (1)

Publication Number Publication Date
WO2014178711A1 true WO2014178711A1 (fr) 2014-11-06

Family

ID=48190409

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/NL2014/050266 WO2014178711A1 (fr) 2013-05-03 2014-04-24 Processus d'épuration anaérobie des eaux usées

Country Status (1)

Country Link
WO (1) WO2014178711A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109231444A (zh) * 2018-09-27 2019-01-18 华南师范大学 一种钙化厌氧颗粒污泥二次成核再利用方法及系统
US10196594B2 (en) 2014-11-20 2019-02-05 Gea Brewery Systems Gmbh Device and method for extracting aroma substances from vegetable aroma carriers into a brewing liquid
CN109368934A (zh) * 2018-09-30 2019-02-22 环境保护部南京环境科学研究所 一种废水自养反硝化脱氮装置及废水处理方法
US20210331958A1 (en) * 2018-08-22 2021-10-28 Veolia Water Solutions & Techologies Support Granular sludge reactor system comprising an external separator

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005115930A1 (fr) * 2004-05-26 2005-12-08 National Research Council Of Canada Couplage bioelectrolytique methanogene/methanotrophique destine a la biorestauration des eaux souterraines
JP2009178628A (ja) * 2008-01-29 2009-08-13 Ihi Corp 嫌気性廃水処理装置
DE202009017869U1 (de) * 2009-04-29 2010-09-23 Envirochemie Gmbh Vorrichtung zum Trennen von gasförmigen, flüssigen und festen Stoffen in einem Bioreaktor
US20110036771A1 (en) * 2007-01-09 2011-02-17 Steven Woodard Ballasted anaerobic system and method for treating wastewater
WO2012101894A1 (fr) * 2011-01-24 2012-08-02 株式会社明電舎 Dispositif de traitement des déchets liquides et procédé associé

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005115930A1 (fr) * 2004-05-26 2005-12-08 National Research Council Of Canada Couplage bioelectrolytique methanogene/methanotrophique destine a la biorestauration des eaux souterraines
US20110036771A1 (en) * 2007-01-09 2011-02-17 Steven Woodard Ballasted anaerobic system and method for treating wastewater
JP2009178628A (ja) * 2008-01-29 2009-08-13 Ihi Corp 嫌気性廃水処理装置
DE202009017869U1 (de) * 2009-04-29 2010-09-23 Envirochemie Gmbh Vorrichtung zum Trennen von gasförmigen, flüssigen und festen Stoffen in einem Bioreaktor
WO2012101894A1 (fr) * 2011-01-24 2012-08-02 株式会社明電舎 Dispositif de traitement des déchets liquides et procédé associé

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
L. W. HULSHOFF PO ET AL., WATER RESEARCH, vol. 38, 2004, pages 1376 - 1389
L. W. HULSHOFF POL ET AL., WATER RESEARCH, vol. 38, 2004, pages 1376 - 1389

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10196594B2 (en) 2014-11-20 2019-02-05 Gea Brewery Systems Gmbh Device and method for extracting aroma substances from vegetable aroma carriers into a brewing liquid
US20210331958A1 (en) * 2018-08-22 2021-10-28 Veolia Water Solutions & Techologies Support Granular sludge reactor system comprising an external separator
US11613483B2 (en) * 2018-08-22 2023-03-28 Veolia Water Solutions & Technologies Support Granular sludge reactor system comprising an external separator
CN109231444A (zh) * 2018-09-27 2019-01-18 华南师范大学 一种钙化厌氧颗粒污泥二次成核再利用方法及系统
CN109231444B (zh) * 2018-09-27 2021-10-01 华南师范大学 一种钙化厌氧颗粒污泥二次成核再利用方法及系统
CN109368934A (zh) * 2018-09-30 2019-02-22 环境保护部南京环境科学研究所 一种废水自养反硝化脱氮装置及废水处理方法
CN109368934B (zh) * 2018-09-30 2024-04-05 环境保护部南京环境科学研究所 一种废水自养反硝化脱氮装置及废水处理方法

Similar Documents

Publication Publication Date Title
EP3392208B1 (fr) Bioréacteur de traitement des eaux usées, système de traitement des eaux usées le comprenant et procédé de traitement des eaux usées
JP6563333B2 (ja) ハイブリッド汚水処理
JP6009362B2 (ja) 排水処理方法
Hassan et al. Development of anaerobic reactor for industrial wastewater treatment: an overview, present stage and future prospects
AU2014254527B2 (en) Process for biological removal of nitrogen from wastewater
CN109311714B (zh) 组合再生式消化与接触罐和溶气浮选的方法
US11180392B2 (en) Sequencing batch reactor for sewage treatment and sewage treatment system comprising same
JP7343518B2 (ja) 同時フェーズ動作型嫌気性連続バッチ反応器
CA2796247A1 (fr) Bioreacteur a membrane anaerobie pour traiter un courant de dechets
EP3265215B1 (fr) Systèmes et procédés pour le traitement d'eau résiduaire diluée
JP5963668B2 (ja) 排水処理方法
US6146532A (en) Process for the biological purification of wastewater
WO2014178711A1 (fr) Processus d'épuration anaérobie des eaux usées
CN104470859A (zh) 使用污泥脱气和污泥回收以及处理设备的厌氧污水处理
JP6626888B2 (ja) 廃水の清澄化方法
JP4571065B2 (ja) 粒状微生物汚泥生成方法及び粒状微生物汚泥生成装置
KR20160040132A (ko) 폐수 처리 방법 및 시스템
CN105948412A (zh) Fbr-uasb-a/obr处理工业废水的组合工艺
JP6474301B2 (ja) 脱水処理方法、排水処理方法及び排水処理装置
JP6437794B2 (ja) 排水処理装置及び排水処理方法
KR102131735B1 (ko) 하수 처리용 컴팩트형 포기조 및 이를 포함하는 하수 처리 시스템
KR20060019643A (ko) 유기물 처리를 위한 고율 혐기성 소화조의 개선
EP2199261A1 (fr) Nouveau procédé d'épuration des eaux usées et son procédé d'utilisation
CN212655638U (zh) 一种发酵废水处理中水回用除菌装置
US20240190738A1 (en) Method and system for continuous-flow aerobic granular sludge process with improved two-stage sedimentation

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 14721560

Country of ref document: EP

Kind code of ref document: A1

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 14721560

Country of ref document: EP

Kind code of ref document: A1