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WO2008027259A2 - procédés et systèmes de traitement biologique d'eaux usées de désulfuration de gaz brûlé - Google Patents

procédés et systèmes de traitement biologique d'eaux usées de désulfuration de gaz brûlé Download PDF

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Publication number
WO2008027259A2
WO2008027259A2 PCT/US2007/018552 US2007018552W WO2008027259A2 WO 2008027259 A2 WO2008027259 A2 WO 2008027259A2 US 2007018552 W US2007018552 W US 2007018552W WO 2008027259 A2 WO2008027259 A2 WO 2008027259A2
Authority
WO
WIPO (PCT)
Prior art keywords
wastewater
reactor
fgd
introducing
flue gas
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/US2007/018552
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English (en)
Other versions
WO2008027259A3 (fr
Inventor
Robert F. Kelly
Michael Pudvay
Antonio Lau
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.)
Veolia Water Technologies Treatment Solutions USA Inc
Original Assignee
Infilco Degremont Inc
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 Infilco Degremont Inc filed Critical Infilco Degremont Inc
Priority to EP07811473A priority Critical patent/EP2054350A2/fr
Priority to CA 2661739 priority patent/CA2661739A1/fr
Publication of WO2008027259A2 publication Critical patent/WO2008027259A2/fr
Anticipated expiration legal-status Critical
Publication of WO2008027259A3 publication Critical patent/WO2008027259A3/fr
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/84—Biological processes
    • 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
    • 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
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
    • 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
    • C02F2101/101—Sulfur compounds
    • 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
    • C02F2101/20—Heavy metals or heavy metal compounds
    • 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
    • C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
    • 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
    • C02F2209/04—Oxidation reduction potential [ORP]
    • 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
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Definitions

  • This disclosure relates to wastewater treatment methods and systems that remove organic and inorganic pollutants captured in the purge stream from air pollution control equipment.
  • Flue Gas Desulfurization (FGD) process wastewater contains elevated levels of chlorides; significant concentrations of heavy metal contaminants such as chromium, mercury, and selenium; often high levels of nitrates; and a very high solids content that consists primarily of calcium sulfate, calcium carbonate, magnesium hydroxide, and fly ash.
  • FGD wastewater contains elevated levels of chlorides; significant concentrations of heavy metal contaminants such as chromium, mercury, and selenium; often high levels of nitrates; and a very high solids content that consists primarily of calcium sulfate, calcium carbonate, magnesium hydroxide, and fly ash.
  • Treatment of FGD wastewater is a significant need for utility operations. Physical / chemical treatment processes are typically used for neutralization and calcium sulfate desaturation, removal of some heavy metals, clarification and sludge thickening.
  • conventional chemical precipitation techniques do not reliably eliminate heavy metal contaminants such as selenium and hexavalent chromium below outfall discharge
  • FGD process wastewater is the focus of increasingly stringent effluent requirements, with outfall discharge standards (monthly average and daily maximum) typically established for:
  • Heavy Metals including but not limited to Arsenic, Chromium, Copper, Mercury & Selenium
  • Selenium is an essential micronutrient for animals and bacteria. However, it becomes highly toxic when present above minute concentrations.
  • the oxidized species of selenium, selenate (Se Vl) and selenite (Se IV) are highly soluble and bioavailable, whereas reduced forms are insoluble and much less bioavailable.
  • Regulatory limits for soluble selenium remain variable with targets ranging from 800 ug/L down to the U.S. national drinking water standard of 50 ug/L, frequently depending upon the discharge receiving water body.
  • Selenium exists in multiple valence states in the natural environment and the impact of selenium speciation on treatment efficiency is known.
  • Selenium in the form of Selenite (Se IV; SeO 3 ) can be removed with 65 to 85% efficiency using physical-chemical treatment approaches while Selenate (Se Vl; SeO 4 ) removal efficiency is limited to ⁇ 10% with physical- chemical treatment.
  • a method of treating flue gas and wastewater generated by treating the flue gas includes: introducing the flue gas and an organic acid conditioning agent into a wet-oxidation scrubber/absorber substantially to remove sulfur dioxide from the flue gas and condition resulting FGD wastewater for downstream biological treatment; introducing FGD scrubber wastewater generated by the absorber into an anoxic biological reactor to substantially denitrify and/or reduce selected heavy metals in the FGD scrubber wastewater; and introducing substantially denitrified wastewater into an anaerobic biological reactor to substantially reduce the amount of sulfate and/or selected heavy metals in the FGD scrubber wastewater.
  • a system for treating flue gas and wastewater generated by treating the flue gas includes: a wet-oxidation scrubber/absorber comprising a flue gas inlet, a flue gas treatment fluid inlet, an organic acid conditioning agent inlet, and a wastewater outlet; an anoxic reactor located downstream of the wet-oxidation scrubber/absorber to substantially denitrify FGD scrubber wastewater generated by the absorber; and an anaerobic reactor located downstream of the anoxic reactor to substantially reduce the amount of sulfate and/or selected heavy metals in the FGD scrubber wastewater.
  • a method of treating FGD scrubber wastewater includes: introducing FGD scrubber wastewater generated by combining flue gas and an organic acid conditioning agent in a wet-oxidation scrubber/absorber into an anoxic reactor to substantially denitrify the FGD scrubber wastewater; and introducing substantially denitrified wastewater into an anaerobic reactor to reduce the amount of sulfate and/or selected heavy metals in the FGD scrubber wastewater.
  • a system for treating FGD scrubber wastewater includes: an anoxic biological reactor located downstream of a wet- oxidation scrubber/absorber to substantially denitrify FGD scrubber wastewater generated by the absorber; and an anaerobic biological reactor located downstream of the anoxic reactor to substantially reduce the amount of sulfate and/or selected heavy metals in the FGD scrubber wastewater.
  • FIG. 1 is a schematic diagram of a representative process flow for a wet-oxidation scrubber/absorber system and associated conventional FGD wastewater treatment system.
  • FIG. 2 is a schematic flow diagram of a representative biological treatment system for FGD scrubber wastewater.
  • This disclosure relates to biological treatment systems for FGD scrubber wastewater, encompassing the feed of a pure organic acid conditioning reagent, such as formic acid, to the wet-oxidation scrubber / absorber and later followed by a combination of anoxic, anaerobic and aerobic staged activated sludge reactors and associated clarification systems for removal of TN 1 reduction and precipitation of heavy metals and elimination of suspended solids from the FGD purge stream.
  • a pure organic acid conditioning reagent such as formic acid
  • This disclosure also relates to processes for biological treatment of
  • FGD scrubber wastewater particularly to treatments that improve the removal efficiency of TN and heavy metals including but not limited to selenium.
  • the treatment system 10 includes a line 12 to add a pure organic acid conditioning reagent, such as formic acid, to absorber 14 as indicated in Fig. 1.
  • a pure organic acid conditioning reagent such as formic acid
  • the absorber 14 also connects to a particle scrubber 16 and a recirculation tank 18.
  • the recirculation tank 18 directly receives flue gas treatment fluid through supply line 20 which is indirectly supplied into absorber
  • Flue gas treatment fluid may comprise, among other things, a lime/limestone water slurry.
  • FGD scrubber wastewater exits absorber 14 through line 32 and enters recirculation tank 18. Selected portions of FGD scrubber wastewater exit through recirculation tank 18 and may proceed to clarifier 34. This may be followed by passage of the clarified wastewater to holding tank 36. Wastewater contained in holding tank 36 can be recycled to recirculation tank 18 by way of line 38. The partially dewatered sludge may be channeled from clarifier 34 to vacuum filter 40 by way of line 42, where most of the remaining water is removed. The waste sludge can then be sent to a settling pond or landfill 44.
  • FGD scrubber wastewater may also flow from clarifier 34 to additional treatment systems such as a biological treatment system of Fig. 2 by way of line 46 and as activated by valve 47.
  • FIG. 2 a selected, representative biological treatment system 48 for FGD scrubber wastewater is shown in a schematic form.
  • the system 48 includes an inlet 50, a staged suspended growth biological reactor 52 comprising anoxic 54 and anaerobic 56 zones, an intermediate clarifier 58, an aerobic suspended growth biological reactor 60, a final clarifier 62, a storage tank 64 and a filtration stage 76.
  • the biological treatment system 48 of Fig. 2 can perform the following functions:
  • the biological treatment system 48 may receive influent feed from an upstream physical-chemical treatment system such as from clarifier 34, for example, of Fig. 1 , in the form of deoxygenated FGD purge wastewater.
  • the biological reactors of the system 48 may include completely mixed, continuous flow, activated sludge reactors.
  • the first cell (or reactor 54) in the system 48 is the anoxic stage, where nitrates are reduced to nitrogen gas via denitrification reactions.
  • FGD wastewater is deficient in macronutrients, including ammonia nitrogen and orthophosphorous, as well as many of the micronutrients required to support biological growth, there is a process requirement for supplemental nutrient addition to yield efficient treatment performance.
  • Reactor 54 is thus fed with a biodegradable nutrient blend, containing macro- and micronutrients to maintain microbial growth.
  • Nutrients include but are not limited to supplemental carbon such as waste sugar, corn syrup, molasses or the like, urea or the like to provide ammonia nitrogen, phosphoric acid, micronutrients and yeast extract to provide necessary trace metals and growth factors. Fermentation of sugars dosed into the anoxic reactor 54 results in the conversion of sucrose to volatile fatty acids (VFAs) that sulfate / selenium reducing microorganisms are capable of metabolizing efficiently in the downstream anaerobic reactor stage(s). Additional carbon sources such as lactate, acetate or the like may also be added directly to the anoxic/anaerobic reactors to enhance selenium removal by enriching the selenium reducing microorganisms.
  • VFAs volatile fatty acids
  • Additional carbon sources such as lactate, acetate or the like may also be added directly to the anoxic/anaerobic reactors to enhance selenium removal by enriching the selenium reducing microorganisms.
  • a pure organic acid stream such as formic acid
  • line 12 of absorber 14 provides a means to introduce a biodegradeable carbon substrate to the wastewater that can provide COD to the system for downstream biological removal of nitrates and selected heavy metals.
  • a dosage of 200 mg/L formate equates to a theoretical COD dosage of about 70 mg/L.
  • the anoxic / anaerobic biological reactor 52 may be an overflow, under-flow weir design which mimics a plug-flow system without the need to incorporate separate reactor tanks that are physically isolated from one another. Other configurations / structures may be used as appropriate.
  • Operational inputs for successful treatment involve targeting the appropriate oxidation-reduction potential (ORP) in the various reactor stages.
  • ORP oxidation-reduction potential
  • the anoxic reactor 54 may preferably be maintained in the range of about -50 to about -300 mV to yield efficient denitrification.
  • the role of the anoxic denitrification reactor 54 is important. We found that efficient removal of selected heavy metals such as selenium substantially depends upon sequential substrate removal, specifically the prior elimination of nitrates.
  • organo- selenium complexes were found to be surprisingly recalcitrant to selenium reduction by the microbial population in downstream biological reactors.
  • use of a pure organic acid reagent, such as formic acid, to improve SO 2 removal efficiency at the scrubber further provides downstream advantages by yielding a wastewater matrix that could readily be treated for selenium removal.
  • the staged biological reactors create a reducing environment for the conversion of selenate or selenite to elemental selenium, which precipitates out of solution into the wastewater solids.
  • the partially treated FGD wastewater leaves the anoxic reactor 54 substantially devoid of nitrate contamination and flows into the next cell (i.e., the anaerobic reactor 56), which in one aspect may be operated at an ORP in the range of about -200 to about -500 mV, where sulfate and heavy metal- reducing organisms begin to remove sulfates and the selected heavy metals from the wastewater.
  • the treated water then flows to an optional third cell (anaerobic reactor stage) to ensure that heavy metals are removed to levels allowing outfall discharge permits to be met.
  • the treated effluent from the anoxic / anaerobic biological reactors 54 / 56 may flow into a mix chamber allowing for chemical addition to improve downstream sedimentation within the intermediate clarifier 58. From the mix chamber of the anoxic / anaerobic reactors 54 / 56, the treated effluent flows into a settling type intermediate clarifier 58, where TSS is settled out and the clarifier underflow solids are recycled to the anoxic reactor 54 by lines 66 and 68 as return activated sludge (RAS) or sent to a sludge holding tank (not shown) by line 70 as waste activated sludge (WAS).
  • RAS return activated sludge
  • WAS waste activated sludge
  • the partially treated FGD wastewater flows into the aerobic biological reactor 60 for removal of BOD and ammonia.
  • the aerobic biological reactor 60 includes operation at positive ORP.
  • the FGD wastewater flows into a settling type final clarifier 62, where TSS is settled out and clarifier underflow solids may be recycled to the head of the aerobic reactor 62 by lines 72 and 74 as return activated sludge (RAS) or sent to a sludge holding tank (not shown) by line 70 as waste activated sludge (WAS).
  • RAS return activated sludge
  • WAS waste activated sludge
  • the clarified water flows into a wet effluent well / tank 64 for pumping to pressure filters 76 and ultimately discharge to the environment.
  • the filters may be gravity sand, multimedia or the like type filters.
  • Powdered Activated Carbon (PAC) or other adsorbent materials such as charred poultry waste or the like added to the anaerobic and/or aerobic biological reactor will also adsorb any remaining organo-selenium complexes to assist reaching a final effluent selenium concentration that is below about 200 ⁇ g/L.
  • PAC can be added at a dosage of about 550 ppm, for example.
  • a biological treatment system comprising of a 2-stage, completely mixed, anaerobic activated sludge reactor having a total reactor volume of approximately 2,000 gallons followed by a 500-gallon clarifier and an aerobic activated sludge reactor and final clarifier was fabricated and installed on a sidestream of FGD scrubber blowdown at an operating power generating station.
  • the facility initiated pure organic acid addition in the form of formic acid to the absorber to enhance the downstream biological treatment process while continuing to provide SO 2 removal at the wet-oxidation scrubber/absorber.
  • the use of a pure organic acid feed resulted in significant reductions in the levels of complexed selenium present. Subsequently, this resulted in improved treatability of the FGD wastewater with the performance of the biological treatment system greatly enhanced as noted below.
  • staged activated sludge design was found to yield substantially complete denitrification of influent FGD scrubber wastewater under anoxic conditions, consistently achieving effluent NO 3 -N concentrations below 1 mg/L for influent nitrate levels ranging from 200 to 600 mg/L.
  • the aerobic reactor performance was found to be much less sensitive to changes in the influent soluble selenium concentration allowing for quick adaptation to system upsets that result in rapid increase in influent Se levels.
  • the complexity of Selenium speciation within FGD scrubber wastewaters may be reduced or eliminated by feeding a pure organic acid conditioning additive, such as formic acid, to the wet-oxidation scrubber/absorber. Subsequently, this approach improves downstream biological treatment while maintaining SO 2 removal efficiency at the absorber.
  • a pure organic acid conditioning additive such as formic acid
  • Reactors are seeded with biomass from natural microbial populations avoiding the need to regularly add "specialized" microbial cultures and thereby reducing annual operational costs.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Biomedical Technology (AREA)
  • Health & Medical Sciences (AREA)
  • Organic Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Hydrology & Water Resources (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Molecular Biology (AREA)
  • Treating Waste Gases (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

L'invention concerne des systèmes et des procédés de traitement de gaz brûlé et des eaux usées générés par le traitement du gaz brûlé et consistant à injecter le gaz brûlé, un fluide de traitement de gaz brûlé éliminant le dioxyde de soufre du gaz brûlé et un agent de conditionnement d'acide organique dans un laveur de gaz/absorbeur par oxydation humide; injecter les eaux usées laveur de gaz FGD générées par le laveur de gaz/absorbeur par oxydation humide dans un réacteur biologique anoxique pour sensiblement dénitrifier les eaux usées de laveur de gaz FGD; et injecter les eaux usées de laveur de gaz FGD sensiblement dénitrifiées résultantes dans un réacteur biologique anaérobie pour sensiblement réduire la quantité de sulfate et/ou de métaux lourds sélectionnés dans les eaux usées de laveur de gaz FGD.
PCT/US2007/018552 2006-08-25 2007-08-22 procédés et systèmes de traitement biologique d'eaux usées de désulfuration de gaz brûlé Ceased WO2008027259A2 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP07811473A EP2054350A2 (fr) 2006-08-25 2007-08-22 Procédés et systèmes de traitement biologique d'eaux usées de désulfuration de gaz brûlé
CA 2661739 CA2661739A1 (fr) 2006-08-25 2007-08-22 Procedes et systemes de traitement biologique d'eaux usees de desulfuration de gaz brule

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US84008406P 2006-08-25 2006-08-25
US60/840,084 2006-08-25

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WO2008027259A2 true WO2008027259A2 (fr) 2008-03-06
WO2008027259A3 WO2008027259A3 (fr) 2009-07-09

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EP (1) EP2054350A2 (fr)
CA (1) CA2661739A1 (fr)
WO (1) WO2008027259A2 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011097094A1 (fr) * 2010-02-02 2011-08-11 General Electric Company Systèmes de traitement de l'eau grise de gazéification
CN103153879A (zh) * 2010-07-27 2013-06-12 泽农科技合股公司 使用化学氧化和生物还原去除硒
CN103739065A (zh) * 2013-12-04 2014-04-23 吉林省电力科学研究院有限公司 一种火电厂脱硫废水厌氧生物处理方法
CN102811956B (zh) * 2010-02-02 2016-11-30 通用电气公司 气化灰水处理系统

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS59173199A (ja) * 1983-03-22 1984-10-01 Kansai Electric Power Co Inc:The ジチオン酸とアンモニアを含む廃水の生物学的処理方法
JP3068312B2 (ja) * 1992-03-11 2000-07-24 三菱重工業株式会社 排煙脱硫方法
US5308509A (en) * 1993-03-08 1994-05-03 The Babcock & Wilcox Company FGD performance enhancement by hydroclone and recycling steps
CZ292547B6 (cs) * 1995-02-06 2003-10-15 Biostar Development C. V. Způsob čištění spalin obsahujících oxidy dusíku a zařízení pro čištění spalin
JP3658802B2 (ja) * 1995-06-23 2005-06-08 栗田工業株式会社 セレン含有水の処理方法
EP0769479A1 (fr) * 1995-10-18 1997-04-23 N.V. Kema Procédé pour purifier un courant d'eau résiduaire ou similaire
JP2006205097A (ja) * 2005-01-31 2006-08-10 Mitsubishi Heavy Ind Ltd 排水の生物学的処理方法
US7790034B2 (en) * 2005-07-25 2010-09-07 Zenon Technology Partnership Apparatus and method for treating FGD blowdown or similar liquids

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011097094A1 (fr) * 2010-02-02 2011-08-11 General Electric Company Systèmes de traitement de l'eau grise de gazéification
CN102811956A (zh) * 2010-02-02 2012-12-05 通用电气公司 气化灰水处理系统
US8557118B2 (en) 2010-02-02 2013-10-15 General Electric Company Gasification grey water treatment systems
AU2011213205B2 (en) * 2010-02-02 2016-05-12 Air Products And Chemicals, Inc. Gasification grey water treatment systems
CN102811956B (zh) * 2010-02-02 2016-11-30 通用电气公司 气化灰水处理系统
CN103153879A (zh) * 2010-07-27 2013-06-12 泽农科技合股公司 使用化学氧化和生物还原去除硒
EP2598448A4 (fr) * 2010-07-27 2014-01-29 Zenon Technology Partnership Élimination de sélénium utilisant une oxydation chimique et une réduction biologique
CN103739065A (zh) * 2013-12-04 2014-04-23 吉林省电力科学研究院有限公司 一种火电厂脱硫废水厌氧生物处理方法

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Publication number Publication date
CA2661739A1 (fr) 2008-03-06
EP2054350A2 (fr) 2009-05-06
WO2008027259A3 (fr) 2009-07-09

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