WO2021020964A1 - Production d'acides gras à partir d'une fraction de tamis de boues activées à partir d'eaux usées traitées - Google Patents

Production d'acides gras à partir d'une fraction de tamis de boues activées à partir d'eaux usées traitées Download PDF

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Publication number
WO2021020964A1
WO2021020964A1 PCT/NL2020/050472 NL2020050472W WO2021020964A1 WO 2021020964 A1 WO2021020964 A1 WO 2021020964A1 NL 2020050472 W NL2020050472 W NL 2020050472W WO 2021020964 A1 WO2021020964 A1 WO 2021020964A1
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Prior art keywords
filter
fraction
reactor
fluid connection
filter fraction
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PCT/NL2020/050472
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English (en)
Inventor
Alexander Antonius Theodorus Wilhelminus Maria HENDRIKS
Mathijs OOSTERHUIS
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Haskoningdhv Nederland B.V
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Priority to EP20746305.0A priority Critical patent/EP3999653A1/fr
Publication of WO2021020964A1 publication Critical patent/WO2021020964A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
    • C12P7/52—Propionic acid; Butyric acids
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/02—Biological treatment
    • C02F11/04—Anaerobic treatment; Production of methane by such processes
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
    • C12P7/54—Acetic acid
    • 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
    • C02F1/004—Processes for the treatment of water whereby the filtration technique is of importance using large scale industrial sized filters
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/24—Separation of coarse particles, e.g. by using sieves or screens
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2305/00—Use of specific compounds during water treatment
    • C02F2305/06—Nutrients for stimulating the growth of microorganisms

Definitions

  • the invention is in the field of wastewater treatment, in particular to a method of producing short chain volatile fatty acids from a sieve fraction of waste water or activated sludge from treated wastewater, and is applicable to a filter frac tion from any aqueous solution comprising biological and/or organic material.
  • the invention further improves removal of P and/or N in a water treatment installation.
  • the invention is in the field of wastewater treatment.
  • Wastewater treatment typically involves several stages. During primary treatment, heavy solids may settle on the bottom of a basin and light oily materials may accumulate on the surface of the water. Heavy solids and light oils may be removed and the primary-treated wastewater may be subjected to a secondary treatment, wherein dissolved and suspended biological material may be removed. Secondary treatment may typically be performed using microorganisms that convert biological material being present into activated sludge. Typically, secondary treatment may include also the removal of pollutants such as phosphates and nitrates and may be combined with a tertiary treatment to further polish the obtained treated wastewater quality. Sec ondary treatment of wastewater typically involves an anaerobic zone, an anoxic zone, and an aerobic zone, wherein wastewater is contacted with activated sludge.
  • microorganisms present in the sludge effectuate sludge growth, wherein organic matter is converted into sludge.
  • Surplus sludge may be separated from the treated water by settlement and subsequently discharged from the wastewater treatment plant as waste.
  • Recent improve ments however, have managed to use the sludge as a valuable resource .
  • a filter fraction When treating wastewater, or likewise an aqueous solution, typically a filter fraction remains.
  • This filter fraction can be extracted from waste water, or active sludge, using a screen filter, sedimentation, a fine sieve, a sieve drum, a sieve bend or another sieve type.
  • This filter fraction has in most cases a high organic matter content (around 90-95%), usu ally contains a lot of cellulose (> 30% of the organic mat ter) , and is often easy to dehydrate to around 30-40% DS with out using polymers. In waste activated sludge these amounts are much lower or absent. Typically about 10% of the solids may be filtered with a sieve of 0.5 mm.
  • CN 104 862 346 A, CN 104 450 805 A and CN 108 384 816 A are likewise not very rele vant .
  • the present invention therefore relates to an improved method of operating a water treatment system, which overcomes one or more of the above disadvantages, without jeopardizing functionality and advantages.
  • the present invention relates in a first aspect to a method of producing volatile short chain fatty acids (see https / /onlinelbrary , wiley . com/doi /10,1002/9783527803293.
  • chi 0 typically C2-C6 fatty acids, such as C2, C 3 , C4, and C5 fatty acids, comprising obtaining a filter fraction from an aqueous solution comprising biological material, that is material typically being from plant origin, the filter fraction may comprise >20 wt .
  • the dry sol ids comprising >50 wt.% organic material, preferably > 80 wt.%, such as > 90 wt.% (wherein the wt.% is based on the dry solids content) , and likewise the organic material being a source of convertible carbon, acidifying the filter fraction under anaerobic conditions by microorganisms, and by producing fatty acids.
  • Pore-sizes used for filtering are typically >
  • the filter fraction can typically relatively easy be dewatered.
  • the filter fraction has in most cases a high or ganic matter content (around 90-95%), usually contains a lot of cellulose, as well as hemicellulose, and lignin or decay products thereof (> 30% of the organic matter) , fibers, and may be easy to dehydrate to around 30-40% DS without using polymers.
  • the filter fraction is largely or fully inactive.
  • the filter fraction typically has low amounts of nutrients; e.g. a N-content is ⁇ 4%, such as 1-2%, a P-content is ⁇ 1%, such as 0.2-0.3%, based on DS, whereas waste activated sludge has about 6%N and 2-3%P, and is also for that reason qualified as being active) .
  • the filter fraction is typically difficult to degrade, such as by digestion of microorganisms. It is found that by increasing the amount of available fatty acids, the amount of biological P removal can also be increased; also the denitrification rate is increased and thereby the required purification volume reduced.
  • the amount of filter fraction in the reactor may be varied, also in this respect, between 0.5-50 grams dry solids/1, preferably between 1-30 grams dry solids/1, more preferably between 2-20 grams dry solids/1, such as between preferably between 3-10 grams dry solids/1. It is found that under such conditions the organic material is converted into fatty acids as much as possible. Typically mainly acetate and propionate are produced, such as 30-70% acetate and 20-60% propionate, preferably 40-60% acetate and 30-40% propionate, based on a total amount of fatty acids.
  • the fatty acids pro quizd can be used for improvement of biological P removal on a wastewater treatment plant (WWTP) with bio-P configuration, acceleration of denitrification in a WWTP is achieved, and production of bioplastics (PHA) is made possible, typically elsewhere.
  • WWTP wastewater treatment plant
  • PHA bioplastics
  • the use of the fatty acids for the P and N removal is attractive because it can save on process additives, such as iron chloride or C-source.
  • the total sludge production may decrease due to the present method.
  • the organic biological material often originates from cel lulose or residues thereof, and often 50-80 wt . % of the or ganic material originates therefrom.
  • Separation of the fatty acids and unconverted filter frac tion may be done with the help of a sieve or cloth filter. It may in addition, or as alternative, also be done selectively, leaving a remaining filter fraction or part thereof in the re actor or the like, or by operating under suitable conditions, such as in a sequence batch reactor, or combinations thereof. Separated residual filter material may be dewatered, such as with a screw press, and taken to a final or further processor. Mixing this residual filter material with the other sludge is also an option. The effluent from the acidification reactor can also be recycled in its entirety to the WWTP without sepa ration of fatty acids and residual (unconverted) filter frac tion .
  • the pH may be regulated, such as by diluting the filter ma terial with rejection water from the sludge dewatering. This rejection water is found to have a relatively large amount of ammonium and phosphate which provide a buffering effect.
  • a base may be dosed, such as lime pellets, which may be obtained from drinking water companies.
  • washing of the filter fraction material, whereby sulphate is removed may be consid ered as a pre-purification step.
  • the temperature in the reactor may be variable and may vary with the ambient temperature. Heating the reactor is not a de sired option, because it costs too much energy. If residual heat is available, the reactor could be operated at a higher temperature; in that case the residence time may need to be shorter to prevent methane formation.
  • the present method provides for a conversion to fatty acids of 30-60% (based on carbon conversion/available carbon) , typi cally 35-45% conversion.
  • level of P in the effluent could be lowered to 0.1-2 mgP/1 by addition of fatty acids such as to 0.2-0.5 mgP/1.
  • the denitrification is accelerated, typically 10-20% accelerated (measured in time/time) , thereby increasing a ca pacity of a WWTP.
  • iron (III) chloride is reduced or even no longer required (which may be as much as 300 ton/y/plant) .
  • a sludge production is slightly decreased (some 3%), the amount of remaining filter fraction is reduced by 40-50%, and as a consequence about 80 tons of carbon dioxide are not emit ted into the atmosphere. Further expensive investments in a sand filter can be prevented, at the cost of a five times cheaper fatty acid reactor. It is therefore considered that a return on investment is about 7 years.
  • the present invention relates in a first aspect to a method according to claim 1.
  • the filter fraction may be obtained from a water treatment in stallation, from bacterial sludge, from a process installa tion, from a cleaning process, from a purification process, and combinations thereof.
  • the filter fraction may be obtained by filtering over a cloth, a sieve, over a filter, in a drum, by centrifugation, and combinations thereof.
  • a par ticle size of the filtered biological material may be smaller than 3 mm, preferably smaller than 2 mm, more pref erably smaller than 1 mm, such as smaller than 0.5 mm, e.g. from 0.02-0.4 mm, such as 0.04-0.1 mm.
  • a pH may be maintained by addition of rejection water from sludge dewatering, by addition of a base, such as a calcium com prising base, such as CaCCh comprising base, and combina tions thereof.
  • a base such as a calcium com prising base, such as CaCCh comprising base, and combina tions thereof.
  • a resi dence time during acidifying may be ⁇ 20 days, preferably ⁇ 10 days, more preferably between 2-6 days, preferably wherein a residence time may be adapted to boundary condi tions, such as temperature.
  • a fatty acid concentration may be maintained ⁇ 40 g/1, preferably ⁇ 20 g/1, such as ⁇ 10 g/1, such as 0.1-7 g/ 1
  • nutri ents may be added, wherein nutrients are selected from N- comprising compounds, P-comprising compounds, and micronutrients .
  • a level of N-comprising nutrients may be maintained above 0.1 mg N/l, preferably above 0.2 mg N/l, more preferably above 1 mg N/l, such as above 2 mg N/l, and/or a level of N-comprising nutrients may be maintained below 100 mg N/l, preferably be low 50 mg N/l, more preferably below 30 mg N/l, such as be low 20 mg N/ 1.
  • a level of P-comprising nutrients may be maintained above 0.1 mg P/1, preferably above 0.2 mg P/1, more preferably above 1 mg P/1, such as above 2 mg P/1, and/or a level of P-comprising nutrients may be maintained below 100 mg P/1, preferably be low 50 mg P/1, more preferably below 30 mg P/1, such as be low 20 mg P/ 1.
  • N and P are relatively low amounts of N and P, respectively, optionally in combination with denitri fying elements such as filters, typically provided in a later stage of the process.
  • maintain amounts of N and P below cer tain levels provides good control.
  • a minimum concentration may be used to ensure that the biomass continues to grow well.
  • a maximum concentration may be used to ensure that a subsequent purification step with VFA does not cause any quality problems with regard to the effluent. Two situations may be considered. A situation where the fatty acid-contain ing solution is added at the beginning or middle of the pu rification process.
  • ammonium and phosphate concentrations do not matter much and could best be kept both at a minimum of 1.0 mg/1.
  • the fatty acid-containing solution is added at the end of the purification process, such as, to sand filters or the deni trification period of a Nereda® process.
  • ammonium maxi mum increase may best be limited to 0.1 mg NH4-N/1 by adding the VFA solution; typically this indicates that 1.0 mg NH4- N/l may be in the VFA solution; for P a maximum increase may best be limited to 0.1 mgP/1 by adding the VFA solution;
  • the filter fraction when the filter fraction is pretreated, such as by washing, or in general, it may contain a too lim ited amount of nutrients, which amount may vary over time, in view of filter fraction source, etc. In such cases nutri ents may be added in order to improve conversion to fatty acids .
  • a sul phate concentration of the filter fraction may be reduced, such as by washing.
  • a tem perature during acidifying is maintained at 0-40 °C, prefer ably at ambient temperature.
  • a re maining filter fraction may be further processed, preferably after de-watering thereof.
  • the present method may be for improving removal of P and/or N in a water treatment instal lation.
  • the method may be operated in a sequence batch reactor, in a continuous batch reactor, in a stirred reactor, in a seg mented reactor, and combinations thereof.
  • the filter fraction before acidifying the filter fraction may be dewatered, such as to 20-50% dry solid contents, preferably 30-40%.
  • an oxi dation reduction potential is maintained in a range of - 400mV ⁇ ORP ⁇ -100 mV, preferably between -300mV ⁇ ORP ⁇ -150 mV, such as -250mV ⁇ ORP ⁇ -180 mV, such as by increasing or decreasing aeration .
  • the system may be loaded with > 0.5 kg COD, preferably > 1, more preferably >2, per m 3 system volume/day.
  • the wastewater may be pre-treated, preferably by at least one of clarification, grit removal, fat removal, grease removal, pH-adjustment, and pre-sedimentation.
  • the present method may fur ther comprise providing a fatty acid producing system 100 com prising an aqueous filter fraction input 1 and a second input 2 for providing an aqueous fluid in fluid connection with said first input, a reactor 5 and a diluted filter fraction fluid connection 3 from said first input to said reactor, a base reservoir 6 in fluid connection 7 with the reactor for in creasing the pH of the fluid in the reactor, a reactor output 8 in fluid connection with a filter 4, a filter output 9 for removing fatty acids, a fluid connection 10 between filter and reactor for returning a part of the filter fraction to the re actor, and a surplus filter fraction output 11 for removing filter fraction.
  • a diluted fluid with 0.5-10 wt .
  • % dry solids is provided to the reactor, such as 1-3 wt . % dry solids.
  • the reactor may comprise controls, such as controls for pH, ORP, N-level, P-level, temperature, solid fraction, fluid level, valves, etc, and combination thereof.
  • controls such as controls for pH, ORP, N-level, P-level, temperature, solid fraction, fluid level, valves, etc, and combination thereof.
  • the present method may fur ther comprise providing a waste water input (21) in fluid connection with a waste water treatment reactor (200), wherein the waste water treatment reactor comprises an outlet (22), the outlet being in fluid connection with a (secondary) sepa ration device (211), the separation device being in fluid connection with an effluent outlet (23) and with a return path (3), wherein the separation device may be a filter, the return path being in fluid connection (24) with the inlet of the waste water treatment reactor and with the a diluted filter fraction fluid connection (3) of the fatty acid producing sys tem (100), the filter output (9) being in fluid connection with the waste water input (21), and the surplus filter frac tion output (11) being in fluid connection with the filter output (25)
  • the reactor and fatty acid producing system may be considered a second aspect of the present invention.
  • Figure 1-2 show reactor set-ups.
  • Figure 3 shows cumulative COD conversion to sCOD in column filled with dry (35% TS) SF.
  • Figure 4 shows denitrification test with acidified SF and acetic acid as a reference.
  • Figure 1 shows a fatty acid producing system 100 comprising an aqueous filter fraction input 1 and a second input 2 for providing an aqueous fluid in fluid connection with said first input, a reactor 5 and a diluted filter fraction fluid connec tion 3 from said first input to said reactor, a base reservoir 6 in fluid connection 7 with the reactor for increasing the pH of the fluid in the reactor, a reactor output 8 in fluid con nection with a separation device or method, such as afilter 4, a filter output 9 for removing fatty acids, a fluid connection 10 between filter and reactor for returning a part of the fil ter fraction to the reactor, and a surplus filter fraction output 11 for removing filter fraction.
  • a separation device or method such as afilter 4
  • a filter output 9 for removing fatty acids
  • a fluid connection 10 between filter and reactor for returning a part of the fil ter fraction to the reactor
  • a surplus filter fraction output 11 for removing filter fraction.
  • FIG. 2 shows a waste water input 21 in fluid connection with a waste water treatment reactor 200, wherein the waste water treatment reactor comprises an outlet 22, the outlet be ing in fluid connection with a separation device such as a filter 211, the separation device being in fluid connection with an effluent outlet 23 and with a return path 3, the re turn path being in fluid connection 24 with the inlet of the waste water treatment reactor and over filter 4 for producing a fine filter fraction with the a diluted filter fraction fluid connection 3 of the fatty acid producing system 100, the filter output 9 being in fluid connection with the waste water input 21, and the surplus filter fraction output 11 being in fluid connection with the filter output 25
  • a column filled with 1 liter of dry SF (35% TS) was contin uously percolated with tap water.
  • Ammonium and phosphate buffer were added to the tap water to prevent nutrient and pH limitation.
  • Temperature in the column was maintained at 37 °C by indirect heating with warm tap water.
  • Soluble COD (sCOD) and VFA' s were measured in the percolate.
  • 25% of the COD in SF was converted to soluble COD, see figure 3.
  • Analysis of the sCOD with HPLC revealed that circa 85% of the COD can be attributed to VFA' s; 2/3 acetic acid and 1/3 propionic acid.
  • sCOD concentrations in the percolate were typically 100-200 mg/1. Percolation flow was 3-6 1/day.
  • the CSTR was manually fed with wet SF (3% TS) 3-4 times per week.
  • the average HRT was 6 days.
  • sCOD concentrations were circa 8-10 g/1, circa 26% of the COD in SF was converted to VFA' s .
  • Acidified SF from the CSTR experiment was centrifuged and used as a carbon source in a denitrification batch experiment.
  • the denitrification rate was compared to acetic acid as a reference, see fig 4.
  • Average denitrification rates at room temperature (20 °C) were 2,6 and 3,0 g NCp-N/kg DS.hr for acid ified SF and acetic acid respectively. Note that the grey dots present the denitrification rate in activated sludge without addition of external carbon source which is repre sentative for most activated sludge installations.

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Abstract

L'invention concerne le domaine du traitement des eaux usées, en particulier un procédé de production d'acides gras à partir d'une fraction de tamis d'eaux usées ou de boues activées à partir d'eaux usées traitées, et est applicable à une fraction de filtre à partir de toute solution aqueuse comprenant du matériel biologique et/ou organique. L'invention améliore en outre l'élimination de P et/ou N dans une installation de traitement de l'eau.
PCT/NL2020/050472 2019-07-26 2020-07-17 Production d'acides gras à partir d'une fraction de tamis de boues activées à partir d'eaux usées traitées WO2021020964A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP20746305.0A EP3999653A1 (fr) 2019-07-26 2020-07-17 Production d'acides gras à partir d'une fraction de tamis de boues activées à partir d'eaux usées traitées

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Application Number Priority Date Filing Date Title
NL2023573A NL2023573B1 (en) 2019-07-26 2019-07-26 Production of fatty acids from a sieve fraction of activated sludge from treated wastewater
NL2023573 2019-07-26

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104450805A (zh) 2014-11-21 2015-03-25 湖南大学 短链挥发性脂肪酸及其制备方法
CN104862346A (zh) 2015-05-04 2015-08-26 同济大学 一种酶碱联合预处理提高剩余污泥产短链脂肪酸的方法
CN108384816A (zh) 2018-02-08 2018-08-10 同济大学 短链脂肪酸及利用污泥厌氧发酵生成短链脂肪酸的方法

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104450805A (zh) 2014-11-21 2015-03-25 湖南大学 短链挥发性脂肪酸及其制备方法
CN104862346A (zh) 2015-05-04 2015-08-26 同济大学 一种酶碱联合预处理提高剩余污泥产短链脂肪酸的方法
CN108384816A (zh) 2018-02-08 2018-08-10 同济大学 短链脂肪酸及利用污泥厌氧发酵生成短链脂肪酸的方法

Non-Patent Citations (9)

* Cited by examiner, † Cited by third party
Title
C.J. RUIKEN ET AL: "Sieving wastewater - Cellulose recovery, economic and energy evaluation", WATER RESEARCH, vol. 47, no. 1, 1 January 2013 (2013-01-01), AMSTERDAM, NL, pages 43 - 48, XP055736956, ISSN: 0043-1354, DOI: 10.1016/j.watres.2012.08.023 *
DA ROS CINZIA ET AL: "Sieving of municipal wastewater and recovery of bio-based volatile fatty acids at pilot scale", WATER RESEARCH, ELSEVIER, AMSTERDAM, NL, vol. 174, 115633, 20 February 2020 (2020-02-20), pages 1 - 10, XP086099657, ISSN: 0043-1354, [retrieved on 20200220], DOI: 10.1016/J.WATRES.2020.115633 *
DAFNE CRUTCHIK ET AL: "Biorefinery of cellulosic primary sludge towards targeted Short Chain Fatty Acids, phosphorus and methane recovery", WATER RESEARCH, vol. 136, 1 June 2018 (2018-06-01), AMSTERDAM, NL, pages 112 - 119, XP055737126, ISSN: 0043-1354, DOI: 10.1016/j.watres.2018.02.047 *
DAFNE CRUTCHIK ET AL: "Supporting Information: Biorefinery of cellulosic primary sludge towards targeted Short Chain Fatty Acids, phosphorus and methane recovery", 1 June 2018 (2018-06-01), XP055737322, Retrieved from the Internet <URL:https://ars.els-cdn.com/content/image/1-s2.0-S0043135418301544-mmc1.docx> [retrieved on 20201006] *
FANG WEI ET AL., J. ENVIRONMENTAL SCIENCES, vol. 87, 5 June 2019 (2019-06-05), pages 93 - 111
JING XIE ET AL: "Influence of sulfadiazine on anaerobic fermentation of waste activated sludge for volatile fatty acids production: Focusing on microbial responses", CHEMOSPHERE, vol. 219, 1 March 2019 (2019-03-01), GB, pages 305 - 312, XP055682830, ISSN: 0045-6535, DOI: 10.1016/j.chemosphere.2018.12.015 *
MORGAN-SA-GASTUME ET AL., BIORESOURCE TECHNOLOGY, vol. 102, no. 3, 1 February 2011 (2011-02-01), pages 3089 - 3097
XIE ET AL., CHEMOSPHERE, vol. 219, 1 March 2019 (2019-03-01), pages 305 - 312
ZHANG ET AL., WATER RESEARCH, vol. 43, no. 15, 1 August 2009 (2009-08-01), pages 3735 - 3742

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EP3999653A1 (fr) 2022-05-25

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