US20130228457A1 - Reactor for recovering phosphate salts from a liquid - Google Patents

Reactor for recovering phosphate salts from a liquid Download PDF

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Publication number
US20130228457A1
US20130228457A1 US13/883,586 US201113883586A US2013228457A1 US 20130228457 A1 US20130228457 A1 US 20130228457A1 US 201113883586 A US201113883586 A US 201113883586A US 2013228457 A1 US2013228457 A1 US 2013228457A1
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United States
Prior art keywords
reactor
reactor according
magnesium
housing
phosphate
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Abandoned
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US13/883,586
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English (en)
Inventor
Jennifer Bilbao
Dieter Bryniok
Alejandra Campos
Siegfried Egner
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Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV
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Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV
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Assigned to FRAUNHOFER-GESELLSCHAFT ZUR FOERDERUNG DER ANGEWANDTEN FORSCHUNG E.V. reassignment FRAUNHOFER-GESELLSCHAFT ZUR FOERDERUNG DER ANGEWANDTEN FORSCHUNG E.V. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BRYNIOK, DIETER, EGNER, SIEGFRIED, BILBAO, JENNIFER, CAMPOS, ALEJANDRA
Publication of US20130228457A1 publication Critical patent/US20130228457A1/en
Abandoned legal-status Critical Current

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    • 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
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • 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
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/02—Biological treatment
    • C02F11/04—Anaerobic treatment; Production of methane by such processes
    • 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
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/46104—Devices therefor; Their operating or servicing
    • C02F1/46109—Electrodes
    • C02F2001/46133—Electrodes characterised by the material
    • 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
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/46104—Devices therefor; Their operating or servicing
    • C02F1/46109—Electrodes
    • C02F2001/46152—Electrodes characterised by the shape or form
    • 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
    • C02F2101/105—Phosphorus compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/002—Construction details of the apparatus
    • C02F2201/003—Coaxial constructions, e.g. a cartridge located coaxially within another
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/46—Apparatus for electrochemical processes
    • C02F2201/461—Electrolysis apparatus
    • C02F2201/46105—Details relating to the electrolytic devices
    • C02F2201/4616—Power supply
    • C02F2201/4617—DC only

Definitions

  • the invention concerns a reactor for complete separation of phosphate from a liquid and recovery of phosphate salts, comprising a housing and two electrodes of different polarity.
  • Phosphate salts such as magnesium ammonium phosphate (in the following abbreviated as MAP) or potassium magnesium phosphate (in the following abbreviated as PMP) are high-value plant adjuvants for which there is high demand.
  • the elements nitrogen, potassium, magnesium, and phosphate of which these plant adjuvants are comprised are typically contained in all solid or liquid organic waste materials. While potassium, magnesium and other ions are present in the form of water-soluble cations, nitrogen and phosphate are predominantly bound to or in organic material or cell mass. Accordingly, a major proportion of nitrogen and phosphate are not available for the production of plant adjuvants. For this reason it is necessary to convert nitrogen and phosphate into their inorganic form that is suitable for precipitation.
  • the spontaneous precipitation of MAP or PMP is limited by the usually very low magnesium concentration in wastewater.
  • Known is the addition of magnesium hydroxide, magnesium oxide or soluble magnesium salts for MAP precipitation.
  • the disadvantage in this context is the bad solubility of the oxides as well as of the salt-like hydroxides.
  • magnesium hydroxide or magnesium oxide dissolve only very slowly and with a minimal proportion. This has the result that it is necessary to continuously perform stirring or mixing which, however, causes extra expenditure in regard to technology and energy and thus also with respect to costs.
  • both compounds because of their bad solubility, must be added in over-stoichiometric amounts because otherwise an incomplete precipitation of the desired plant adjuvants occurs and significant quantities of phosphate remain in the wastewater.
  • magnesium salts are beforehand transferred into a solution, the efficiency of the method decreases because of the dilution with water.
  • Wastewater has usually pH values between 5 and 7. Therefore, for increasing the pH value, a base is added.
  • a soluble base for example, sodium hydroxide.
  • a base that is sparingly soluble for example, magnesium hydroxide, the latter will hardly dissolve in water and the aforementioned disadvantages will occur.
  • WO 00200101019735 A1 discloses a reactor for removal of dissolved nitrogen and phosphate from the aqueous portion of liquid manure by means of electrochemical precipitation.
  • the reactor described therein requires relatively high electrical voltages and is therefore energy-intensive and cost-intensive.
  • a disadvantage is also that nitrogen and phosphate that are present organically bound in the aqueous portion of the liquid manure cannot be removed by the disclosed method. As a result of this, this wastewater must therefore be subjected to a subsequent purification in a water treatment plant.
  • the construction of the reactor is disadvantageous in that, due to the arrangement of the electrodes, large areas are generated in which the liquid to be purified has no direct contact with the electrodes. Moreover, as a result of the geometry of the sacrificial anode more magnesium than required is released. Both effects reduce the efficiency of the reactor significantly.
  • due to the use of aluminum-containing electrodes the plant poison aluminum ends up in the precipitation product. When this product is applied to the soil, the aluminum can be released and the plant growth can be affected negatively.
  • An electrochemical precipitation reactor for MAP is disclosed in WO 2007/009749 A1.
  • the reactor is however not suitable for the precipitation of other phosphate salts.
  • the construction of the reactor does not allow for automatic separation between purified wastewater and precipitated MAP so that it is necessary to arranged downstream of the reactor a further apparatus for solid/liquid separation.
  • a significantly higher apparatus expenditure is required because, as a result of the construction, the housing of the reactor cannot be operated as a cathode.
  • the magnesium is dissolved non-uniformly because, due to the spatial arrangement of the electrodes in the reactor, only one side of the anode is participating in the reaction.
  • the invention has the object to provide a reactor by means of which phosphate-containing wastewater can be treated and supplied to a further use. Moreover, the invention has the object to provide a reactor for recovery of phosphate salts as plant adjuvants which overcomes the aforementioned disadvantages of the prior art.
  • the object is solved according to the invention by a reactor with a housing. At the center of the housing a sacrificial anode of magnesium or a magnesium-containing material is arranged. An inert cathode is arranged concentrically about the sacrificial anode.
  • the arrangement of the electrodes in accordance with the invention provides for a best possible control of the release of magnesium ions. Since the spacing between magnesium anode and cathode is kept as minimal as possible, the ions that are required for the precipitation of the phosphate salts are immediately in contact with each other and a constantly high concentration of magnesium ions in the reaction space is ensured. At the same time, because of the geometry of the sacrificial anode, its surface is very small so that only little magnesium is spontaneously released. In this way, advantageously an unnecessary excess of magnesium ions is prevented.
  • the reactor according to the invention it is possible by application of a minimal electrical direct current, smaller than 1 V with current strengths below 1 A, to supply magnesium ions to the phosphate-containing and ammonium-containing liquid and to split the water that is contained in the liquid to OH ⁇ and H + ions so that the pH value is increased and the reactions required for precipitation can take place. Due to the minimal energy demand, the costs for operating the device drop in comparison to methods known from the prior art. It is even possible to operate the reactor by galvanic operation. Electrical current is produced thereby.
  • an anaerobic fermentation process is arranged upstream of the reactor according to the invention.
  • nitrogen and phosphorus that are bound organically are decomposed to inorganic water-soluble ions.
  • ammonium (NH 4 + ) and phosphate (PO 4 3 ⁇ ) the phosphate salts, in particular MAP and PMP, can be formed.
  • nitrogen and phosphate that are bound predominantly to or in organic material or cell mass are converted advantageously into a water-soluble form and are thus available for the production of plant adjuvants.
  • biogas is produced which has a significant market value as an energy source.
  • an advantageous embodiment of the invention provides that the housing is manufactured of an electrically conductive material, for example, metal and therefore serves as an inert cathode.
  • the reaction space is limited to the space between the two electrodes. In this way, dead space is avoided and thus material costs are lowered.
  • a further advantage of the invention provides that the sacrificial anode is comprised substantially of magnesium.
  • this includes also electrode materials that are comprised of a magnesium alloy or magnesium with minimal additions of other components.
  • the reactor according to the present invention has an inlet for the phosphate-containing liquid, an outlet for the purified liquid, as well as a removal device for the precipitated phosphate salts.
  • the crystals can be removed via the removal device by means of a shut-off valve, for example, a seat valve or disk valve or ball valve, from the reactor without the inlet or outlet being changed and thereby the purification performance of the reactor being negatively affected.
  • An advantageous embodiment of the reactor according to the invention provides for the operation of the reactor as an upflow reactor.
  • the inlet is located laterally at the bottom end of the reactor.
  • the wastewater flows upward and escapes laterally at the top.
  • This arrangement has the advantage that an automatic separation of liquid that flows upwardly and precipitated salts that sink to the bottom is taking place.
  • the reactor can be operated also as a downflow reactor wherein the liquid and solid move in the same direction. In this way, the sedimentation rate of the precipitated phosphate salts is accelerated. This means that the reactor can be made smaller for the same throughput.
  • the crystals are separated in a filter from the liquid.
  • the precipitated phosphate salts can be removed together with the liquid from the reactor. Accordingly, additional fixtures or devices for separate solids removal are saved. Also, in case of common removal of phosphate salts and purified wastewater, a turbulent flow is generated in the conduit and prevents clogging of the conduit by the crystals.
  • the housing of the reactor is closed.
  • the electrolytic reactions that occur in the reactor produce large quantities of foam which in case of a closed housing cannot overflow. Accordingly, in an advantageous way, a product loss is avoided.
  • the housing of the reactor can also be open partially or entirely.
  • the reactor according to the invention operates even better when it has a slanted bottom. In this way, it is possible that the precipitated crystals glide along the slanted surface downwardly and collect at the removal device. In this way, the crystals can be removed from the reactor without its continuous operation having to be interrupted.
  • the formation of the slanted surface is realized by a preferably conical bottom. Conceivable is also the shape of a pyramid.
  • An advantageous embodiment of the reactor according to the invention provides that to the sacrificial anode a positive pole and to the cathode a negative pole of a direct current source are connected.
  • the supply of electrical current prevents deposits on the electrode which are not stable in the electrical field.
  • the reactor on the other hand, is operated without a direct current source, we by the process of magnesium release electrons are released. This means that the reactor requires no electrical current but even produces electrical current.
  • FIG. 1 a schematic illustration of the reactor according to the invention
  • FIG. 2 a schematic illustration of a first embodiment of the reactor according to the invention
  • FIG. 3 a schematic illustration of a second embodiment of the reactor according to the invention
  • FIG. 4 a schematic illustration of a third embodiment of the reactor according to the invention
  • FIG. 5 a schematic illustration of a third embodiment of the reactor according to the invention for recovery of phosphate salts
  • FIG. 6 a schematic illustration of the use of the reactor according to the invention with upstream fermentation process
  • FIG. 1 shows a schematic illustration of a reactor 10 according to the invention.
  • the reactor 10 has a housing 12 .
  • the housing 12 serves for receiving a phosphate-containing liquid 14 .
  • an electrode 16 is arranged at the center of the housing 12 .
  • the electrode 16 is a so-called sacrificial anode which is connected to the positive pole of a direct current source, not illustrated in the drawing, while the housing 12 forms the cathode 18 which is connected to a negative pole of the direct current source.
  • the sacrificial anode 16 is comprised of a magnesium-containing material so that magnesium ions are transferred into the solution 14 as soon as electrical voltage is applied to the electrodes 16 and 18 .
  • the formed phosphate salts are sparingly soluble in aqueous solution and precipitate as crystals which deposit at a bottom of the reactor 10 .
  • One configuration of the reactor 10 according to the invention provides for galvanic operation.
  • the two electrodes 16 , 18 are not connected to the external direct current source.
  • the magnesium ions are transferred into solution by galvanic operation.
  • FIG. 2 shows a first embodiment variant of the reactor 10 according to the invention. Illustrated is the housing 12 of the reactor and centrally arranged therein is the electrode 16 that is embodied as a sacrificial anode. Concentric between housing 12 and electrode 16 there is the cathode 18 . In this special arrangement the spacing between sacrificial anode 16 and inert cathode 18 is minimal so that the ions that are participating in the precipitation are immediately in contact with each other.
  • FIG. 3 the reactor 10 is illustrated. Laterally at a preferably conical bottom 22 there is an inlet 24 . An outlet 26 is located at the top laterally at the housing 12 of the reactor 10 . An optional return line 28 connects the outlet 26 with the inlet 24 . At the bottom end of the preferably conical bottom 22 there is the removal device 30 .
  • the phosphate-containing liquid 14 flows through the inlet 24 from the bottom to the top through the reactor 10 and exits from it through the outlet 26 .
  • the precipitated phosphate salts glide along the slanted plane of the conical bottom 22 in downward direction and are removed via the removal device 30 .
  • the reactor 10 can be operated continuously and the precipitated and deposited crystals can be removed at any time without changing a throughput of the reactor.
  • the optional return line 28 already purified liquid 14 is returned to the reactor 10 as circulating water.
  • FIG. 4 shows a third embodiment of the reactor 10 according to the invention.
  • the reactor 10 is flowed through in downward direction.
  • the inlet 24 is located laterally at the top on the housing 12 .
  • the outlet 26 is located laterally at the conical bottom 22 .
  • the optional return line 28 connects the outlet 26 with the inlet 24 .
  • the removal device 30 is arranged at the conical bottom 22 .
  • the phosphate-containing liquid 14 flows through the inlet 24 from the top to the bottom through the reactor 10 and exits from it through the outlet 26 . Precipitated phosphate salts are removed via the removal device 30 without affecting the operation of the reactor. By means of return line 28 the already purified liquid 14 is supplied again to the reactor 10 as circulating water.
  • FIG. 5 shows a further embodiment of the reactor 10 according to the invention.
  • the reactor 10 is flowed through in downward direction.
  • the inlet 24 is located laterally at the top at the housing 12 .
  • the outlet 26 is located at the bottom end at the conical bottom 22 and extends from there to a downstream filter 31 .
  • the optional return line 28 connects the outlet 26 with the inlet 24 .
  • the precipitated phosphate salts are removed together with the purified liquid 14 from the reactor 10 .
  • the phosphate salts are separated from the liquid 14 .
  • FIG. 6 an application of the reactor 10 according to the invention in connection with producing biogas from phosphorus-containing wastewater is schematically illustrated.
  • a wastewater flow 32 of organic origin is supplied to a bioreactor 34 .
  • the organic carbon compounds that are contained in the solids are converted into biogas and mineral residual substances.
  • ammonium-containing and phosphate-containing process water 36 is produced.
  • possibly contained solids 40 are separated in a filter 38 .
  • the solids 40 which are retained in the filter 38 are returned into the bioreactor 34 .
  • the phosphate salts are separated.
  • the ammonium-containing and phosphate-containing outflow 26 can be returned partially into the bioreactor 34 . In this way, an impairment of the fermentation process, caused by a high ammonium concentration, is prevented.
US13/883,586 2010-11-06 2011-10-31 Reactor for recovering phosphate salts from a liquid Abandoned US20130228457A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102010050692A DE102010050692B3 (de) 2010-11-06 2010-11-06 Reaktor zur Rückgewinnung von Phosphatsalzen aus einer Flüssigkeit
DE102010050692.3 2010-11-06
PCT/EP2011/069119 WO2012059465A1 (de) 2010-11-06 2011-10-31 Reaktor zur rückgewinnung von phosphatsalzen aus einer flüssigkeit

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US (1) US20130228457A1 (de)
EP (1) EP2635534B1 (de)
BR (1) BR112013011181A2 (de)
CA (1) CA2815914C (de)
DE (1) DE102010050692B3 (de)
DK (1) DK2635534T3 (de)
RU (1) RU2013124995A (de)
WO (1) WO2012059465A1 (de)

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US10363523B2 (en) 2012-12-19 2019-07-30 Fuji Electric Co., Ltd. Exhaust gas purifying apparatus
WO2022036326A1 (en) * 2020-08-14 2022-02-17 The Board Of Trustees Of The Leland Stanford Junior University Systems and methods of flexible electrochemical stripping to recover alkaline ammonia and acidic ammonium from wastewaters

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DE102012220810B3 (de) 2012-11-14 2014-02-13 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Verfahren zur erhöhten Phosphorrückgewinnung aus organischen Reststoffen
DE102014207842C5 (de) 2014-04-25 2018-05-17 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Kombinierte Rückgewinnung von Phosphor, Kalium und Stickstoff aus wässrigen Reststoffen
DE102015215037B4 (de) 2015-08-06 2021-02-25 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Reaktor mit Opferanode
DE102016109822A1 (de) 2016-05-27 2017-11-30 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Elektrolytischer Reaktor
DE102016109824A1 (de) 2016-05-27 2017-11-30 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Elektrolytischer Reaktor umfassend eine Kathode und eine Anode
DE102016115554A1 (de) 2016-08-22 2018-02-22 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Anlage zur Gewinnung von Phosphatsalzen und biologische Kläranlage sowie Verfahren zum Betreiben dieser Anlagen
EP3375760A1 (de) 2017-03-13 2018-09-19 Joachim Clemens Verfahren zur fällung von phosphor und natrium in abwasser
DE102019108832A1 (de) 2019-04-04 2020-10-08 Antonia Hollerbach Verfahren zur Abwasserbehandlung
DE102021127350A1 (de) 2021-10-21 2023-04-27 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung eingetragener Verein Elektrolytische Reaktoren

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10363523B2 (en) 2012-12-19 2019-07-30 Fuji Electric Co., Ltd. Exhaust gas purifying apparatus
WO2022036326A1 (en) * 2020-08-14 2022-02-17 The Board Of Trustees Of The Leland Stanford Junior University Systems and methods of flexible electrochemical stripping to recover alkaline ammonia and acidic ammonium from wastewaters

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Publication number Publication date
CA2815914A1 (en) 2012-03-10
EP2635534B1 (de) 2016-09-21
WO2012059465A1 (de) 2012-05-10
DE102010050692B3 (de) 2012-03-22
EP2635534A1 (de) 2013-09-11
RU2013124995A (ru) 2014-12-20
CA2815914C (en) 2017-07-25
BR112013011181A2 (pt) 2016-08-02
DK2635534T3 (da) 2017-01-02

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