Classifications

• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen; Reversible storage of hydrogen
  • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
  • C01B3/04—Production of hydrogen; Production of gaseous mixtures containing hydrogen by decomposition of inorganic compounds
  • C01B3/047—Decomposition of ammonia
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
  • C01C1/00—Ammonia; Compounds thereof
  • C01C1/02—Preparation, purification or separation of ammonia
  • C01C1/10—Separation of ammonia from ammonia liquors, e.g. gas liquors
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F9/00—Multistage treatment of water, waste water or sewage
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
  • C01B2203/08—Methods of heating or cooling
  • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
  • C01B2203/0861—Methods of heating the process for making hydrogen or synthesis gas by plasma
• • 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
  • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
• • 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
  • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
  • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
• • 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
  • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
  • C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
• • 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
  • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
  • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
• • 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
  • C02F1/487—Treatment of water, waste water, or sewage with magnetic or electric fields using high frequency electromagnetic fields, e.g. pulsed electromagnetic fields
• • 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
  • C02F1/72—Treatment of water, waste water, or sewage by oxidation
  • C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
• • 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

Definitions

• the present invention relates to a system for treating a liquid source comprising ammonia. More particularly, the system of the present invention comprises a module for extracting the ammonia in the form of gaseous ammonia from the liquid source and a module for converting the gaseous ammonia extracted into dinitrogen and dihydrogen.
• the present invention also relates to a method of treating a liquid source comprising ammonia. More particularly, the method of the present invention comprises a step of extracting the ammonia in the liquid source in the form of gaseous ammonia and a step of converting the extracted gaseous ammonia into dinitrogen and dihydrogen.
• the management and treatment of wastewater is necessary for the protection of the environment.
• the objective of wastewater treatment is to eliminate pollution, in particular particulate pollution (we also speak of suspended matter) and soluble pollution (we also speak of dissolved pollution), and in particular carbon, nitrogen and phosphorus pollution.
• a wastewater treatment plant can also recover this pollution by reusing it, for example for resource recovery or energy generation.
• growing urbanization and population growth are putting significant pressure on the land available for wastewater treatment plants. These must be more compact and limit the discharge of pollutants even though they must deal with larger quantities of pollution to be treated.
• Ammonia is considered a pollutant because its accumulation in water bodies can cause serious ecological problems, such as accelerated eutrophication of lakes and rivers, oxygen depletion dissolved and toxicity to fish and other aquatic animals present in the water body.
• effluent treatment processes are based on the elimination of pollutants (anaerobic and aerobic biological processes, adsorption, chemical oxidation or combustion) or on the concentration of these pollutants (flocculation, precipitation, ultrafiltration, nanofiltration, reverse osmosis and evaporation ).
• the traditional method of removing ammonia from municipal and industrial wastewater is based on biological treatments, i.e. nitrification and denitrification.
• the recovery of phosphorus in a recoverable form can also be implemented in anaerobic digester liquors using the crystallization/precipitation of non-metallic minerals, for example in the form of struvite (mineral composed of mono-ammonium phosphate , known in English under the name “Magnesium Ammonium Phosphate” whose acronym is “MAP”), calcium phosphates, brushite, hydroxyapatite, etc.
• struvite mineral composed of mono-ammonium phosphate , known in English under the name “Magnesium Ammonium Phosphate” whose acronym is “MAP”
• patent application EP 2238081 discloses a phosphorus recovery process aimed at limiting the undesirable precipitation of phosphorus in the form of struvite in the digester and/or the pipes.
• the crystallization processes are based on the solubility balance of the minerals formed, which depend on the temperature and/or the pH.
• the more concentrated the solution from which the phosphorus is to be recovered the easier it is to convert a large portion of it into the desired valuable mineral. Therefore, the conversion efficiency that can be achieved is concentration dependent, and the rather low initial concentration of phosphate in the anaerobic digestion liquor often limits the applicability and recovery efficiency of these crystallization processes. Consequently, such a phosphorus recovery process may not be applicable to all installations due to a PO 4 content that is sometimes too low to carry out crystallization or due to too low conversion rates which are detrimental to the process. economic balance of such a solution.
• phosphorus we mean several forms of compound comprising phosphorus, in particular the chemical forms phosphate and compounds comprising ammonia and phosphate, such as mono-ammonium phosphate (MAP), salts of ammonia and phosphate. phosphoric acid, etc.
• MAP mono-ammonium phosphate
• salts of ammonia and phosphate such as phosphoric acid, etc.
• the present invention aims to overcome all or part of the problems cited above by proposing a system which uses in an optimized manner the ammonia concentration and optionally the phosphorus concentration of a liquid source.
• the system of the present invention makes it possible in particular to directly recover the ammonia and/or phosphorus contained in a liquid source instead of eliminating them, these being previously considered mainly as pollutants.
• the system of the present invention doubles the value of these elements by their recovery, potentially their separation, and by their reuse.
• the subject of the invention is a system for treating a liquid source comprising ammonia, the system comprising a module for extracting the ammonia included in the source in the form of gaseous ammonia. liquid and producing a discharge liquid, and a module for converting the ammonia extracted into dinitrogen and dihydrogen, the conversion module being a reactor using a non-thermal plasma coupled or not to catalysis.
• the stripping module of one of the systems previously described is configured to operate under vacuum.
• the liquid source comprising ammonia from one of the systems previously described is fermented urine.
• one of the systems previously described further comprises a module for purifying and/or separating the dinitrogen and the dihydrogen extracted by the conversion module.
• one of the systems described above further comprises a means for reinjecting the dinitrogen and the dihydrogen produced by the means of converting the extracted ammonia, or a means for reinjecting the dihydrogen purified and/or separated from the dinitrogen , towards a methanation reactor.
• one of the systems previously described further comprises, upstream of the concentration module, an anaerobic digester supplying at least one anaerobic digestate liquor to a liquid/solid separation module and/or a dehydration module, the liquid/solid separation module and/or the dehydration module providing a liquid fraction being the liquid source comprising ammonia.
• the system further comprises a means for reinjecting the dinitrogen and the dihydrogen produced by the means of converting the extracted ammonia, or a means for reinjecting the dihydrogen purified and/or separated from the dinitrogen, towards the anaerobic digester .
• the liquid source further comprises phosphorus and the system further comprises a first phosphorus recovery module included in the liquid source or the concentrated liquid source, the ammonia concentration module in the liquid source being also a module for concentrating the phosphorus present in the liquid source.
• the liquid source further comprises phosphorus and the system further comprises a second phosphorus recovery module included in the discharge liquid, the extraction module being configured to maintain a residual concentration of ammonia in the discharge liquid.
• the extraction module is a stripping module, and the first or the second phosphorus recovery module and the stripping module are included in a single reactor.
• the invention also relates to a method of treating a liquid source comprising ammonia, the method comprising the following steps: a step of extracting gaseous ammonia from the ammonia included in the liquid source and producing a discharge liquid, and a step of converting the gaseous ammonia extracted into dinitrogen and dihydrogen, the conversion step being carried out with a reactor using a non-thermal plasma coupled or not to catalysis.
• the liquid source further comprises phosphorus
• the method further comprises a step of recovering the phosphorus in the liquid source, and/or in the liquid source after a step of concentrating the phosphorus in the liquid source, and/or in the discharge liquid.
• the method further comprises a step of reinjecting the dihydrogen and the extracted dinitrogen, or the dihydrogen alone after purification or separation of the dinitrogen, to an anaerobic digester or to a methanation reactor.
• the method further comprises a preliminary step of concentrating the ammonia included in the liquid source before the step of extracting the gaseous ammonia from the ammonia included in the liquid source.
• Figure 1 represents a system for treating a liquid source comprising ammonia according to the present invention and an option of this system.
• Figure 2 represents a system for treating a liquid source comprising ammonia, and optionally phosphorus, according to the present invention and further comprising one or more additional elements among: one or more phosphorus recovery modules , a dihydrogen and dinitrogen separation module, and a methanation reactor.
• Figure 3 represents a system for treating a liquid source as described in Figure 2, further comprising optional reinjection means towards an anaerobic digester and a liquid/solid separation module.
• Figure 1 represents a treatment system 10 of a liquid source 11 comprising ammonia according to the present invention and an option of this system.
• the system of the present invention comprises an extraction module 12 in the form of gaseous ammonia from the ammonia included in the liquid source 11.
• the extraction module 12 receives as input the liquid source 11 comprising ammonia and makes it possible to separate the liquid ammonia in the form of an ammonia gas from the liquid source, transforming the liquid source into a discharge liquid 13 , this discharge liquid necessarily containing an ammonia concentration lower than the ammonia concentration of the liquid source 11.
• the extraction module 12 allows the transfer of ammonia into the gas phase and the recovery of this gas phase.
• the extraction module can be a stripping module, also called “strippers", or stripping columns. .
• stripping systems are described in patent FR2988304 B1.
• Such a stripping module makes it possible in particular to cause the ammonia to volatilize by means of a current of steam, gas or air passing through the liquid against the current.
• the stripping module in the system of the present invention can be a physicochemical or membrane stripping module.
• Membrane stripping comprises two treatment stages, the first stage consisting of a pretreatment of the liquor obtained from the anaerobic digester, this liquor having preferably undergone a liquid/solid separation stage, during which the equilibrium of the liquid phase is moved to the gas phase typically by raising the pH between 9.3 and 10 and increasing the temperature of the liquid source, typically between 35 and 50°C. Further pH modifications may be necessary. Pretreatment potentially extracts suspended solids and byproducts contained in liquors and byproducts from elevated temperature and pH. The ammonia then diffuses through a hydrophobic membrane or a membrane contactor, with the possibility of circulating an acidic solution on the other side of the membrane contactor (TMCS: transmembrane chemisorption) to improve the transfer. In the case of a TMCS, the acidic liquor concentrated in NH 4 + can then be subjected to an increase in pH to pass the ammonia in the dissolved phase (NH 4 + ) towards the ammonia gas phase (NH 3 ).
• TMCS transmembrane chem
• the stripping module is a vacuum stripping module.
• vacuum stripping requires a single pH change step to extract ammonia in gaseous form and optionally allows the use of dinitrogen as a vector.
• a vacuum stripping module allows you to remove the necessary quantity of stripping air.
• the ammonia in gaseous form extracted by the extraction module 12 is then transferred to a conversion module allowing the transformation of the gaseous ammonia extracted into dinitrogen and dihydrogen 15.
• the conversion module is a reactor using a non-thermal plasma coupled or not to catalysis.
• the reactor using a non-thermal plasma coupled to catalysis is a plasma discharge reactor with a dielectric barrier, also called a “DBD reactor”.
• a reactor using a non-thermal plasma also called cold plasma or non-equilibrium plasma
• the majority of the coupled energy is mainly delivered to the free electrons which exceed several orders of magnitude the temperature of the heavy species in the plasma (ions and neutral molecules).
• Such mixtures will have high-energy electrons in a relatively cold mass of neutral ions and molecules; therefore, the apparent temperature of the gas remains similar to the ambient temperature if exothermic or endothermic phenomena are absent.
• This type of plasma refers to a plasma state which is not in thermal equilibrium: equilibrium is not reached because the electron density is not high enough compared to other heavy particles to achieve a transfer of energy. sufficient energy between electrons and heavy particles.
• Ionization and chemical processes in these plasmas are established by the temperature (or energy level) of the electrons and are not so sensitive to thermal processes and gas temperature.
• the most common method of generating plasma involves applying an electric field to a neutral gas. If the applied field exceeds a certain energy density threshold (called breakdown voltage), a gas discharge is formed, thus initiating the formation of a plasma.
• breakdown voltage a certain energy density threshold
• a DBD, or DBD plasma, reactor involves a specific type of alternating current (AC) discharge at atmospheric pressure, providing an unbalanced, non-thermal, cold plasma.
• the main advantages of the DBD plasma reactor are its ability to produce highly reactive plasma at room temperature with low electrical power consumption and short response time.
• An ammonia gas can then be transformed into hydrogen and nitrogen (dihydrogen and dinitrogen) in a DBD plasma reactor with high yields.
• Mr. El-Shafie has proven that a “PPR” reactor (Plasma Plate Reactor) can be used for this purpose (M.
• source of liquid comprising ammonia is meant a liquid source whose ammonia concentration is greater than 0. However, for economic and industrial reasons, a minimum concentration of at least 500 mg /l is preferred.
• the liquid source 1 1 comprising ammonia according to the present invention can be an effluent from a water treatment plant, an industrial or agricultural operation or any other effluent comprising ammonia.
• the liquid source may have undergone prior stages of transformation, fermentation or not.
• the liquid source 1 1 may comprise fermented urine, or aged urine (known in English under the term "lant”) mixed or not with another liquid, the fermentation increasing the ammonia concentration by decomposition of the urea.
• an ammonia concentration of at least 3000 mg/l is preferred.
• a source of waste heat for example energy production sites heat emitters, would allow evaporation and would make it possible to reach an economically feasible concentration. All means making it possible to increase the ammonia concentration of a liquid source are possible for supplying the system of the present invention.
• the treatment system 10 of a liquid source 11 of the present invention comprises a concentration module 16 of the ammonia in the liquid source.
• This concentration module 16 makes it possible to increase the ammonia concentration of the liquid source 11 so as to make this concentration sufficient for the treatment of the concentrated liquid source to be economically and industrially interesting.
• the concentration module 16 of the present invention may comprise a filtration module by ultrafiltration, by nanofiltration, by direct osmosis, by reverse osmosis, or even by electrodialysis.
• a combination of these modules can also be implemented.
• These filtration modules used for the present invention which could be interchangeably called membrane separation modules, allow in particular the separation of dissolved materials and thus the obtaining of a concentrated flow and a diluted flow, also called concentrate. /retentate and permeate respectively.
• Figure 2 represents a treatment system 20 of a liquid source comprising ammonia, and optionally phosphorus, according to the present invention.
• the treatment system of Figure 2 comprises the supply of a liquid source 11 to an extraction module 12 in the form of gaseous ammonia from the ammonia included in the liquid source 11.
• the extracted gaseous ammonia is then transferred to a conversion module 14 allowing the transformation of the extracted gaseous ammonia into dinitrogen and dihydrogen 15, the conversion module 14 being a reactor using a non-thermal plasma coupled or not to catalysis, preferably a DBD reactor.
• the treatment system 20 of a liquid source 11 of the present invention comprises a concentration module 16 for the ammonia in the liquid source, this concentration module 16 being able to be a concentration module 16. filtration by ultrafiltration, by nanofiltration, by direct osmosis, by reverse osmosis, or by electrodialysis. A combination of these modules can also be implemented.
• the treatment system 20 of a liquid source 11 also optionally comprises a purification and/or separation module 21 of the dinitrogen and dihydrogen extracted by the conversion module 14.
• such module allows the reuse of dihydrogen without dinitrogen or vice versa.
• the treatment system 20 of a liquid source 11 comprising ammonia and phosphorus according to Figure 2 can optionally comprise a first recovery module 23 of the phosphorus included in the liquid source 11 or the concentrated liquid source 11a after its concentration by the concentration module 16.
• liquid source 11 comprising ammonia and phosphorus according to the present invention can be an effluent from a water treatment plant, from an industrial or agricultural operation or any other effluent comprising ammonia and phosphorus .
• the liquid source may have undergone prior stages of transformation, fermentation or not.
• the liquid source 11 may comprise fermented urine, or aged urine (known in English under the term "lant") mixed or not with another liquid, the fermentation increasing the ammonia concentration by decomposition of the urea. .
• an ammonia concentration of at least 150 mg/l is preferred. All means making it possible to increase the phosphorus concentration of a liquid source are possible for supplying the system of the present invention.
• the concentration module 16 of the liquid source 11 can make it possible to increase the concentration of ammonia and/or phosphorus so as to achieve economically and industrially preferred concentrations.
• the treatment system 20 of a liquid source 11 comprising ammonia and phosphorus according to Figure 2 can optionally comprise a second recovery module 24 of the phosphorus included in the discharge liquid 13.
• the second recovery module 24 of phosphorus in the discharge liquid 13 allows the recovery of phosphorus in the discharge liquid 13 by precipitation or by mineral or metallic crystallization, for the formation of struvite, calcium phosphates, brushite, hydroxyapatite, or others.
• the compounds formed depend on the materials available to transform them with the phosphorus in the discharge liquid 13.
• the first phosphorus recovery module 23 allows the recovery of phosphorus in the liquid source 11 or the concentrated liquid source 11a by precipitation or by mineral or metallic crystallization, for the formation of struvite, calcium phosphates, brushite, hydroxyapatite, or others.
• the compounds formed depend on the materials available to transform them with the phosphorus in the liquid source 11 or the concentrated liquid source 11a.
• the first phosphorus recovery module 23 and/or the second phosphorus recovery module 24 make it possible to obtain elements comprising phosphorus, in particular precipitates or crystallized elements which can be reused 25 By reuse, it is understood that the product recovered comprising phosphorus, in particular a precipitate or a crystallized element, by the first recovery module 23 and/or by the second phosphorus recovery module 24 is used in other processes, for example by using the struvite formed as fertilizer for agriculture.
• the recovery of phosphorus by the first and/or the second phosphorus recovery module 23, 24 can be carried out by physicochemical treatment, consisting of the precipitation of phosphorus by adding, for example, a metallic salt or an alkaline earth salt.
• a metallic salt or an alkaline earth salt for example, ferric chloride or calcium salts such as calcium chloride can be used.
• the phosphorus in precipitated form is then extracted in a separator, the phosphorus precipitated with the metallic or alkaline earth salt being retained in the physicochemical sludge resulting from the separation.
• the extraction module 12 in the form of gaseous ammonia from the ammonia included in the liquid source 11 or in the concentrated liquid source 11 a can be configured so as to carry out stripping operations beyond a predefined ammonia concentration threshold and to stop the stripping operations if the ammonia concentration in the source liquid 11 or the concentrated liquid source 11 a is lower than this predefined concentration threshold.
• the extraction module 12 can be configured so as to carry out stripping operations beyond a residual concentration threshold. predefined amount of ammonia in the discharge liquid 13 and to stop the stripping operations if the residual ammonia concentration is below the concentration threshold. Indeed, a residual concentration of ammonia in the discharge liquid may be necessary in the case where an operator wishes to form a precipitate requiring ammonia with the second phosphorus recovery module 24. In the case where an operator wishes to form a precipitate not requiring ammonia with the second phosphorus recovery module, then it is not necessary to control the residual concentration of ammonia in the discharge liquid 13, at the outlet of the extraction module 12.
• the extraction module 12 is configured so that the residual concentration of ammonia in the discharge liquid respects a targeted objective. , making it possible to optimize phosphorus recovery with the phosphorus recovery module 24.
• the extraction module 12 in the form of gaseous ammonia from the ammonia included in the liquid source 11 can be configured so as to carry out stripping operations beyond a predefined phosphorus concentration threshold and to stop the stripping operations if the phosphorus concentration in the liquid source 11, in the liquid source 11a, or in the discharge liquid 13 is lower than this predefined concentration threshold .
• the concentrated liquid source 11a or in the discharge liquid 13 one or more sensors can be arranged at the inlet and/or or inside and/or at the outlet of the extraction module 12 so as to measure the concentration of ammonia and/or phosphorus. Such sensors can also or alternatively be arranged at the entrance and/or inside and/or at the outlet of the concentration module 16.
• Figure 2 also illustrates that the treatment system 20 of the present invention can comprise a purification and/or separation module 21 of the dinitrogen and dihydrogen 15 converted by the conversion module 14 from the ammonia extracted by the extraction module 12.
• This purification and/or separation module 21 allows in particular the reuse of dinitrogen and/or dihydrogen individually.
• Figure 2 also illustrates that the treatment system 20 of the present invention can comprise a methanation reactor 22 which receives the dihydrogen purified or separated by the purification and/or separation module 21.
• the methanation reactor typically allows the synthesis of methane (CH 4 ) from dihydrogen (H 2 ) and carbon dioxide (CO 2 ).
• Figure 3 represents a treatment system 30 of a liquid source 11 as described in Figure 2, further comprising optional reinjection means towards an anaerobic digester and a liquid/solid separation module.
• the reinjection means according to Figure 3 correspond to one or more conduits allowing transfer from the conversion means 14 and/or from the purification and/or separation module 21 to an anaerobic digester 31.
• a transfer from the conversion means 14 a mixture of dihydrogen and dinitrogen is transferred to the anaerobic digester 31.
• a transfer from the purification and/or separation means 21 it is only the purified and/or separated dihydrogen which is transferred to the anaerobic digester 31.
• Figure 3 also illustrates the possibility for the treatment system 30 of the present invention to form a complete cycle by connecting the anaerobic digester 31 to the inlet of the ammonia extraction module included in the liquid source 1 1.
• the anaerobic digester makes it possible to obtain a digester liquor anaerobic (or a digestate) of which a portion, the liquid fraction of the anaerobic digester liquor obtained after separation in a solid/liquid separation module (for example by dehydration), can serve as a liquid source 1 1.
• the anaerobic digester liquor 31 can plausibly comprise a quantity of solids that is too large to be treated directly by the processing module. extraction 12 of ammonia in gaseous form.
• a liquid/solid separation module 32 is necessary, making it possible to obtain, among other things, a liquid fraction of the anaerobic digester liquor 31.
• This module can be a solids separation module from pore water, a dehydration module, a sedimentation module, a filtration module, a centrifugation module, or even a combination of these.
• the liquid fraction of the anaerobic digester liquor 31 after treatment by the liquid/solid separation module 32 can be transferred to a concentration module 16 in order to obtain the concentrated liquid source 1 1 a.
• the first or the second recovery module phosphorus and the ammonia gas extraction module are combined in a single reactor.
• the precipitation of phosphorus can be done in the lower part of the reactor with a pH close to or below the pKa NH 4 7NH 3 , the precipitation, for example, of struvite being more effective at a higher pH, while stripping can be induced. in an upper part of the reactor, where the pH will be above the pKa.
• the single reactor comprising the stripping module and a phosphorus recovery module is configured to operate under vacuum.
• gas injections that is to say sparging (in English "gas sparging") in this single reactor can be carried out to make the phosphorus recovery and extraction operations by stripping of the phosphorus more efficient. gaseous ammonia.
• the present invention also relates to a method of treating a liquid source 1 1 comprising ammonia and optionally phosphorus.
• This processing method can be implemented using any of the processing systems previously described.
• the liquid source 11 comprising ammonia and optionally phosphorus as described above is suitable for the method of the present invention.
• the present invention thus also relates to a method of treating a liquid source 11 comprising ammonia, the method comprising a step of extracting gaseous ammonia from the ammonia included in the liquid source 11 .
• This step is preferably carried out by a stripping module, even more preferably a vacuum stripping module.
• the liquid obtained at the end of this step therefore has an ammonia concentration lower than that of the liquid source 11 before this step.
• This liquid obtained at the end of this step is called discharge liquid 13.
• the gaseous ammonia extracted by the extraction step is then converted during a step of converting the gaseous ammonia extracted into dinitrogen and dihydrogen 15.
• This step is carried out using a reactor using a non-thermal plasma coupled or not to catalysis, preferably a dielectric barrier plasma discharge reactor (DBD).
• DBD dielectric barrier plasma discharge reactor
• the use of such a reactor for the conversion of gaseous ammonia is advantageous because it eliminates the need for high heat, unlike conventional thermal cracking methods for which significant heat is necessary, this depends on the catalyst used.
• the method of the present invention can be completed when the liquid source 11 also comprises phosphorus, the method then comprising a step of recovering the phosphorus in the liquid source 11 and/or in the discharge liquid 13. This step can be carried out with a phosphorus recovery module as described in the systems of the present invention.
• the method may include receiving measurements by sensors making it possible to evaluate the ammonia and/or phosphorus concentration so as to determine whether these concentrations exceed specific thresholds for which phosphorus recovery is industrially interesting.
• these thresholds vary depending on the materials available to combine with the phosphorus and/or ammonia from the liquid source 11 or from the liquid of discharge, depending on the desired material after recovery and combination, in particular among the following materials: struvite, calcium phosphates, brushite, hydroxyapatite, or others.
• These thresholds can also vary depending on the choice of the operator, who can prioritize or not the extraction and conversion of ammonia in the liquid source 11.
• the processing system allows, to adapt the system according to an objective or one or more concentration thresholds.
• the method may also include a step of reinjection of the dihydrogen and the dinitrogen 15 obtained at the end of the conversion step, or only the dihydrogen, towards an anaerobic digester 31 or towards a methanation reactor 22.
• the method includes the purification and/or separation of dihydrogen and dinitrogen using a purification and/or separation module 21.
• the anaerobic digester 31 to which the dihydrogen or the dihydrogen and the dinitrogen 15 are reinjected can provide a liquid source comprising ammonia which can be reused for the method of the present invention.
• the liquor from the anaerobic digester 31 probably requires prior treatment in order to reduce the quantity of solids.
• This step prior to supplying the liquid source 11 comprising ammonia, for a step of extracting gaseous ammonia includes a step of liquid/solid separation and/or dehydration.
• a liquid/solid separation module 32 is necessary.
• This module can be a solids separation module from pore water, a dehydration module, a sedimentation module, a filtration module, a centrifugation module, or even a combination of these.
• the method can advantageously comprise a step of concentrating the ammonia and optionally the phosphorus included in the liquid source 11 before the step of extracting the gaseous ammonia from the ammonia included in the liquid source 11.
• This concentration step can be carried out by a filtration module by ultrafiltration, by nanofiltration, by direct osmosis, by reverse osmosis, or even by electrodialysis. A combination of these modules can also be implemented.
• the present invention also corresponds to an installation comprising a system as described above and/or implementing the method as described above.

Landscapes

• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Inorganic Chemistry (AREA)
• Engineering & Computer Science (AREA)
• Environmental & Geological Engineering (AREA)
• Water Supply & Treatment (AREA)
• Life Sciences & Earth Sciences (AREA)
• Analytical Chemistry (AREA)
• Hydrology & Water Resources (AREA)
• Health & Medical Sciences (AREA)
• General Health & Medical Sciences (AREA)
• Combustion & Propulsion (AREA)
• Physical Water Treatments (AREA)
• Physical Or Chemical Processes And Apparatus (AREA)

Applications Claiming Priority (2)

Publications (1)

Family

ID=83280212

Family Applications (1)

Country Status (3)

Families Citing this family (1)

Family Cites Families (7)

• 2022
  • 2022-07-01 FR FR2206710A patent/FR3137377A1/fr active Pending
• 2023
  • 2023-06-29 EP EP23736121.7A patent/EP4547601A1/de active Pending
  • 2023-06-29 WO PCT/EP2023/067819 patent/WO2024003249A1/fr not_active Ceased

Also Published As

Similar Documents

Legal Events