 PROCESS FOR RECYCLING RESIDUAL SOLUTIONS COMPRISING PHOSPHORUS AND DEVICE FOR SUCH A METHOD
专利摘要:
The invention relates to a method and device for the purification of phosphoric acid contained in a waste solution comprising undesirable volatilizable materials. The waste solution is mixed with a solution of enriched phosphoric acid and is sprayed into a flame of a combustion chamber to form a purified phosphoric acid P3 combustion solution of undesirable volatilizable materials. The combustion gases from the combustion chamber are contacted with a feed solution in a gas-acid contactor to increase the temperature and concentration of P2O5 and thereby form the enriched phosphoric acid solution. Part of this solution is conducted at a flow Qp in the combustion chamber. The remainder of the solution is conducted in a recirculation loop to be reintroduced into the gas-acid contactor at a flow rate Q2. The ratio of flows, Qp / (Qp + Q2) is controlled to a predefined value. 公开号:BE1026163B1 申请号:E2018/5916 申请日:2018-12-20 公开日:2019-10-29 发明作者:Bernard Heptia；Damien Gabriel；Denis Leruth；Carl Szöcs 申请人:Prayon； IPC主号:
专利说明:
METHOD FOR RECYCLING RESIDUAL SOLUTIONS COMPRISING PHOSPHORUS AND DEVICE FOR SUCH A PROCESS FIELD OF THE INVENTION The present invention relates to a process and to a device for purifying residual solutions of phosphoric acid originating for example from industrial or agricultural processes and comprising phosphorus in the form of species of orthophosphate type. and / or polyphosphate _ as well as undesirable volatilizable materials which make their subsequent use difficult, if not impossible. The process of the present invention is particularly effective and makes it possible to clean the residual phosphoric acid solutions from their undesirable volatilizable materials and, if necessary, to produce phosphoric acid solutions at high concentrations while limiting the necessary energy consumption. the production of purified phosphoric or polyphosphoric acid solutions. The present invention allows better management of the combustion gases produced by the process before their discharge into the atmosphere. TECHNOLOGICAL BACKGROUND Many industrial or agro-industrial processes generate aqueous residual solutions comprising phosphorus. These solutions are qualified as waste because they cannot be used without prior treatment in these same industries. The phosphorus in these solutions can be present in the form of species of orthophosphate type or of polyphosphate type depending on the P2O5 content of these solutions. Because of the presence in these solutions of undesirable volatilizable materials such as fluorine, sulfur, carbon, etc., these residual solutions cannot generally be recycled in processes for the production of materials with higher added value, such as as solutions of purified phosphoric acid or polyphosphoric acid (= PPA), nor in the production of phosphate salts. For this reason, these volatilizable materials are described below as “undesirable volatilizable materials. To date, these high potential residual solutions are treated as simple waste with very low value and high polluting power. Polyphosphoric acid (= PPA) is a viscous liquid which can be produced in particular from phosphoric acid in the form of a solution comprising PCM 3- ions. PPA has the general formula HO [P (OH) (O) O] n H, with n> 1. When n = 2 PPA is commonly called pyrophosphoric acid; when n = 3, we speak of tripolyphosphoric acid. For n> 3, we simply speak of polyphosphoric acid, regardless of the value of n. PPA can be produced by dehydration and polycondensation of orthophosphoric acid, H3PO4, according to equation (1). An aqueous solution of polyphosphoric acid is thus obtained, the distribution of molecular species of which depends inter alia on the polycondensation temperature, Tpc. BE2018 / 5916 (1) P— OH + n-1 H 2 O OO IIII HO —P — OH + n-1 HO— P - OHHO OHOH [0004] Polyphosphoric acid is most often in the form of linear chains. Cyclic forms of metaphosphoric or branched type may however also exist. As illustrated in Figure 1, the polycondensation temperature determines the equivalent phosphoric acid concentration in P2O5 units at equilibrium in the liquid state (Figure 1 (a)) and the latter determines the distribution of molecular species (ie, the distribution of phosphoric acid in different forms of different value n (Figure 1 (c)), so an aqueous solution of phosphoric acid with equivalent concentration in P2O5 units of less than about 61% will be made up mostly of H3PO4 molecules. When the equivalent concentration in P2O5 units increases, this indicates that the solution includes more and more polymerized molecules, with the value of n increasing with the concentration in P2P equivalents> 5 as indicated in Figure 1 (c). The dehydration and polycondensation of a solution of phosphoric acid to polyphosphoric acid requires an evaporation of water molecules which requires the supply of heat energy. Patent EP2411325 B1 reviews a certain number of known processes for the production of polyphosphoric acid and describes a new wet process compared to the reviewed processes which make it possible to benefit from high energy efficiency, to drastically limit the impact. environmental. This patent describes a device resistant to very severe operating conditions for the production of polyphosphoric acid, making it possible to limit maintenance costs and to establish equipment durability and finally to ensure the production of a quality polyphosphoric acid without contamination during the manufacturing process. It would be interesting to produce a material with high added value such as purified phosphoric acid or polyphosphoric acid from low value residual solutions. However, the use of such residual solutions in a process for the production of purified phosphoric acid or of PPA as described in EP2411325 B1 is impossible because of the presence of undesirable volatilizable compounds in such solutions. JP2000178014 describes a process for recovering phosphoric acid from recovery solutions, in which a recovery solution comprising phosphorus molecules is incinerated at a temperature of 900 to 1000 ° C. The combustion gases containing phosphorus molecules are cooled in a cooler and the phosphorus molecules are recovered as phosphoric acid. The present invention provides a more efficient process than that described in JP2000178014 for the production of purified phosphoric acid or PPA from residual solutions comprising phosphorus from generally industrial processes and which, until BE2018 / 5916 days are simply treated as waste. The present invention and its advantages are described in more detail in the following sections. SUMMARY OF THE INVENTION The present invention is described in the attached independent claims. Preferred variants are defined in the dependent claims. In particular, the present invention relates to a process for the purification of an aqueous residual solution comprising phosphorus molecules and undesirable volatilizable materials comprising the following steps: (a) introducing into a gas-acid contactor, a feed stream (F0) of a feed solution PO which is aqueous and comprising phosphorus molecules preferably in the form of species of orthophosphate type at a mass concentration, xpO, between 0 and 54% equivalent in P2O5 units, (b) introduce into the gas-acid contactor a recirculation flow (F2) of recirculated enriched phosphoric acid solution (P2), (c) introduce into the contactor gas-acid from combustion gases (G1); (d) contact the feed (F0) and recirculation (F2) and combustion gas (G1) flows to form, in the gas-acid contactor, on the one hand, • an enriched phosphoric acid solution (P1 ) comprising a mass concentration, xp1, of P2O5 content which is greater than xpO (xp1> xpO) and, on the other hand, • the contacted combustion gases (G3), (e) separating the contacted combustion gases (G3) of the enriched phosphoric acid solution (P1), then • remove the contacted combustion gases (G3) from the gas-acid contactor, and • remove the enriched phosphoric acid solution (P1) from the gas-acid contactor (1) , (f) forming from said enriched phosphoric acid solution (P1), on the one hand, • a recirculation flow (F2) of recirculated enriched phosphoric acid solution (P2) to introduce it into the contactor gas-acid (1) as defined in step (b) and, on the other hand, • a spray flow (Fp) of the phos acid solution enriched phoric (P1) to introduce it into a combustion chamber, (g) spraying through a burning flame in the upper part of the combustion chamber a mixture flow (Fm) of a mixture solution (Pm) comprising phosphorus at a mass concentration, xpm, and undesirable volatilizable materials, the mixture flow being formed by, on the one hand, • the enriched phosphoric acid solution (P1) and optionally, on the other hand, • a flux residue (Fr) of an aqueous residual solution (Pr) comprising a mass concentration, xpr, of at least 1% P2O5, for: evaporate water and thus concentrate the mixing solution (Pm), BE2018 / 5916 • optionally oxidize and in all cases evaporate the undesirable volatilizable impurities, • form combustion gases (G1), and • form a combustion solution (P3) having, by mass concentration, xp3 in P2O5 greater than the concentration of the residual solution (Pr), and a content of volatilizable impurities lower than that of the residual solution (Pr), (h) separating the combustion solution (P3) from the combustion gases (G1) and • recovering the combustion solution (P3), and • transfer the combustion gases (G1) to the gas-acid contactor (1) as defined in step (c). The feed solution (F0) can comprise a concentration xpO of between 0.1 and 50%, preferably from 1 to 35%, preferably from 5 to 20% P2O5. In some cases, the feed solution may also include undesirable volatilizable materials, but this is not essential in the case where a residual solution Pr comprising undesirable volatilizable materials is added to the combustion chamber, as explained more low. The flow rate, Q0, of the supply solution (F0) in the contactor expressed per unit of nominal power [MW 1 ] of the combustion chamber is preferably between 100 and 3000 kg / (h MW), preferably between 500 and 2500 kg / (h MW). The enriched phosphoric acid solution (P1) is identical to the recirculated enriched phosphoric acid solution (P2) and comprises a concentration xp1 of phosphorus preferably greater than or equal to 1%, preferably less than 60%, more preferably between 5 and 50%, preferably between 10 and 40% P2O5. The total flow rate, Q1 = (Qp + Q2), of the solution (P1) out of the contactor expressed per unit of nominal power [MW 1 ] of the combustion chamber is preferably between 600 and 123,000 kg / (h MW) , preferably between 1000 and 50,000 kg / (h MW). The ratio, Qp / (Qp + Q2), between the mass flow rate (Qp) of the spray flow (Fp) and the total mass flow rate (Qp + Q2) is preferably less than 50%, preferably less than 10%, preferably less than 5%, more preferably less than 2.5% and in which the ratio Qp / (Qp + Q2) is greater than 0.1%, preferably greater than 0.5%. The residual solution (Pr) may comprise a concentration xpr of phosphorus greater than or equal to 2%, preferably at least 5%, more preferably at least 10%, preferably at least 20% P2O5. The residual solution (Pr) comprises a concentration xpv of undesirable volatilizable materials of at least 5 ppm, preferably of at least 10 ppm, preferably of at least 100 ppm, preferably of at least 1%, preferably at least 5%, preferably at least 10%, more preferably at least 25% by weight relative to the total weight of the solution. The flow rate (Qr) of the residual solution (Pr) in the combustion chamber expressed per unit of nominal power [MW 1 ] of the combustion chamber is preferably non-zero and preferably between 5 and BE2018 / 5916 1500 kg I (h MW), preferably between 400 and 1000 kg / (h MW). If the flow rate (Qr) of the residual solution (Pr) in the combustion chamber is zero, then the feed solution (PO) must include a non-zero concentration xpv of undesirable volatilizable materials, for example at least 5 ppm, preferably at least 10 ppm, preferably at least 100 ppm, preferably at least 1%, preferably at least 5%, preferably at least 10%, more preferably at least 25% by weight relative to the total weight of the solution. The Qr / (Qr + Q0) ratio can be between 0 and 99%, preferably between 5 and 90%, more preferably between 10 and 80%, or even between 15 and 45%. The mixture flow (Fm) can comprise a phosphorus concentration (xpm), preferably greater than 1% P2O5 (xpm> 1% P2O5,) and comprises undesirable volatile materials, originating from the residual solution Pr and / or the PO feed solution. In this document, the flow rates Q0, Qp and Qr are mass flows of the feed solutions (PO), enriched phosphoric acid (P1) and residues (Pr), respectively. The mixing solution (Pm) may comprise a concentration xpm greater than 2%, preferably greater than 5%, more preferably greater than 20%, more preferably greater than 30%, preferably greater than 40%, and more preferably between 45 and 60% P2O5. The mixing solution (Pm) may comprise a concentration xpv of undesirable volatilizable materials preferably of at least 5 ppm, preferably of at least 10 ppm, preferably of at least 100 ppm, preferably of at least 1 %, preferably at least 5%, preferably at least 10%, more preferably at least 25% by weight relative to the total weight of the solution. The flow rate (Qm) of the mixing solution (Pm) in the combustion chamber expressed per unit of nominal power [MW-1] of the combustion chamber is preferably between 305 and 3000 kg / (h MW), of preferably between 200 and 2000 kg / (h MW). The combustion solution (P3) can comprise a phosphorus concentration xp3 greater than 1% equivalent in units of P2O5, preferably greater than 10%, preferably greater than 25%, particularly preferably greater than 40%, or is preferably between 30 and 76%. The flow rate (Q3) of the combustion solution (P3) out of the combustion chamber expressed per unit of nominal power [MW-1] of the combustion chamber is preferably between 240 and 1500 kg / (h MW), preferably between 600 and 3000 kg / (h MW). The feed (F0) and recirculation (F2) flows can either be mixed before their introduction into the gas-acid contactor to form a flow of a mixture of the feed solution (PO) and the solution d recirculated enriched phosphoric acid (P2), or contacted after having been introduced separately into the gas-acid contactor to form a flow of a mixture of the feed solution (F0) and the recirculated enriched phosphoric acid solution ( P2). It is preferable that the residual flow (Qr) of the residual solution (Pr) is non-zero. The residual (Fr) and spray (Fp) flows can then either be mixed to form the mixture flow (Fm) before being sprayed into the flame in the combustion chamber, or sprayed BE2018 / 5916 separately in the combustion chamber to form the mixture flow (Fm) in the flame or just before reaching the flame. The residual solution (Pr) and, optionally, the feed solution (PO) and therefore the spray solution (Pp), comprise undesirable volatilizable materials. It is also possible that only the spraying solution (Pp) comprises undesirable volatilizable materials, for example in the case of a flow Qr = 0, It is however preferred that the residual flow (Qr) is non-zero. The contact between the feed (F0) and recirculation (F2) flows and the combustion gases (G1) in step (d) can be carried out co-current or against the current, from preferably co-current by flowing from an upper part to a lower part of the gas-acid contactor. During the contact step (d), the ratio (Qg1 / (Q0 + Q2)) between a mass flow (Qg1) of the combustion gas (G1) introduced into the gas-acid contactor and a total mass flow ( Q0 + Q2) of the contact (F0) and recirculation (F2) supply flows introduced into the gas-acid contactor, is preferably between 0.1 and 50%, preferably between 0.5 and 10%, more preferably between 1 and 7%. The present invention also relates to a device for producing purified phosphoric acid (P3) according to a method according to any one of the preceding claims, comprising: (A) a combustion chamber having: • a spray inlet into the combustion chamber allowing the introduction at a flow rate of an enriched phosphoric acid solution (P1) in spray form in a combustion unit, • a residue inlet into the combustion chamber or in upstream of the spray inlet allowing the introduction of a residual solution (Pr) or of a mixture of residual solutions (Pr) and enriched phosphoric acid (P1) in spray form in a combustion unit, • l the combustion unit being arranged in the upper part of the combustion chamber, and being capable of forming a flame having a temperature of at least 1500 ° C by combustion of a fuel, said combustion unit comprising: oun burner, odes fluid connections between the burner and, on the one hand, a source of oxygen and, on the other hand, a source of fuel making it possible to supply the flame, • a combustion outlet of the combustion chamber for recovering a combustion solution (P3) in the liquid phase, and arranged downstream of the combustion unit which is itself arranged downstream of the spray and residue inlet, • a combustion gas discharge outlet (G1) coming from the flame (B) a gas-acid contactor having • a supply inlet connected to a source of a supply solution (F0), allowing introduction to a contact supply flow ( Q0) of a feed solution (F0), BE2018 / 5916 • a combustion gas inlet allowing the introduction into the gas-acid contactor of the combustion gases (G1) at a flow rate (Qg1), • a recirculation inlet identical or different from the supply inlet of contact, allowing the introduction of a recirculated enriched phosphoric acid solution (P2) at a recirculation rate (Q2), • the supply and / or recirculation inlets and the gas inlet (1gu) being arranged to allow, on the one hand, a contact between the feed flow FO and recirculation flow F2 to form a flow of a mixture of the feed solution (FO) and the recirculated enriched phosphoric acid solution P2 and, on the other hand, contact of the mixture thus formed with the combustion gases (G1), • one or more outlets of enriched phosphoric acid, (C) a first fluidic spray connection connecting an upstream end coupled • to the ph acid outlet enriched phosphoric acid gas contactor or • at a branch point with a first fluid connection (3) which is coupled to the enriched phosphoric acid outlet, (D) a first spray fluid connection connecting an upstream end (3u) coupled • to the enriched phosphoric acid outlet of the acid gas contactor (1) or • to a branch point with a first fluid connection (3) which is coupled to the enriched phosphoric acid outlet, at a coupled downstream end at the entry of enriched phosphoric acid (2pu) into the combustion chamber, Characterized in that the device further comprises (E) a recirculation fluid connection connecting a coupled upstream end, • to an outlet of recirculated enriched phosphoric acid (1 pd) from the gas-acid contactor or • to a branch point with the first fluid connection, at a coupled downstream end, • at the recirculation inlet of the gas-acid contactor or • at a supply connection supplying the gas-acid contactor with supply solution (FO), and (F ) means for controlling and maintaining a ratio, Qp / (Qp + Q2), between a spray mass flow rate (Qp) flowing in the spray fluid connection (3p) and a defined total mass flow rate (Qp + Q2) as the sum of the mass spray flow (Qp) and a mass recirculation flow (Q2) flowing in the recirculation fluid connection at a value less than 50%, preferably less than 10%, preferably in less than 5%, more preferably less than 2.5% and in which the ratio Qp / (Qp + Q2) has a value greater than 0.1%, preferably greater than 0.5%. The residue inlet is preferably in fluid communication with a source of a BE2018 / 5916 residual solution (Pr) which is aqueous and comprises phosphorus molecules in orthophosphate and / or polyphosphate form and undesirable volatilizable materials. BRIEF DESCRIPTION OF THE FIGURES. Different aspects of the present invention are illustrated in the following Figures. Figure 1: graphically illustrates the relationship between the boiling temperature and the P2O5 concentration at equilibrium of the liquid phase (part (a)) and the vapor phase (part (b)), as well as the relationship between the P2O5 concentration and the weight distribution of the phosphoric acid molecules according to the different values of n (part (c)). Figure 2: illustrates a variant device according to the present invention. Figure 3: reports values of a selection of parameters illustrative of the method according to the present invention. Figure 4: illustrates a variant device according to the present invention. Figure 5: illustrates a variant device according to the present invention. DETAILED DESCRIPTION OF THE INVENTION Figures 2 to 5 illustrate the method and non-exhaustive variants of devices for implementing said method. In the following, the term "flow" represented by the letter "F" is used in its commonly accepted interpretation of simply a flow of a fluid. Only Figure 3 indicates the flows with the letter "F". The other Figures illustrating devices indicate flow rates "Q" corresponding to the flows "F" in Figure 3. The term "flow rate" represented by the letter "Q" characterizes the mass of the flow per unit of time and is expressed in [kg / s] or [kg / h]). The term "flow", even used alone, therefore defines a mass flow. In order to express the flow rates as a function of the nominal power of the combustion chamber, the mass flow rates of the different flows are expressed below in units of [kg / (h MW)], which represents a flow rate per unit of nominal power. [MW 1 ] from the combustion chamber. As the combustion solution, P3, resulting from the combustion of the mixing solution, Pm, obtained at the end of the process of the present invention can comprise purified phosphoric acid alone or in admixture with polymerized molecules whose respective concentrations vary according to the temperature and the concentration of P2O5 of the mixture solution Pm contacting the flame of the combustion chamber (cf. FIG. 1), which itself depends inter alia on the concentration in the residual solution, Pr, used, reference will be made in the remainder of the document to the solution P3 obtained by the expression "solution of purified phosphoric acid", even if it is clear that this solution can also include polymerized molecules and therefore PPA. It is also obvious that the level of purity of the P3 solution will depend on the applications for which this purified acid is intended and that the presence of certain ions will not always be contraindicated in certain BE2018 / 5916 applications. Conventions and Definitions Unless otherwise stated in this patent, the term concentration is used to express mass concentrations (percentages by weight, w / 0). To define the content of the species which concerns us mainly, when we speak of the concentration of solutions of phosphoric acid or others, we must hear the content by weight expressed in units of P2O5 equivalents, which we will write "% eq . P2O5 "or"% P2O5 ". With regard to gas flows, such as for example combustion gases, where several species of interest can coexist depending on the operating conditions, in gaseous or liquid form (for example by entrainment of droplets), or even possibly solid (fumes) , the concentration in these flows is also expressed in P2O5 equivalent units (by weight, w / 0). The ionic dissociation of the species that interest us is not considered in this text. For information, the concentration of a phosphoric acid solution can also sometimes be expressed in units of H3PO4 equivalents. The correspondence between the two concentration units is defined by the relation: 1 eq. P2O5 = 0.7245 eq. H3PO4. It is understood in this text by the expressions “Phosphoric acid solution”, an aqueous solution comprising HO [P (OH) (O) O] n H, with n> 1 “Orthophosphoric acid”, an aqueous solution comprising very mainly HO [P (OH) (O) O] nH, with n = 1, that is to say an aqueous solution of phosphoric acid containing less than 61% by weight of P2O5; "Polyphosphoric acid solution" (= PPA), an aqueous solution mainly comprising HO [P (OH) (O) O] n H, with n>1; that is to say an aqueous solution of phosphoric acid containing more than 76% by weight of P2O5; "Polycondensation of phosphoric or orthophosphoric acid" means the polycondensation of the molecules considered as represented by equations (1) and / or (2) in continuation. "Aqueous solution comprising phosphorus", a solution containing phosphorus dissolved in the form of species of orthophosphate or polyphosphates type. Depending on the P2O5 content of these solutions, the ortho or polyphosphate species can be present as shown in Figure 1 (c). These species can be present in the form of ions. Process - gas-acid contacts The process of the present invention comprises the introduction into a gas-acid contactor (1) of the following flows. • A feed stream, F0, feed solution, PO, from the contactor to a feed rate, Q0. The feed solution, PO, is an aqueous solution preferably comprising phosphorus, preferably in the form of species of orthophosphate type (cf. BE2018 / 5916 Figure 1) at a mass concentration, xpO, between 0 and 54%, preferably from 0.1 to 50%, more preferably from 1 to 35%, preferably from 5 to 20% P2O5. The feed solution, FO, makes it possible to return to the combustion chamber the species containing phosphorus which would have left it with the combustion gases G1. In a variant of the present invention, the solution, PO, does not include phosphorus - (xpO = 0) and can be water. The PO solution may contain compounds which can react with undesirable volatilizable substances, to destroy them, for example, hydrogen peroxide, chlorate or nitrate ions. These compounds can for example react with dissolved carbonaceous materials to form carbon dioxide (CO2) which is easily volatilizable. In an alternative variant of the present invention, the solution, PO, is a source of phosphorus and comprises P2O5. For example, the PO contact feed solution can comprise a phosphorus xpO concentration of 5 to 54%, preferably less than 45%, more preferably between 10 and 35% P2O5. Higher concentrations of the feed solution do not interfere with the process, and can increase the phosphorus concentration xpm of the mixture solution, Pm, reaching the flame in the combustion chamber. The P2O5 content in the purified phosphoric acid solution, P3, at the end of the process can thus be varied. The flow rate, Q0, of the solution, PO, in the contactor expressed per unit of nominal power [MW -1 ] of the combustion chamber is preferably between 100 and 3000 kg / (h MW), preferably between 500 and 2500 kg / (h MW), or between 1000 and 2000 kg / (h MW). In a variant of the present invention, the PO solution comprises undesirable volatilizable materials such as typically carbon, fluorine, chlorine, sulfur, nitrogen in soluble form (ionic or not). For example, they can be present in the PO solution in xpv concentrations of undesirable volatilizable matter of at least 5 ppm (parts per million), or at least 10 ppm, preferably at least 100 ppm. Preferably, the concentration xpv of undesirable volatilizable materials is less than 5%, preferably less than 2% by weight of total organic carbon relative to the total weight of the solution. For example, the PO solution can comprise at least 10 ppm of fluorine, or at least 100 ppm of fluorine, at least 1% of fluorine. Depending on the applications, such solutions cannot be used as such. If the PO solution does not contain undesirable volatilizable materials, then a recirculation solution (Pr) containing such undesirable volatilizable materials is added to the combustion chamber in order to produce a mixing solution comprising undesirable volatilizable materials in the concentrations indicated above. To avoid excessive deposition of dirt in the gas-acid contactor, it is preferable that most or all of the undesirable volatilizable materials be introduced directly into the combustion chamber, contained in the residual solution Pr. BE2018 / 5916 • A recirculation flow F2 of recirculated enriched phosphoric acid solution, P2, which will be defined in detail below. The flow rate of the recirculated enriched phosphoric acid solution, P2, in the contactor expressed per unit of nominal power [MW 1 ] of the combustion chamber can be between 300 and 120,000 kg / (h MW), preferably between 600 and 100,000 kg / (h MW), preferably greater than 9,000 kg / (h MW), preferably between 1,500 and 80,000 kg / (h MW). The recirculation flow F2 of recirculated enriched phosphoric acid solution P2 is the result of bringing a mixture of the feed streams, F0, and recirculation F2 of recirculated enriched phosphoric acid solution, P2, d '' a previous cycle with a flow of combustion gases, G1. • A flow of combustion gases G1 which are formed during the combustion of a mixture flow, Fm, of a mixture solution, Pm, comprising phosphorus at a mass concentration, xpm, greater than that of the flow of contact supply, F0 in a combustion chamber which will be described and discussed in detail below. The combustion gas flow G1 comprises phosphorus molecules in the form of droplets or vapors, carried from the combustion chamber to the gas-acid contactor. For example, the flow of combustion gas G1 can comprise between 0.1 and 15% P2O5, for example between 0.5 and 13%, or even between 1 and 10% P2O5, preferably between 2 and 5% P2O5. In addition, the combustion gases include undesirable volatilized materials which result from the combustion of the mixture solution Pm. The feed flow F0 and the recirculation F2 and the combustion gases G1 are therefore brought into contact with each other in the gas-acid contactor (we therefore speak of a direct gas-acid contactor) to form, d on the one hand, a solution of enriched phosphoric acid P1 and, on the other hand, contacted combustion gases G3. In a preferred variant, illustrated in Figures 2 & 4, the feed flow F0 and recirculation, F2, are mixed before their introduction into the gas-acid contactor to form a flow of a mixture of the solution of PO supply, contactor and recirculated enriched phosphoric acid solution, P2. For this, it suffices to connect a recirculation conduit (3r) carrying the flow F2 and a supply conduit (3a) conveying the flow F0 upstream of an inlet (1 pu) of the gas-acid contactor (1). The pressures in the recirculation (3r) and supply (3a) pipes must be controlled in order to avoid backflow of liquid in one of the two branched pipes. Figure 2 shows a supply line (3a) connected to the recirculation line (3r), while Figure 4 illustrates a recirculation line (3r) connected to a supply line (3a). In both configurations, the combustion gases, G1, are then brought into contact with the solution flow mixture (F0 + F2) thus formed, after its introduction into the gas-acid contactor (1). In an alternative variant, illustrated in Figures 3 & 5, the feed flow F0 and recirculation F2 are contacted after having been introduced separately into the gas-acid contactor to form a flow of a mixture of the feed solution PO of contactor and acid solution BE2018 / 5916 enriched phosphoric recirculated P2. The phosphoric acid flows FO and F2 and combustion gases G1 are thus all brought into contact in the gas-acid contactor. It suffices to provide in the gas-acid contactor an inlet (1pu) for feed flow FO separated from an inlet (1pru) for recirculation flow F2. The contact between the feed flows F0 and the recirculation F2 or their mixture (F0 + F2) and the combustion gases G1 in the gas-acid contactor can be made by flow contact at co-current or at against the current. In particular, the liquid phases flow downward in the direction of gravity, and the gas phase rises upward. In a preferred variant, the two or three flows flow co-current from an upper part to a lower part of the gas-acid contactor. In the context of the present invention, the terms "higher" and "lower" are understood according to the direction of the forces of Earth's gravity which extend towards the Earth's center of gravity. Thus, in the absence of pressure gradients, a liquid naturally flows from the upper part of a reactor to its lower part which is downstream of the upper part in the direction of Earth's gravity. It is possible to contact the combustion gases G1 with the feed and recirculation flows of phosphoric acid, F0 & F2, or their mixture (F0 + F2) by guiding the combustion gases in a flow transverse to those of phosphoric acids. Contacting according to co-current flows is however preferred. The contact between the feed flows F0 and recirculation F2 or their mixture (F0 + F2) and the combustion gases G1 forms a solution of enriched phosphoric acid, P1, and contacted combustion gases, G3. This contact can be made by percolating the flows through a filling material which resists the operating conditions. During the contact between combustion gases G1 and the feed flows F0 and recirculation F2, exchanges occur. On the one hand, the phosphorus molecules transported by the combustion gases in the form of droplets and vapor are carried away by the flows F0 and F2, allowing the formation of the enriched phosphoric acid solution, P1, having a higher P2O5 content. to those of each of the flows F0 and F2. On the other hand, a heat exchange takes place between the hot combustion gases, at a temperature Tg1 between 200 to 600 ° C, to the aqueous solutions of the flows F0 and F2 which are at lower temperatures, as indicated in Figure 3. The gases contacted G3 are therefore at a temperature Tg3 <Tg1 facilitating their subsequent treatments with a view to their evacuation into the atmosphere. At the same time, the enriched phosphoric acid solution, P1, is thus at a temperature, T1, higher than that of the mixture of solutions PO and P2; T1 is higher than the temperature T0 of the feed solution PO (which can be of the order of 20 to 200 ° C) and is substantially equal to the temperature T2 of the recirculated enriched phosphoric acid solution, P2, since 'it is the same solution at two ends of the recirculation loop (3r). The enriched phosphoric acid solution P1 and the contacted combustion gases G3 formed following contacting the feed and recirculation flows of phosphoric acid, F0 & F2, with the combustion gases G1 are then separated by well-known means of separation BE2018 / 5916 of the trade, such as a centrifugal or gravity separator, a coalescer, a demister, a mattress, baffles, etc. The contacted combustion gases G3 are then evacuated from the gas-acid contactor (1) at a temperature substantially lower than that of the contacted combustion gases G3 introduced into said gas-acid contactor for subsequent treatments. As the major part of the phosphorus molecules contained in the flow of combustion gases, G1, are transferred in the flow, F1, of enriched phosphoric acid solution P1 during the contact of the flow G1 with the flows FO and F2, the flow of contacted gases, G3, is much poorer in P2O5 than the combustion gas flow, G1, with contents which can be less than 1% P2O5. The contacted combustion gases G3 containing the undesirable volatilized materials can also be washed after they leave the gas-acid contactor, with an aqueous washing solution in order to dissolve and eliminate, before releasing the gases into the atmosphere, undesirable compounds such as for example fluorinated or chlorinated compounds, SO3, etc. Other treatments of the contacted combustion gases G3 are possible, including for example the condensation of gases in an indirect condenser. The enriched phosphoric acid solution P1 also left the gas-acid contactor, separately from the combustion gases contacted G3. Process F1 and flow division Fp and F2 The enriched phosphoric acid solution P1 can comprise a concentration xp1 in P2O5 units greater than or equal to 1%, preferably less than 60%, more preferably between 5 and 50%, preferably between 10 and 40% P2O5. The P2O5 concentration of the enriched phosphoric acid solution P1 naturally depends on the P2O5 concentration of the feed solution, PO, and the flow of combustion gases, G1. As discussed below, the phosphorus concentration of the P1 enriched phosphoric acid solution is generally higher than that of the feed solution, PO. Before, during or after its evacuation from the gas-acid contactor, the enriched phosphoric acid solution P1 is divided into two distinct streams: • a recirculation flow F2 of enriched recirculated phosphoric acid solution P2 to introduce it into the gas-acid contactor (1) through a recirculation loop (3r) to bring it into contact with the feed flow F0 and the combustion gases G1 as described above, and • a spray flow Fp of a spray solution Pp to introduce it into a combustion chamber (2), The spray solution Pp and the solution of recirculated enriched phosphoric acid P2 are identical in composition to each other and identical to the enriched phosphoric acid solution P1 (P1 = Pp = P2) since they have not undergone any alteration between the time of their formation in the gas-acid contactor and the division into two separate flows of recirculation F2 and of spraying Fp. The temperatures, Tp, T2, of the solutions Pp and P2 are also substantially identical to the temperature BE2018 / 5916 T1 of solution P1 which can be of the order of 100 to 300 ° C. The solutions Pp and P2 preferably comprise, in steady state, a higher concentration of P2O5 than that of the supply solution PO of the contactor. For example, the Pp and P2 solutions can comprise phosphorus concentrations of between 1 and 60%, preferably between 5 and 50% P2O5, preferably between 10 and 40% P2O5. There are two main reasons for this. First, bringing the feed and recirculation flows of phosphoric acid into contact with the combustion gases G1 which are at a higher temperature Tg1 of the order of 300 to 600 ° C. (cf. FIG. 3 ), causes the evaporation of part of the water contained in the aqueous phase of the PO and P2 solutions, which de facto increases the P2O5 concentration of the P1, Pp and P2 solutions. Secondly, as we will discuss below, the combustion gases G1 formed during the combustion of the mixture flow, Fm, of the mixture solution Pm in the combustion chamber include droplets or vapors of phosphoric acid. The combustion gases G1 can comprise between 0.1 and 15% P2O5, preferably between 0.5 and 13%, preferably between 1 and 10%, preferably between 2 and 5%, (cf. Figure 3). Upon contact with the feed streams of PO solution and recirculated enriched phosphoric acid P2, most of these molecules are transferred from the combustion gases to the mixture of acid solution (P0 + P2). After contact, the combustion gases contacted G3 contain much fewer P2O5 molecules than the gas G1 before contact, in general less than 1%; preferably less than 0.5%, advantageously less than 0.1% by weight (see Figure 3). By this transfer of P2O5 molecules to the acid mixture, the P2O5 concentration thereof increases. In a variant of the invention, the enriched phosphoric acid solution P1 is divided into two spray flows Fp and recirculation F2 at the outlet of the gas-acid contactor in a spray fluid connection (3p) and in a recirculation fluid connection (3r), respectively, as illustrated in Figure 2. Each of the fluid connections (3p) and (3r) is equipped with a pumping system (4, 4r) to ensure the flow rates and a spray flow Fp at a spray flow Qp to a combustion chamber (2) and to drive the recirculation flow F2 at a flow Q2 to the gas-acid contactor thus forming a recirculation loop. In an alternative variant, the enriched phosphoric acid solution P1 is taken out of the gas-acid contactor in a first fluid connection (3) which is common and divides in two at a branch point (5) in " T "or" Y "with, on the one hand, the spraying fluid connection (3p) which drives the spraying flow Fp at a flow rate Qp, to a combustion chamber (2) and, on the other hand a connection recirculation fluid (3r) which drives the recirculation flow F2 at a rate Q2 to the gas-acid contactor, thus forming a recirculation loop. Different variants of this configuration including a branch point (5) are illustrated in Figures 3 to 5. The spraying rates Qp and recirculation Q2 can be ensured by one or more valves (see Figure 3 and 4), by pumps (4, 4r) on each of the branches of the branch point (5) (see Figure 5) and / or by sections of spraying conduits (3p) and BE2018 / 5916 recirculation (3r) sized to obtain the desired flow rates or other well-known means used industrially to distribute a flow between 2 supplies (for example, T-shaped, Y-shaped pipes with sets of regulated valves). The enriched phosphoric acid solution P1 leaves the contactor at a total flow rate, Q1 = (Qp + Q2). The total flow rate Q1 expressed per unit of nominal power [MW 1 ] of the combustion chamber is preferably between 600 and 123,000 kg / (h MW) or between 1,000 and 120,000 kg / (h MW), preferably between 12,000 and 100,000 kg / (h MW). As discussed above, the flow F1 of enriched phosphoric acid (P1) is divided into two flows Fp and F2 each having a spray flow rate Qp and a recirculation flow Q2. The division into two flows can be done before the exit of the gas-acid contactor, at the exit of this one, or after the exit. The spraying Qp and recirculation Q2 flow rates must be determined as a function inter alia of the capacity of the combustion chamber and of the gas-acid contactor, of the temperature of the combustion gases G1 and their P2O5 content. In a stationary state of production, the ratio, Qp / (Qp + Q2), between the mass flow Qp of the spray flow Fp and the total mass flow (Qp + Q2) of the flow of enriched phosphoric acid F1, (which is in fact the sum of the spraying rates Qp and of recirculation Q2) is preferably less than 50%, preferably less than 20% and more preferably less than 10%. In a preferred variant of the invention, the ratio Qp / (Qp + Q2) is less than 5%, preferably less than 4%, more preferably less than 2.5% and even less than 2%. The ratio Qp / (Qp + Q2) is preferably greater than 0.1%, or even greater than 0.2% and preferably greater than 0.5%. Increasing the flow rate Q2 relative to the flow rate Qp makes it possible, on the one hand, to cool the combustion gases G1 to a lower temperature, which is necessary before their evacuation and, on the other hand, to further enrich the content of P2O5 of the Pp-enriched phosphoric acid solution. The ratio, Q2 / (Qp + Q2), between the mass flow Q2 of the recirculation flow F2 and the total mass flow (Qp + Q2), is of course the complement of the ratio Qp / (Qp + Q2), the sum of which is 100%. The recirculation rate Q2 is therefore preferably greater than or equal to the spraying rate Qp and, in certain preferred variants, is considerably greater than Qp with a flow rate ratio, Qp / Q2, which can range from 0.1 / 99.9 to 49/51 ( = 0.1 to 96%). Preferably, the flow rate ratio Qp / Q2 is between 1/99 and 5/95 (= 1 to 5.3%). As discussed above, the flow rate, Q2, of the recirculated enriched phosphoric acid solution, P2, in the contactor expressed per unit of nominal power [MW 1 ] of the combustion chamber can be between 300 and 120,000 kg / (h MW), preferably between 600 and 110,000 kg / (h MW), preferably between 9000 and 100,000 kg / (h MW). Thus, the flow rate, Qp, of the spraying solution, Pp, flowing to the combustion chamber expressed per unit of nominal power [MW 1 ] of the combustion chamber can be between 300 and 3000 kg / (h MW ), preferably between 600 and 2000 kg / (h MW), preferably between 1000 and 1500 kg / (h MW). BE2018 / 5916 Process - Flow Fp, Fr and Fm [0045] A flow of mixture Fm of a solution of mixture Pm comprising undesirable volatilizable materials at a non-zero mass concentration xpv and phosphorus at a mass concentration, xpm, greater than that of contact feed flow F0 is formed by the spray flow Fp, optionally mixed with a residual flow Fr of an aqueous residual solution Pr originating from the residues of a prior industrial process. If the feed solution, F0, does not contain undesirable volatilizable materials, then mixing of the feed stream PO with a residual stream Fr is compulsory. Otherwise, it is optional, but preferred. The flow of mixture Fm is sprayed through a burning flame in the upper part of a combustion chamber (2) to: • possibly oxidize the undesirable volatilizable materials and volatilize them, • form combustion gases G1 carrying away the undesirable volatilizable materials thus volatilized (= undesirable volatilized materials) and thus purify the residual solution Pr, • evaporate water and thus concentrate the mixture solution Pm, • form a solution of purified phosphoric acid P3. • polymerize, possibly according to the initial P2O5 content, molecules of phosphoric acid purified into polyphosphoric acid. The residual stream Fr includes: • a mass concentration, xpr, of at least 1% P2O5, • a mass concentration, xer, of water, and • undesirable volatilizable materials. The waste stream (Fr) comprises a phosphorus xpr concentration of at least 1% or at least 5%, preferably at least 10%, more preferably at least 15%, preferably at least 20% P2O5, The flow rate, Qr, of the residual solution (Pr) in the combustion chamber expressed per unit of nominal power [MW -1 ] of the combustion chamber is preferably not zero and preferably between 5 and 1500 kg / (h MW), preferably between 400 and 1000 kg / (h MW). The temperature of the residual solution Fr can be between 20 and 200 ° C, preferably between 40 and 150 ° C, more preferably between 50 and 100 ° C. Preheating the solution Fr is advantageous in terms of the efficiency of combustion of the mixture solution Fm in the flame. The residual solution Pr and, optionally the feed solution PO, is or preferably contains a solution from industry. This solution can be generated by washing installations or during routine production or maintenance operations in industries such as the metallurgical, food, pharmaceutical, chemical industries and particularly the production of phosphate salts or fertilizers. . These solutions are generally difficult to recycle as such by their various pollutant contents, in particular soluble residues of organic matter and by their low phosphorus concentrations. They must therefore be treated before being then concentrated. The residual solution can also come from BE2018 / 5916 processes for recovering phosphorus from raw materials called "secondary" and which are in fact compounds containing phosphorus other than phosphate ore. Mention may in particular be made of bone ash, sludge or ash from sludge from treatment plants, pig and chicken manure, etc. These waste solutions or waste acid solutions or waste solutions include P2O5 but also often undesirable volatilizable materials such as typically carbon, fluorine, chlorine, sulfur, nitrogen in soluble form (ionic or not). The concentrations of undesirable volatilizable materials obviously depend on the origin of the residual solution. For example, they may be present in the residual solution Fr in xpv concentrations of undesirable volatilizable materials of at least 5 ppm (parts per million), preferably at least 10 ppm, preferably at least 100 ppm%, preferably at least 1%, more preferably at least 5% by weight of total organic carbon relative to the total weight of the solution or also at least 10 ppm of fluorine, at least 100 ppm of fluorine, at least 1% fluorine. Depending on the applications, these solutions cannot be used as they are. In a stationary state of production, the ratio, Qp / QO, between the flow rate Qp of the spray flow Fp and the flow rate Q0 of the feed flow F0 is preferably between 100 and 250%, preferably between 101 and 140%, preferably between 110 and 115%. This ratio can be higher than 100% because the contact of the flows Q0 and Q2 with the combustion gases in the gas-liquid contactor increases the mass of the flow, F1, leaving the gas-liquid contactor. The value of this ratio can decrease depending on whether the value of the residual flow, Qr, increases. The flow rate ratio Qr / (Qp + Qr) between the residual flow Qr and the sum of the spray flow rates, Qp, and of residues, Qr, represents the fraction of flow entering the combustion chamber which is formed of the residual solution, Pr. The value of this ratio depends inter alia on the contents of P2O5 and of undesirable volatilizable materials in the residual solution and / or of the feed solution, which are decisive for the content of P2O5 and of undesirable volatilizable materials of the mixing solution Pm. For example, the ratio Qr / (Qp + Qr) may be between 0 and 94%, preferably between 5 and 90%, more preferably between 10 and 80%, or even between 15 and 45%, [0051] Regardless of the value of the ratio Qr / (Qp + Qr), the mixing solution Pm preferably comprises a phosphorus concentration xpm greater than 1%, preferably greater than 2% or 5%, more preferably greater than 20% , more preferably greater than 30%, preferably greater than 40%, and more preferably between 45 and 60% P2O5. The flow rate, Qm, of the solution Pm in the combustion chamber is the sum of the spraying flow rates Qp and the residual solution Qr. Expressed per unit of nominal power [MW 1 ] of the combustion chamber, the mixing flow rate Qm is preferably between 305 and 3000 kg / (h MW), preferably between 900 and 2000 kg / (h MW). Process -Evaporation of Unwanted Volatilizable Materials and Polycondensation A main function of the combustion chamber is to degrade by oxidation and then to vaporize the undesirable volatilizable materials present in the residual solution. A second BE2018 / 5916 function of the combustion chamber is to evaporate the water present in the solutions to concentrate the residual and feed solutions. A third (optional) function is the polycondensation of the phosphate molecules present in polyphosphoric acid (PPA). The distribution of the species present in the solution thus formed depends on the P2O5 concentration of the mixture solution Fm reaching the combustion flame, as well as on the polycondensation temperature. As can be seen in Figure 1 (c), PPA is only formed if the P2O5 content is high enough, around 60% P2O5, which is higher than the phosphorus content generally present in Fr waste solutions. If PPA is desired, then it is necessary to increase the phosphorus content of the Fm mixing solution by feeding the combustion chamber with an Fp spray solution having a higher phosphorus concentration. The combustion in the flame of the mixing solution Pm therefore forms, on the one hand, combustion gases G1 formed by the evaporation of water and, in particular, undesirable volatilizable materials and, on the other part, a combustion solution P3 which is in the liquid state and comprising phosphorus and, if the concentration of P2O5 and the polycondensation temperature, Tpc, are sufficient, species polymerized by polycondensation of the phosphoric acid contained in the solution Pm. The flame is preferably a slightly oxidizing flame, preferably comprising between 1 to 5% of excess air. The temperature reached by the Pm mixing solution in the flame is an important parameter of the process since it will allow the volatilization of undesirable volatilizable compounds present in the residual solution and therefore in the mixing solution. The concentration of P2O5 obtained in the combustion solution, P3, is also dependent on it as shown in the graph in Figure 1 (a). It is also important to keep the mixing solution containing phosphoric acid in contact with the flame and the combustion gases for a sufficient time so that the water can evaporate and eventually polycondensation can be carried out. The flame is powered by a fuel and a source of oxygen, typically air or, for a higher temperature, oxygen. The fuel is preferably natural gas, butane, propane, or any other fuel, whether gaseous or liquid. In the absence of spraying of the mixture solution Pm, the flame preferably reaches a theoretical temperature of at least 750 ° C, preferably at least 1000 ° C, more preferably at least 1700 ° C, for example 1800 ° C ± 50 ° C. In the process of the present invention, the increase in temperature is instantaneously limited because, on the one hand, the mixture solution Pm is supplied at a lower temperature Tm, of the order of 20-300 ° C. and, on the other hand, because the evaporation of the water molecules from the solution is energy consuming. The residual flow Fr and of spraying Fp can be mixed to form the flow of mixture Fm before being sprayed into the flame in the combustion chamber, as illustrated in Figures 2 & 5. Alternatively, the two streams Fr and Fp can be sprayed separately in the combustion chamber to form the mixture stream Fm in the flame or just before reaching the flame, as illustrated in Figures 3 & 4. BE2018 / 5916 The combustion solution P3 which consists of a solution of purified phosphoric acid is therefore an aqueous solution of phosphoric acid which may contain species polymerized according to the P2O5 content present in the solution (see Figure 1 ). If the production of PPA is desired, it is preferable that the mixture solution sprayed in the flame reaches a polycondensation temperature, Tpc, of at least 400 ° C, preferably at least 500 ° C and even greater than 550 ° C, or even around 650 ° C or 700 ° C, for a predefined polycondensation time. A high polycondensation temperature Tpc makes it possible to obtain polyphosphoric acid solutions with a high concentration of P2O5, of the order of 86% and more, with longer chain lengths n (eg, n> 5 to 12) ( see Figure 1 (c)). The temperatures required for the polycondensation of phosphoric acid require chemically and thermally resistant materials for the various elements of the reaction device. The mixing solution Pm, which comprises molecules of orthophosphoric acid and optionally oligomers of polyphosphoric acid (of m + 1 condensed units) undergoes a polycondensation reaction under the action of temperature to release water and form longer polymer chains, according to equation (1) described above and according to equation (2) (with m> 1 and r> 1): Ilii HO —P-O - P —O -H II Oh oh O II HO— P — OH I OH HO — P — O -P — O -H + r H2O OH L 0H J m + r (2) The combustion solution P3 thus formed is then separated from the combustion gases G1 formed during the evaporation of the water and undesirable volatilizable materials and possibly of the polycondensation of the polyphosphoric acid in a gas-liquid separator (9). The combustion solution P3 containing phosphoric acid and optionally polyphosphoric acid and practically free of undesirable volatilizable materials is recovered while the combustion gases G1 are transferred to the gas-acid contactor (1) to be brought into contact with the feed flows F0 and recirculation F2, as described above. The flow F3 of the combustion solution P3 thus recovered can have a high temperature of the order of 150 to 700 ° C, preferably 200 to 650 ° C, preferably 300 to 500 ° C depending on the temperature of vaporization of undesirable volatile matter contained in the mixing solution, Pm. The temperature necessary for the volatilization of volatilizable materials present in the Pm mixture solution varies according to the nature of the materials present in the Pm mixture solution. It is preferable to cool the solution P3 in a heat exchanger (11) (see Figure 2) to a temperature below T3 which allows a greater choice of materials for the storage tank of phosphoric acid (and possibly polyphosphoric purified) thus formed and cooled, while maintaining the solution in the liquid state. BE2018 / 5916 The combustion solution P3 comprising purified phosphoric (and optionally polyphosphoric) acid thus formed and recovered comprises a concentration of undesirable volatilizable materials lower than that of the residual solution Pr. For example, the combustion solution P3 comprises less than 50% of the undesirable volatilizable materials contained in the residual solution Pr, preferably less than 70%, more preferably less than 80% or less than 90%, and ideally less than 95 or 99%. The combustion solution P3 has a higher concentration of P2O5 'than that of the mixture solution Pm. This is explained by the evaporation of a large part of the water from the solution when it passes through the flame. The concentration P2p3 of P2O5 x3 of the combustion solution P3 is normally greater than 10% P2O5, preferably greater than 15%, preferably greater than 25%, particularly preferably greater than 40%, or is preferably between 30 and 76 %, The flow rate, Q3, of the combustion solution P3 out of the combustion chamber is representative of the capacity for purification of phosphoric acid. Expressed per unit of nominal power [MW 1 ] of the combustion chamber, the flow rate Q3 is preferably between 240 and 1500 kg / (h MW), preferably between 500 and 1000 kg / (h MW). The combustion gases G1 consist mainly, on the one hand, of CO2, O2, H2O, on the other hand, of undesirable volatilizable materials such as, for example, nitrogen oxides (Nox), sulfur oxides, HF, HCl, CO2, and also of phosphorus-containing molecules, the latter being able to be present in quantities varying between 0.1 and 15% by weight of P2O5, according to the concentration xpm of the mixing solution, Pm. In general, the P2O5 content which may be present in the combustion gases G1 varies between 0.5 and 13% by weight, preferably between 1 and 10%, preferably between 2 and 5% P2O5. The temperature Tg1 of the transferred combustion gases G1 is significantly lower than the temperature that the flame can reach because, as discussed above, the temperature in the combustion unit drops during the polycondensation reaction which requires a lot of energy, mainly to evaporate the water from the polycondensation reaction. The combustion gases enter the acid-gas contactor at a temperature Tg1 which is of the order of the polycondensation temperature Tpc, and is generally between 200 and 600 ° C, preferably between 400 and 500 ° C. Process - Recirculation and Combustion Gas Loop As discussed above, a recirculation fraction of the enriched phosphoric acid solution P1 leaving the gas-acid contactor (1) is reintroduced into the gas-acid contactor thus forming a recirculation loop while a spray fraction Pp is routed to the combustion chamber (2). The recirculation fraction is preferably greater than or equal to the spraying fraction and is ideally considerably greater than the spraying fraction, with Qp / Q2 ratios of the spraying flow rate Qp to the recirculation flow rate Q2 possibly ranging from 0.1 / 99.9 to 49/51 (= 0.1 to 96%). Preferably, the flow rate ratio Qp / Q2 is between 1/99 and 5/95 (= 1 to 5.3%). BE2018 / 5916 When they are introduced into the gas-acid contactor, the feed flows F0 and of recirculation F2 can be mixed before their introduction into the gas-acid contactor to form a flow of a mixture of the solution power supply PO and the recirculated enriched phosphoric acid solution P2, as illustrated in Figures 2 & 4. Alternatively, the flows F0 and F2 can be contacted after having been introduced separately into the gas-acid contactor to form a flow of a mixture of the contact feed solution PO and the recirculated enriched phosphoric acid solution P2, as shown in Figures 3 & 5. The recirculation loop is an important element of the present invention. The main consequence of the introduction of such a recirculation loop is that the ratio (Qg1 / (Q0 + Q2)) between the mass flow Qg1 of the combustion gas G1 introduced into the gas-acid contactor (1) and the flow total mass (Q0 + Q2) of the feed flows F0 and of recirculation F2 introduced into the gas-acid contactor (1), is much lower than in the absence of such a recirculation loop. The ratio (Qg1 / (Q0 + Q2)) according to the present invention is preferably between 0.1 and 50%, more preferably between 0.5 and 20 or less than 10%, and is ideally between 1 and 7%. In the absence of such a recirculation loop (ie, Qg1> 0, Q0> 0 and Q2 = 0), the ratio (Qg1 / Q0) is considerably greater, with values greater than 60%, generally greater at 100%, indicative of a flow of combustion gas Qg1 greater than the supply flow Q0 of supply solution PO of the contactor. The recirculation loop therefore makes it possible to control the ratio between the flow of combustion gas G1 and the total flow (Q0 + Q2) of feed solutions of phosphoric acid PO and of recirculated enriched phosphoric acid solution P2 . In particular, it considerably increases the mass of phosphoric acid solution contacted with the combustion gas. This has several advantages. On the one hand, the transfer of droplets and vapors of P2O5 contained in the combustion gases G1 to the flow of the mixture of solutions PO and P2 is much greater. The P2O5 concentration of the spray solution formed during contact with the combustion gases is thus higher than if the flow rate ratio Qg1 / (Q0 + Q2) had been higher. The better gas / liquid contact thus obtained allows better recovery by the enriched phosphoric acid solution P1 of the P2O5 contained in the combustion gases G1. In addition, the combustion gases G3 after contact with the flows F0 and F2 are thus cleaned of their P2O5 content, lightening their treatment before releasing them into the atmosphere. On the other hand, with such flow ratios, the temperature Tg3 of the combustion gases G3 after their contact with the flows F0 and F2 is reduced much more effectively than in the process described in EP2411325 B1, thus requiring no another heat exchanger (or at least of smaller capacity), essential in the process of EP2411325 B1 for lowering the temperature of the combustion gases to an acceptable value for their discharge into the atmosphere. Device BE2018 / 5916 The method of the present invention can be implemented in a device comprising a combustion chamber (2), a gas-acid contactor (1) and various fluid connections between the combustion chamber and the gas-acid contactor . It is clear that the device can include several combustion chambers and / or several gas-acid contactors positioned in parallel or in series. Device - combustion chamber (2) The combustion chamber (2) makes it possible to carry out the combustion of the Pm mixing solution, by spraying it into the flame. The mixing solution Pm is formed from the spraying solution Pp mixed with the residual solution Pr to form a combustion solution P3 comprising phosphoric acid (and optionally polyphosphoric acid) purified from undesirable volatilizable materials. The walls of the combustion chamber must resist the corrosive nature of the spraying solutions Pp and of residues Pr and the high temperatures prevailing inside it. It is preferable that the walls are made of silicon carbide or carbon. amorphous. It is possible to use double walls with a neutral gas or the combustion gases circulating between the two walls, which can have advantages in terms of temperature of the walls, and impermeability of these to acid solutions (poly )phosphoric. The combustion chamber (2) has one or more spray inlet (s) (2pu) in the combustion chamber allowing the introduction of a spraying solution Pp at a flow rate Qp, or a solution of Pm mixture at a flow rate (Qp + Qr), in sprayed form in a combustion unit located in an upper part of the combustion chamber (cf. Figures 2 & 4). In a variant of the invention, the combustion chamber may include one or more residue inlet (s) (2pdu) allowing the introduction of a residual solution Pr at a flow rate Qr, separate from the inlet (s) spray (2pu) (see Figures 3 & 5). A supply of an inert gas, such as nitrogen, can be provided to optimize the spraying of the spraying solution Pp and of residues Pr and / or of mixture Pm, which can have a high viscosity at the inlet of the combustion chamber. The residue inlet (2pdu) is in fluid communication with a source of a residual solution (Pr) which is aqueous and comprises phosphorus and undesirable volatilizable materials. The combustion chamber (2) comprises a combustion unit ( 2c) arranged in the upper part of the combustion chamber, and capable of forming a flame having a temperature of at least 1000 ° C, preferably at least 1500 ° C, and even at least 1700 ° C, preferably 1800 ° C ± 50 ° C, by combustion of a fuel in the presence of oxygen. The flame temperature can be controlled by varying the flow of oxygen supplying the flame. The combustion unit includes: • a burner, • fluid connections between the burner and, on the one hand, a source of oxygen and, on the other hand, a source of fuel (10) enabling the flame to be fed, BE2018 / 5916 ratio between the fuel and oxygen supplies to the burner make it possible to control the temperature of the flame. Preferably, the fuel used is chosen from natural gas, methane, butane, propane. The source of oxygen is usually air or oxygen. The combustion chamber (2) is equipped with a gas-liquid separator (9) to separate the combustion solution P3 thus formed from the combustion gases G1. For example, the combustion gases can be separated from the combustion solution by an enlargement of the transverse flow surface, which has the consequence of reducing the flow speed and therefore the kinetic energy of the gas flows G1 and combustion F3. As the flows flow from top to bottom, by the drop in their kinetic energy, the gases will slow down and can be diverted towards a deflector which guides them towards the exit of the combustion gases. Thanks to their higher density, the purified phosphoric and possibly polyphosphoric acid droplets from the combustion solution P3 continue to flow downwards by gravity. The combustion chamber (2) has a combustion outlet (2pd) from the combustion chamber to recover a liquid phase of purified (poly) phosphoric acid, and arranged downstream of the combustion unit which is it -Even arranged downstream of the mixing or spraying inlet and of residues, the term "downstream" is expressed relative to the direction of flow of the spraying solutions Pp and of polyphosphoric acid P3 in the combustion chamber. As explained above, the direction of flow is preferably from top to bottom in the direction of gravity. The device can thus be equipped with a storage tank for the phosphoric acid thus produced (not shown). Preferably, the device comprises a heat exchanger (11) arranged between the combustion outlet (2pd) and the storage tank, in order to cool the combustion solution P3 from a temperature between about 200 and 650 ° C to a temperature of the order of 100 to 150 ° C when it reaches the storage tank. Finally, the combustion chamber (2) is provided with an outlet for evacuating combustion gases G1 from the flame. These combustion gases are charged with droplets and vapors of P2O5 and undesirable volatilized materials. They have a temperature Tg1 and do not need to be cooled before being introduced into the gas-acid contactor. Device - gas-acid contactor (2) The gas-acid contactor (1) makes it possible to heat and increase the equivalent concentration in P2O5 units of the feed solution introduced into the contactor, before it enters the chamber combustion (2) to optimize the purification yield of phosphoric acid and the energy consumption of the polycondensation reaction. The gas-acid contactor (1) has a supply inlet (1pu) connected to a source of a supply solution PO of the contactor or of a mixture of supply solution PO of the contactor and solution enriched phosphoric acid P2. As discussed above, the solution BE2018 / 5916 of power supply PO of the contactor comprises between 0 and 54% P2O5, preferably from 0.1 to 50%, preferably from 1 to 35%, more preferably between 15 and 20% P2O5. The supply inlet (1 pu) must be dimensioned to allow the introduction of the PO supply solution for the contactor at a feed rate QO or the introduction of the mixture of PO supply solution for the contactor enriched phosphoric acid solution recirculated P2 at a flow rate (QO + Q2). The recirculated enriched phosphoric acid solution, P2, can also be introduced into an inlet (1pru) of recirculated enriched phosphoric acid, P2, separate from the supply inlet (1 pu). The gas-acid contactor (1) is preferably a direct contactor. It includes a combustion gas inlet (1gu) allowing the introduction into the gas-acid contactor of the combustion gases G1 coming from the combustion gas discharge outlet G1. The supply inlet (1gu) must be dimensioned to allow the introduction of combustion gases G1 at a flow rate Qg1. As discussed above, the combustion gases G1 brought into contact with the supply solution PO of the contactor make it possible (a) to increase the temperature of supply solution PO of the contactor, (b) to evaporate part of the water of the PO supply solution of the contactor and (c) exchange with the PO solution the droplets and vapors of P2O5 contained in the combustion gas G1. The gas-acid contactor (1) is provided with a recirculation inlet (1pru), allowing the introduction of a recirculated enriched phosphoric acid solution P2. In a variant of the invention, the flows F0 and F2 are mixed before being introduced into the gas-acid contactor and the recirculation inlet is then the same as the supply inlet (1pu). In an alternative variant, the supply (1 pu) and recirculation (1 pru) inputs are separated. The recirculation inlet must be sized to allow the introduction of the recirculated enriched phosphoric acid solution P2 at a feed rate Q2. The gas inlet (1gu), the supply inlet (1 pu) and, if it is separate from it, the recirculation inlet (1pru) are arranged to allow, on the one hand , • a contact between the feed streams F0 and recirculation stream F2 to form a stream (F0 + F2) of a mixture (P0 + P2) of the feed solution PO of the contactor and the acid solution enriched phosphoric recirculated P2 and, on the other hand, • a contact of the flow of the mixture thus formed with the flow of combustion gases G1. The gas inlet (1gu) is preferably arranged so that the combustion gases G1 (and referred to as G2 during contact) flow co-current with the feed flows F0 and recirculation F2 d 'Phosphoric acid. But it is possible to arrange the gas inlet so that the combustion gases flow against the current of the flows F0 and F2. The gas-acid contactor preferably comprises a filling material, through which percolate the feed flows F0 and recirculation F2 of phosphoric acid solutions. The filling material is preferably placed on a perforated support, for example a support grid. BE2018 / 5916 The gas-acid contactor (1) comprises one or more enriched phosphoric acid outlets (1pd, 1prd), the enriched phosphoric acid outlet (s) (1pd, 1prd) are positioned downstream of the gas inlet (1gu), which is itself positioned downstream of the supply inlet (1pu) and, if it is separate from it, the recirculation inlet (1pru). The term "downstream" is expressed in relation to the direction of flow of the feed and recirculation flows of the feed solutions of phosphoric acid and of enriched phosphoric acid recirculated P2 in the gas-acid contactor. The enriched phosphoric acid outlet (s) (1pd, 1prd) make it possible to take out the enriched phosphoric acid solution P1 formed in the gas-acid contactor formed by the contact between the flows F0 and F2 and the combustion gases G1. The gas-acid contactor (1) comprises a gas-liquid separator making it possible to separate the liquids from the gases after the contact between the combustion gases G1 and the solutions PO and P1. For example, the gas-acid contactor may include a de-mister which makes it possible to recover any droplets of liquid present in the combustion gas contacted G3 before it leaves via the gas outlet (1gd). The gas-acid contactor (1) also includes an outlet (1gd) of combustion gas, making it possible to evacuate from the gas-acid contactor the combustion gases contacted G3 after their contact with the mixture of solutions PO and P2, The device can be followed by a washing tower for the combustion gases contacted G3 located downstream of the combustion gas outlet (1gd) from the gas-acid contactor, making it possible to eliminate any fluorinated and sulfur compounds that the gases contain before releasing them into the atmosphere. The device is equipped with a fluid connection (6) of combustion gases connecting one end (6u) coupled to the outlet for evacuation of the combustion gases from the combustion chamber (2), at one end (6d ) coupled to the combustion gas inlet (1gu) in the gas-acid contactor (1). The temperature in this fluid connection (6) should preferably be kept as high as possible so that at the level of the inlet (1 gu) in the gas-acid contactor, the combustion gases G1 have a temperature as close as possible to the temperature Tg1 that they have at the outlet of the combustion chamber, that is to say approximately 200 to 600 ° C. The device is equipped with a fluid connection (3, 3p) connecting an upstream end (3u) coupled to the outlet of enriched phosphoric acid (1pd) from the acid gas contactor (1), at a downstream end (3d ) coupled to the spray inlet (2pu) of the combustion chamber (2). As the enriched phosphoric acid solution P1 has recovered most of the phosphorus molecules carried away by the combustion gases G1, the fluid connection (3.3p) allows these molecules to be reinjected into the combustion chamber in order to obtain a solution P3 combustion as rich as possible in P2O5. The enriched phosphoric acid solution P1 has a temperature higher than that of the supply solution PO of the contactor, which allows better management of the heat energy of the process by injecting into the combustion chamber a solution already at a temperature relatively high. If the production of PPA is desired, the highest concentration of P2O5 and the highest temperature of the P1 enriched phosphoric acid solution allow BE2018 / 5916 to increase the concentration efficiency in the combustion chamber. This improvement in the transfer of phosphoric acid molecules and in concentration yield is made possible by the recirculation loop making it possible to reintroduce into the gas-acid contactor part of the flux of phosphoric acid P1 taken out of the same gas contactor. -acid. Thus, the device also comprises a recirculation fluid connection (3r) connecting an upstream end coupled either • to an outlet of recirculated enriched phosphoric acid (1prd) from the gas-acid contactor (1), or • to a branch point (5v) with the first fluid connection (3), • at a branch point (4r) with the first fluid connection (3u), at a downstream end (3r) coupled to the recirculation inlet (1pru) or ( 1pu) of the gas-acid contactor. The device is provided with means for controlling and maintaining a ratio, Qp / (Qp + Q2), between a mass flow rate of spray Qp flowing in the first fluid connection (3) and a total mass flow rate (Qp + Q2) defined as the sum of the mass spray flow Qp and a recirculation mass flow Q2 flowing in the recirculation fluid connection (3r) at a value less than 50%, preferably less than 10%, preferably less than 5%, more preferably less than 2.5% and in which the ratio Qp / (Qp + Q2) has a value greater than 0.1%, preferably greater than 0.5%. As illustrated in Figure 2, the fluid connections (3p) and (3r) can be separated over their entire length between the gas-acid contactor and the combustion chamber with, on the one hand, the spray fluid connection (3p) connecting a first outlet of enriched phosphoric acid (1pd) to the inlet of enriched phosphoric acid (2pu) in the combustion chamber and, on the other hand, the recirculation fluid connection (3r) connecting a second enriched phosphoric acid outlet (1prd) at the recirculated enriched phosphoric acid inlet (1pu) from the gas-acid contactor or at the supply connection (3a) supplying the gas-acid contactor with PO supply solution from the contactor. Each of the fluid spraying (3p) and recirculation (3r) connections being provided with a pump (4, 4r) sized to maintain the ratio, Qp / (Qp + Q2) at a desired value or with a transfer system fluids. In an alternative variant illustrated in Figures 3 to 5 the gas-acid contactor is provided with a single outlet (1pd) of phosphoric acid enriched P1 of the gas-acid contactor which is coupled to a first fluid connection (3) . The upstream parts of the spraying (3p) and recirculation (3r) fluid connections are coupled to a branch point (5), thus forming with the first fluid connection (3) a T or Y branch. In this variant, different means can be used to control and maintain the ratio, Qp / (Qp + Q2) at the desired value. In a first variant illustrated in Figure 5, the means for ensuring a ratio, Qp / (Qp + Q2) to the desired value comprise a pump (4) arranged on the fluid connection of BE2018 / 5916 spraying (3p) and having a capacity for pumping a liquid at a spraying rate Qp and a recirculation pump (4r) arranged on the recirculation fluid connection (3r) and having a capacity for pumping a liquid at a recirculation rate Q2, In a second variant illustrated in Figures 3 and 4, the means for ensuring a ratio, Qp / (Qp + Q2) comprise a pump (4) arranged on the first fluid connection (3 ) upstream of the branch point (5) and having a capacity for pumping a liquid at a main flow rate (Qp + Q2) and one or more valves (5v) (eg a three-way valve) arranged at the branching point (5) and making it possible to divide the main flow rate into a spray flow rate Qp towards the spray fluid connection (3p) and into a recirculation flow Q2 toward the recirculation fluid connection (3r), [0095] In a third variant (not illustrated), the means for ass urer the report, Qp / (Qp + Q2) comprise a pump (4) arranged on the first fluid connection (3) upstream of the branch point (5) and having a capacity for pumping a liquid at a main flow rate (Qp + Q2) and pipes forming the spraying (3p) and recirculation (3r) fluid connections dimensioned so as to obtain the desired Qp / (Qp + Q2) ratio. This solution is less flexible than the first two in that once the pipes are dimensioned, the ratio Qp / (Qp + Q2) cannot be varied easily, which is not necessarily a problem if the ratio must not vary during the lifetime of the device. In a fourth variant (not illustrated), the means for ensuring the ratio, Qp / (Qp + Q2) comprise a pump (4) arranged on the first fluid connection (3) upstream of the branch point (5 ) and having a capacity for pumping a liquid at a main flow rate (Qp + Q2) and forming the fluidic spraying (3p) and recirculation (3r) connections as well as valves adjusted so as to obtain the Qp / (Qp + Q2) desired. Table 2 lists a series of ranges of values of the different parameters suitable for implementing the method of the present invention. Table 2: Examples of parameter values suitable for the process of the present invention Ti xPI Qi° C % [Ρ 2 Ο 5 ] [kg / (h MW)]min max Low max Low max F0 20 200 > 0% 54% 100 3000 F1 100 300 > FO 60% 600 123000 F2 100 300 > FO, = F1 60% 300 120000 FP 100 300 > FO, = F1 60% 300 3000 Fr 20 200 > 1% 50% 5 1500 fm 20 300 > 1% 60% 305 3000 F3 150 700 > Fm, 76% 240 1500 G1 200 600 0.1% 15% __ __ G3 100 250 <G1 1% - - BE2018 / 5916 # Feature 1 Gas-acid contactor igd Flue gas outlet from the gas-acid contactor igu Combustion gas inlet in the gas-acid contactor 1PD Exit of enriched phosphoric acid solution, P1, from the gas-acid contactor 1PU Supply inlet for the contact solution, PO, or mixture (P0 + P2) in the gas-acid contactor 1pru Input of phosphoric acid enriched with recirculation, P2, into the gas-acid contactor (optional). 2 Combustion chamber 2c Combustion unit 2PD Combustion outlet, P3, from the combustion chamber 2pdu Residue inlet, Pr, into the combustion chamber 2PU Spray solution inlet, Pp, into the combustion chamber or combined inlet of direct feed streams and spray streams 3 First fluid connection 3a Fluid power connection 3d Downstream end of the first fluid connection (3) 3p Spray fluid connection 3r Fluid recirculation connection to the gas-acid contactor (1) 3rd Downstream end of the recirculation fluid connection (3r) 3u Upstream end of the spray fluid connection (3p) or the first fluid connection (3) 4 Pump 4r Recirculation pump 5v Valve or set of valves (e.g. three-way valve) 6 Fluid connection of combustion gases 6d Combustion gas connection outlet 6u Combustion gas connection input 10 Fuel source for the combustion unit (10) 11 Heat exchanger fp Spray stream of enriched phosphoric acid solution F2 Recirculated enriched phosphoric acid solution recirculation flow F3 Combustion solution flow Fr Waste stream of waste solution Pr fp Spray stream of enriched phosphoric acid solution fm Mixing flow of mixing solution Fm (Fr + Fp) G1 Combustion gases BE2018 / 5916 G3 Contacted combustion gases PO Feeding solution P0 + P2 Mixture of PO contactor feed solution and P2 recirculated enriched phosphoric acid solution P1 Enriched phosphoric acid solution P2 Recirculated enriched phosphoric acid solution P3 Combustion solution Pr Residual solution pp Spray solution Pm Mixing solution (= Pr + Pp) QO Feed rate of the PO feed solution of the contactor Q1 Enriched phosphoric acid output at the contactor output (= Q2 + Qp) Q2 Recirculation rate of the recirculated enriched phosphoric acid solution Q3 Flow rate of the combustion solution qgi Flue gas flow to the gas-acid contactor (1) Qg2 Flue gas flow in the gas-acid contactor (1) GG3 Flow of combustion gases contacted outside the gas-acid contactor (1) Qm Flow rate of the mixing solution Pm Qp Spray rate of spray solution Pp qr Flow rate of the residual solution Pr TO Contactor PO solution supply temperature T1 Temperature of the P1 enriched phosphoric acid solution T2 Recirculated enriched phosphoric acid solution temperature P2 T3 Temperature of combustion solution P3 tgi Flue gas temperature G1 tg3 Temperature of the combustion gases contacted G3
权利要求:
Claims (12) [1] 1. Process for the purification of an aqueous residual solution comprising phosphorus molecules and undesirable volatilizable materials comprising the following steps: (a) introducing into a gas-acid contactor (1), a feed stream (F0) of a feed solution P0 which is aqueous and comprising phosphorus molecules preferably in the form of species of orthophosphate type to a mass concentration, xp0, of between 0 and 54% equivalent in units of P2O5, (b) introducing into the gas-acid contactor (1) a recirculation flow (F2) of recirculated enriched phosphoric acid solution (P2), (c) introducing combustion gases (G1) into the gas-acid contactor (1); (d) contact the feed (F0) and recirculation (F2) and combustion gas (G1) flows to form, in the gas-acid contactor, on the one hand, • an enriched phosphoric acid solution (P1 ) comprising a mass concentration, xp1, of P2O5 content which is greater than xp0 (xp1> xp0) and, on the other hand, • the contacted combustion gases (G3), (e) separating the contacted combustion gases (G3) of the enriched phosphoric acid solution (P1), then • remove the combustion gases contacted (G3) from the gas-acid contactor (1), and • remove the enriched phosphoric acid solution (P1) from the gas-acid contactor (1), (f) forming from said enriched phosphoric acid solution (P1), on the one hand, • a recirculation flow (F2) of recirculated enriched phosphoric acid solution (P2) to introduce it in the gas-acid contactor (1) as defined in step (b) and, on the other hand, • a spray flow (Fp) of the enriched phosphoric acid solution (P1) to introduce it into a combustion chamber (2), (i) spray through a burning flame in the upper part of the combustion chamber (2) a mixture flow (Fm) of a mixture solution (Pm) comprising phosphorus at a mass concentration, xpm, and undesirable volatilizable materials, the mixture flow being formed by, on the one hand, • the enriched phosphoric acid solution (P1) and optionally, on the other hand, • a residual flow (Fr) of an aqueous residual solution (Pr) comprising a mass concentration, xpr, of at least 1% P2O5, for: • evaporate water and thus concentrate the mixing solution (Pm), • optionally oxidize and in all cases evaporate undesirable volatilizable impurities, • form combustion gases (G1), and • form a combustion solution (P3 ) having, BE2018 / 5916 a mass concentration, xp3 in P2O5 greater than the concentration of the residual solution (Pr), and a content of volatilizable impurities less than that of the residual solution (Pr), (g) separating the combustion solution (P3) combustion gases (G1) and • recover the combustion solution (P3), and • transfer the combustion gases (G1) to the gas-acid contactor (1) as defined in step (c). [2] 2. Method according to claim 1, in which • the feed solution (FO) comprises a concentration xpO of between 0.1 and 50%, preferably from 1 to 35%, preferably from 5 to 20% P2O5 and in which • a flow rate, QO, of the supply solution (FO) in the contactor expressed per unit of nominal power [MW 1 ] of the combustion chamber is preferably between 100 and 3000 kg / (h MW), preferably between 500 and 2500 kg / (h MW). [3] 3. Method according to claim 1 or 2, in which • the enriched phosphoric acid solution (P1) is identical to the recirculated enriched phosphoric acid solution (P2) and comprises a phosphorus concentration xp1 greater than or equal to 1 %, preferably less than 60%, more preferably between 5 and 50%, preferably between 10 and 40% P2O5 and in which • a total flow rate, Q1 = (Qp + Q2), of the solution (P1) outside the contactor expressed per unit of nominal power [MW 1 ] of the combustion chamber is preferably between 600 and 123,000 kg / (h MW), preferably between 1,000 and 50,000 kg / (h MW) and • a ratio, Qp / (Qp + Q2), between the mass flow (Qp) of the spray flow (Fp) and the total mass flow (Qp + Q2) is preferably less than 50%, preferably less than 10%, preferably less than 5 %, more preferably less than 2.5% and in which the ratio Qp / (Qp + Q2) is greater 0.1%, preferably greater than 0.5%. [4] 4. Method according to any one of the preceding claims, in which the residual solution (Pr) comprises a concentration xpr of phosphorus greater than or equal to 2%, preferably at least 5%, more preferably at least 10%, preferably at least 20% P2O5, • the residual solution (Pr) comprises a concentration xpv of undesirable volatilizable materials of at least 5 ppm, preferably of at least 10 ppm, preferably of at least 100 ppm, preferably at least 1%, preferably at least 5%, preferably at least 10%, more preferably at least 25% by weight relative to the total weight of the solution, and in which BE2018 / 5916 • a flow rate (Qr) of the residual solution (Pr) in the combustion chamber expressed per unit of nominal power [MW -1 ] of the combustion chamber is non-zero and preferably between 5 and 1500 kg / (h MW), preferably between 400 and 1000 kg / (h MW). [5] 5. Method according to any one of the preceding claims, in which, • a Qr / (Qr + Q0) ratio is between 0 and 99%, preferably between 5 and 90%, more preferably between 10 and 80%, or between 15 and 45%, and in which • the mixture flow (Fm) comprises a phosphorus concentration (xpm), greater than 1% P2O5 (xpm> 1% P2O5,) And in which Q0, Qp and Qr are mass flows of the feed solutions (P0), enriched phosphoric acid (P1) and residues (Pr), respectively. [6] 6. Method according to any one of the preceding claims, in which, the mixing solution (Pm) comprises a concentration xpm greater than 2%, preferably greater than 5%, more preferably greater than 20%, more preferably greater than 30%, preferably greater than 40%, and more preferably between 45 and 60% P2O5. The mixing solution (Pm) comprises a concentration xpv of undesirable volatilizable materials of at least 5 ppm, preferably of at least 10 ppm, preferably of at least 100 ppm, preferably of at least 1%, preferably at least 5%, preferably at least 10%, more preferably at least 25% by weight relative to the total weight of the solution, and in which, • a flow rate (Qm) of the mixing solution (Pm) in the combustion chamber expressed per unit of nominal power [MW -1 ] of the combustion chamber is preferably between 305 and 3000 kg / (h MW), preferably between 200 and 2000 kg / (h MW). [7] 7. Method according to any one of the preceding claims, in which the combustion solution (P3) comprises a phosphorus concentration xp3 greater than 1% equivalent in units of P2O5, preferably greater than 10%, preferably greater than 25%, particularly preferably greater than 40%, or is preferably between 30 and 76%, and in which, • the flow rate (Q3) of the combustion solution (P3) out of the combustion chamber expressed per unit of nominal power [MW -1 ] of the combustion chamber is preferably between 240 and 1500 kg / (h MW), preferably between 600 and 3000 kg / (h MW). [8] 8. Method according to any one of the preceding claims, in which the feed (F0) and recirculation (F2) flows are either, • mixed before their introduction into the gas-acid contactor to form a flow of a mixture feed solution (P0) and recirculated enriched phosphoric acid solution (P2), i.e. BE2018 / 5916 • contacted after having been introduced separately into the gas-acid contactor to form a flow of a mixture of the feed solution (F0) and the recirculated enriched phosphoric acid solution (P2). [9] 9. Method according to any one of the preceding claims, in which • A residual flow (Qr) of the residual solution (Pr) is non-zero, • The residual solution (Pr) and, preferably, the spraying solution ( Pp) include undesirable volatilizable materials, and in which the waste stream (Fr) and the spray stream (Fp) are either, • mixed to form the mixture stream (Fm) before being sprayed into the flame in the chamber or either • sprayed separately into the combustion chamber to form the mixture flow (Fm) in the flame or just before reaching the flame. [10] 10. Method according to any one of the preceding claims, in which the contact between the feed (F0) and recirculation (F2) flows and the combustion gases (G1) in step (d) takes place at co-current or counter-current, preferably co-current flowing from an upper part to a lower part of the gas-acid contactor and in which during the contact step (d), a ratio ( Qg1 / (Q0 + Q2)) between a mass flow (Qg1) of the combustion gas (G1) introduced into the gas-acid contactor (1) and a total mass flow (Q0 + Q2) of the contact supply flows ( F0) and recirculation (F2) introduced into the gas-acid contactor (1) is between 0.1 and 50%, preferably between 0.5 and 10%, more preferably between 1 and 7%. [11] 11. Device for producing purified phosphoric acid (P3) according to a process according to any one of the preceding claims, comprising: (A) a combustion chamber (2) having: • a spray inlet (2pu) into the combustion chamber allowing the introduction at a flow rate of an enriched phosphoric acid solution (P1) in spray form in a combustion unit (2c), • a residue inlet ( 2pdu) in the combustion chamber or upstream of the spray inlet (2pu) allowing the introduction of a residual solution (Pr) or a mixture of residual solutions (Pr) and enriched phosphoric acid (P1 ) in spray form in a combustion unit (2c), • the combustion unit (2c) being arranged in the upper part of the combustion chamber, and being capable of forming a flame having a temperature of at least 1500 ° C by combustion of a fuel, said combustion unit comprising: o a burner, o fluid connections between the burner and, on the one hand, a source of oxygen and, on the other hand, a source of fuel (10) making it possible to supply the flame, BE2018 / 5916 • a combustion outlet (2pd) from the combustion chamber to recover a combustion solution (P3) in the liquid phase, and arranged downstream of the combustion unit which is itself arranged downstream of the spray inlet (2pu) and residue (2pdu), • a combustion gas discharge outlet (G1) from the flame (B) a gas-acid contactor (1) having • a supply inlet (1pu ) connected to a source of a feed solution (F0), allowing the introduction at a contact feed rate (Q0) of a feed solution (F0), • a combustion gas inlet ( 1gu) allowing the introduction into the gas-acid contactor of the combustion gases (G1) at a flow rate (Qg1), • a recirculation input (1pru) identical or different from the contact supply input (1pu), allowing the introduction of a recirculated enriched phosphoric acid solution (P2) at a recirculation rate n (Q2), • the feed (1pu) and / or recirculation (1pru) and gas inlet (1gu) inlets being arranged to allow, on the one hand, o contact between the feed stream F0 and recirculation flow F2 to form a flow of a mixture of the feed solution (F0) and the recirculated enriched phosphoric acid solution P2 and, on the other hand o contact of the mixture thus formed with the gases combustion (G1), • one or more enriched phosphoric acid outlets (1pd), (C) a first spray fluid connection (3p) connecting an upstream end (3u) coupled • to the enriched phosphoric acid outlet ( 1m) of the acid gas contactor (1) or • at a branch point (5) with a first fluid connection (3) which is coupled to the outlet of enriched phosphoric acid (1m), (D) a first fluid connection spray (3p) connecting an upstream end (3u) coupled • to the phosphoric acid outlet an enriched eu (1pd) from the acid gas contactor (1) or • at a branch point (5) with a first fluid connection (3) which is coupled to the outlet of enriched phosphoric acid (1pd), at a downstream end (3d) coupled to the entry of enriched phosphoric acid (2pu) into the combustion chamber (2), Characterized in that the device further comprises (E) a recirculation fluid connection (3r) connecting an upstream coupled end, • to an outlet of recirculated enriched phosphoric acid (1pd) from the gas-acid contactor (1) or • to a branch point (5) with the first fluid connection (3), at a downstream end coupled, • at the recirculation inlet (1pru) of the gas-acid contactor (1) or BE2018 / 5916 • to a supply connection (3a) supplying the gas-acid contactor in supply solution (F0), and (F) means for controlling and maintaining a ratio, Qp / (Qp + Q2), between a mass spray flow (Qp) flowing in the spray fluid connection (3p) and a total mass flow (Qp + Q2) defined as the sum of the mass spray flow (Qp) and a mass flow of recirculation (Q2) flowing in the recirculation fluid connection (3r) at a value less than 50%, preferably less than 10%, preferably less than 5%, more preferably less than 2.5% and in which the ratio Qp / (Qp + Q2) has a value greater than 0.1%, preferably greater than 0.5%. [12] 12. Device according to claim 12, in which the residue inlet (2pdu) is in fluid communication with a source of a residual solution (Pr) which is aqueous and comprises phosphorus molecules in orthophosphate and / or polyphosphate form and undesirable volatilizable materials.
类似技术:
公开号 | 公开日 | 专利标题 BE1018702A3|2011-07-05|METHOD AND DEVICE FOR PRODUCING POLYPHOSPHORIC ACID BE1026163B1|2019-10-29|PROCESS FOR RECYCLING RESIDUAL SOLUTIONS COMPRISING PHOSPHORUS AND DEVICE FOR SUCH A METHOD EP2379445B1|2013-06-26|Method for the upgrading of the gas mixture from a deaerator associated with the production of a synthesis gas, and plant for implementing the same EA036132B1|2020-10-01|High efficiency process for degassing of hydrogen sulfide from liquid sulfur WO2019185702A1|2019-10-03|Method for recycling residual solutions comprising phosphorus and device for such a method WO1999058459A1|1999-11-18|Method for treating humid waste containing an oxidable organic material WO2019185698A1|2019-10-03|Method for producing polyphosphoric acid and device for such a method EP3489294B1|2020-10-28|Method for treatment of carbonated materials by vapothermolysis FR2824060A1|2002-10-31|METHOD AND DEVICE FOR PRODUCING HYDROGEN-CONTAINING GAS FROM HYDROGEN SULFIDE EP1916024A1|2008-04-30|Unit and process for treating refinery process wastewater FR2859483A1|2005-03-11|Cast iron manufacture includes collection of carbon dioxide from output gases from blast furnace and use of it in petroleum extraction WO2017013038A1|2017-01-26|Clc method and facility with production of high-purity nitrogen EP1080045B1|2002-07-17|Method for treating fluid liquid containing a volatile fraction EP3137813B1|2018-09-12|Layout of an outlet tuyere for a submerged plasma torch for waste treatment FR2611195A1|1988-08-26|Process for the purification of and overpressurisation of electrolytic fluorine FR2899597A1|2007-10-12|Production of fuel gas from organic/organo-halogen product in a form of liquid, gas/powder useful as energy source, comprises mixing the product with water to provide stoichiometric ratios between carbon atoms and oxygen mixtures EP1385623A1|2004-02-04|Method and installation for regenerating absorbents used for capturing sulphur dioxide in combustion fumes FR2681719A1|1993-03-26|Process and device for treating a liquid effluent originating from an industrial plant such as a nuclear power station, with a view to its removal
同族专利:
公开号 | 公开日 RS61669B1|2021-04-29| US20210009419A1|2021-01-14| ES2867953T3|2021-10-21| BE1026165B1|2019-10-29| IL277368D0|2020-11-30| MA52170A|2021-02-17| PL3546423T3|2021-09-13| BE1026163A1|2019-10-22| JP2021519254A|2021-08-10| JP2021519255A|2021-08-10| BE1026165A1|2019-10-22| EP3546423A1|2019-10-02| EP3774651A1|2021-02-17| BR112020019741A2|2021-03-02| US11161741B2|2021-11-02| BE1026150A1|2019-10-22| BE1026150B1|2019-10-29| IL277367D0|2020-11-30| CA3094317A1|2019-10-03| US20210130171A1|2021-05-06| BR112020019736A2|2021-02-17| CA3094281A1|2019-10-03| MA52171A|2021-02-17| EP3546423B1|2021-01-06| EP3774650A1|2021-02-17|
引用文献:
公开号 | 申请日 | 公开日 | 申请人 | 专利标题 US3272597A|1961-03-03|1966-09-13|Knapsack Ag|Apparatus for producing higher polyphosphoric acids| EP1421030B1|2001-08-09|2010-09-08|Innophos, Inc.|Method for making polyphosphoric acid| EP2411325B1|2009-03-26|2017-04-05|Prayon Technologies|Method and device for producing polyphosphoric acid| US3671202A|1964-02-21|1972-06-20|Allied Chem|Concentration of wet-process phosphoric acid| JP3743185B2|1998-12-11|2006-02-08|住友化学株式会社|Method for producing phosphoric acid| EP1172331B1|1998-12-28|2006-08-16|Toyo Boseki Kabushiki Kaisha|Method for purification of phosphoric acid| US6612906B2|2001-10-22|2003-09-02|David Benderly|Vibratory material removal system and method|
法律状态:
2019-11-27| FG| Patent granted|Effective date: 20191029 |
优先权:
[返回顶部]
申请号 | 申请日 | 专利标题 BE2018/5218A|BE1026150B1|2018-03-30|2018-03-30|PROCESS FOR PRODUCING POLYPHOSPHORIC ACID AND DEVICE THEREFOR| BE2018/5218|2018-03-30|MA052170A| MA52170A|2018-03-30|2019-03-27|PROCESS FOR RECYCLING RESIDUAL SOLUTIONS COMPRISING PHOSPHORUS AND DEVICE FOR SUCH A PROCESS| CA3094317A| CA3094317A1|2018-03-30|2019-03-27|Method for recycling residual solutions comprising phosphorus and device for such a method| EP19713470.3A| EP3774650A1|2018-03-30|2019-03-27|Method for recycling residual solutions comprising phosphorus and device for such a method| PCT/EP2019/057706| WO2019185702A1|2018-03-30|2019-03-27|Method for recycling residual solutions comprising phosphorus and device for such a method| BR112020019741-6A| BR112020019741A2|2018-03-30|2019-03-27|method for the purification of an aqueous waste solution containing phosphorus molecules and unwanted volatile materials and device for the production of purified phosphoric acid| JP2020551796A| JP2021519254A|2018-03-30|2019-03-27|A method for reusing a residual solution containing phosphorus and a device for this method| US17/041,681| US20210130171A1|2018-03-30|2019-03-27|Method for recycling residual solutions comprising phosphorus and device for such a method| IL277367A| IL277367D0|2018-03-30|2020-09-15|Method for recycling residual solutions comprising phosphorus and device for such a method| 相关专利
Sulfonates, polymers, resist compositions and patterning process
Washing machine
Washing machine
Device for fixture finishing and tension adjusting of membrane
Structure for Equipping Band in a Plane Cathode Ray Tube
Process for preparation of 7 alpha-carboxyl 9, 11-epoxy steroids and intermediates useful therein an
国家/地区
|