LIQUID-LIQUID PROCESS FOR EXTRACTING METALS USING ORGANO-PHOSPHOROUS COMPOUNDS

Abstract: The invention relates to a liquid liquid process for extracting metals from aqueous solution. The process comprises bridging into contact the aqueous solution with an organic phase containing at least one complex-forming agent insoluble in water and correspond­ ing to the general formula: in which Z¹ and Z² represent an oxygen atom or a sulphur atom and may be the same or different and R¹ and R² which may be the same or different represent straight or branched alkyl, cycloalkyl, aryl or aralkyl groups containing at least one electron-attracting group, to extract the metal from the aqueous solution The process is used to extract nickel, copper, uranium, molybdenum, lead cadmium, cobalt, iron, zinc, vanadium, tin and tungsten A second stage may be employed wherein the organic solution containing the metal is contacted with a second aqueous solution to strip the metal from the organic to the second aqueous solution

Description: EXTRACTION PROCESS The present invention relates to a process for extracting metals from an aqueous solution. This type of process is an important operation in the processing of ores by hydrometallurgical routes. One process at present used to extract a metal from its ore comprises comminution of the ore and then solubilisation of the metal values by a chemical treatment whereupon a pregnant leach liquor is produced. The liquor may then be contacted with an organic phase containing an extracting agent solubilised in a diluent in order to extract the metal values into the organic phase. Extraction comprises two operations: a first stage mixing of the two phases, which favours complex-formation and the transfer of the compound to be extracted from one phase to the other, and a second stage separation by natural or forced decantation. Generally speaking, the treatments to which the metal thus extracted is subjected, such as electrolysis or crystallisation, require an additional extraction of the metal from the organic phase, which is termed the de-extraction stage or "stripping". The properties of the complex-forming agent in hydrometallurgy depend on the nature of the two phases present, and also on the composition and the molecular structure of the said agent. The properties of the complexes formed and the selectivity of the extraction agent depend in particular on the molecular structure. It is known that organophosphoric acid derivatives of formula (RO) 2 POOH and organodithiophosphoric acid derivatives of formula (RO) 2PSSH form complexes with numerous metallic ions in an acid medium. Because of this they are used as complex-forming agents, especially in the extraction of nickel, uranium, zinc, cobalt, etc. It is also known that modifying the nature of the radical R in the compounds -of the formulae (RO)2 POOH or (RO)2 PSSH,can varythe inductiveeffect ofM on the P = S and P = 0 bonds, the angle of the Z-P-Z bond where Z represents 0 or S, and the interaction between the complexforming agent and the diluent and between the complexforming agent and the aqueous phase. These effects have repercussions on the stability of the metallic complex formed, on the kinetics of the reactions of formation or dissociation of the complexes, of mass transfer, on the solubility of the extraction agent in the two phases present and on the selectivity. The overall result of all these interactions is difficult to predict, since certain of them have opposite effects. Only experimentation will make it possible to assess the value and efficacy of a new extraction agent or to select its structure as a function of the problem to be solved. Moreover, it is often necessary to carry out leaching in an acid medium, and sometimes to operate at elevated temperature and under pressure. Lixiviating agents which have been used up to now have numerous disadvantages under these conditions, so that efforts have been made to develop lixiviating agents giving good yields and capable of working under these conditions. In certain cases it is desirable to be able to extract other metals in addition to the principal metal, thus helping to increase the profitability of a process and to render possible exploitation of a deposit which would otherwise not be sufficiently profitable if only the principal metal were extracted from it. The present invention therefore relates to a process for the extraction of metals, in the form of metallic salts in aqueous solution, by means of liquid-liquid extraction, by forming a complex with an extraction agent which is an organophosphoric acid and/or an organothiophosphoric acid or dithiophosphoric acid. Thus according to the present invention there is provided a process for the liquid-liquid extraction of metals from an aqueous solution wherein the aqueous solution is brought into contact with an organic solvent containing awaterinsolubleextractant of general formula: EMI3.1 wherein Z1 and z2 represent oxygen or sulphur atoms and may be the same or different and R1 and R2 which may be the same or different, represent straight or branched chain alkyl, cycloalkyl, aryl or arylalkyl groups containing at least one electron acceptor group, to extract the metal from the aqueous solution. Suitable electron acceptor groups include halogen, nitro, cyano, hydroxy, amino and alkoxy groups. Preferably the electron acceptor group is a chlorine atom. Preferably at least one of the groups ZÚ and Zê represents a sulphur atom. RÚ and Rê may be phenyl groups substituted by a halogen electron acceptor group and optionally by one or more alkyl groups containing 1 to 10 carbon atoms. Alkoxy groups, if present, preferably contain 1 to 4 carbon atoms, and most preferably are methoxy or ethoxy. Cycloalkyl groups, if present, preferably contain 3 to 10 carbon atoms. The compounds used in a process according to the invention are known per se and may be prepared by known methods. Dithiophosphoric acids may be prepared by the action of an alcohol or a phenol on phosphorus pentasulphide. Thiophosphoric acids may be prepared by the action of sulphur on a phosphide or of sodium hydroxide on a chloro-thiophosphate derivative. Phosphoric acids may be prepared by the action of an alcohol or phenol on phosphorus pentoxide and of water in the present of bromine and a tertiary amine on a phosphine. The extraction agents thus obtained may be purified by means of known purification methods, but they are preferably utilised in the crude form, which appreciably improves the kinetics of the extraction and/or de-extraction reactions, and also the physical properties of the phase mixtures (better decantation and better phase transfer). This improved activity of the phosphorus derivatives is probably a result of the presence in the reaction medium of polar or solvating derivatives such as excess alcohol, or mono- or poly-phosphorus secondary derivatives. The possibility of utilising the reaction mixture constitutes a further advantage of the invention and makes it possible to reduce the cost of the process. The process according to the invention can be applied to the extraction of any metal which forms a stable complex with the extracting agent and which dissolves in the organic phase. Suitable organic solvents are immiscible with water and under the chosen pH conditions are inert to acids, metal salts and the compound used as extraction agent. Preferred solvents are aliphatic, alicyclic and aromatic hydrocarbons such as hexane, heptane, cyclohexane, benzene, toluene, xylene, etc., chlorinated solvents such as carbon tetrachloride, chloroform, perchlorethylene, etc., ketones insoluble in water, esters, etc. Solvents frequently utilised alone or in a mixture with each other include crude oil or processed oil fractions with a high flash point, such as light naphtha, heavy naphtha, kerosene, paraffinic solvents and naphthenic solvents. The separation of the aqueous phase from the organic phase during the process according to the invention is promoted if a solvent is used which has a density which is distinctly different from that of the aqueous solution. The quantity of organic solvent used may vary over a wide range and depends on the quantity of metal to be extracted and the quantity of extraction agent employed. The volumetric ratio of the organic phase to the aqueous phase may vary between 10/1 and 1/10 for the extraction and approximately between 1/5 and 50/1 for the de-extraction (stripping). The preferred ranges lie between 5/1 to 1/2 for the extraction and 1/2 to 10/1 for the stripping. It is possible to improve still further the extraction and stripping reactions of the metals in the process according to the invention by adding a polar organic additive with a solvating effect such as a phosphate or thiophosphate, polyphosphate of an alcohol or an inorganic additive such as a neutral ammonium salt, or an alkali metal or alkaline earth metal salt. The process according to the invention may be applied to aqueous solutions resulting from the leaching of ores or from the processing of metal scrap or other residues containing metals resulting, for example, from acid treat ment, by using an acia such as sulphuric acid, sulphurous acid or hydrochloric acid. The process may also be applied to spent liquors containing metals resulting from electrolytic or chemical operations. The extraction and stripping of the metallic ions may be effected in conventional liquid-liquid extraction equip ment Preferred equipment comprises a mixing chamber in which the two liquids are thoroughly mixed by means of a suitable stirrer system and a separation chamber in which the two liquids are separated by virtue of their different densities. Extraction and stripping take place mainly at ambient temperature, but depending on the metal to be extracted or other metals present, it may be desirable, especially during stripping, to work at a temperature in the range 5 to 75 C. The operating pressure is generally atmospheric pressure, but it is also possible to work under a pressure of from 1 to 5 bar. The aqueous solution should be acidic and the pH is preferably less than 3. The process may be used in particular for the extraction of nickel, copper, uranium, molybdenum, lead, cadmium, cobalt, iron, zinc, vanadium, tin and tungsten. The invention is illustrated by the following examples. Example 1 The initial aqueous solution contained 5 g per litre of nickel in the form of sulphate. The pH of the aqueous solution which contained sulphuric acid was in the vicinity of 1. The organic solution contained a mixture of hydrocarbons. It had a density at 150 of 0.895 and a flash point above 650, and its aromatics content was greater than 97 per cent by weight. The ratio of the organic phase to the aqueous phase by volume was equal to 1 in the extraction stage. The reaction mixture resulting from the preparation of the compound of formula (RO)2 PSSH in which R designates the chlorophenyl group was used as the extractant. Diparachlorophenyl dithiophosphoric acid was prepared according to the following process: 124 g of parachlorophenol was introduced into a reactor provided with a stirrer and means for reflux. 49 g of phosphorus pentasulphide was added over 1 hour after having brought the flask to a temperature of 1500 C. The reaction was stopped after one hour's agitation at 150 C. After filtration a crude synthesis product was obtained containing four major products: - unreacted phenol ROH 10% - dithiophosphoric acid (RO)2P (S) SH 75% - trithiophosphoric acid RO P (S) (SH)2 8% - trisubstituted phosphate (R0)3PS 7 The content of dithiophosphoric acid of the solvent was 43 g/litre. The aqueous phase (250 ml) containing the nickel salt was placed in a separating funnel equipped with an agitator with vanes. The organic phase (250 ml) containing the extraction agent was then added. The phases were then agitated. Analyses by atomic absorption of the nickel contained in the aqueous phase made it possible to follow the metal extraction as a function of the time. At the end of a period "tes" = 10 mins, extraction equilibrium was reached. The extraction yield which corresponded to the quantity of nickel extracted in relation to the quantity of nickel initially present in the aqueous solution was equal to 74%. The stripping was carried out by bringing 250 ml of the organic phase thus obtained into contact for 10 minutes with 10 N HC1 in a volumetric ratio of 5:1. The stripping yield was equal to 99%. Example 2 to 9 By operating as described in Example 1 and also using the reaction mixture resulting from the preparation of the dithiophosphoric acid derivative, the following results were obtained: Table 1 EMI8.1 <tb> <SEP> Extraction <SEP> Agent <SEP> Extraction <SEP> Extraction <tb> <SEP> Example <SEP> (RO)2 <SEP> PSSH <SEP> Extraction <SEP> <tb> Agent <tb> <SEP> Nature <SEP> of <SEP> the <SEP> Radical <SEP> R <SEP> % <SEP> teq <tb> <SEP> g/litre <tb> <SEP> 2 <SEP> Chlorobutyl <SEP> 32 <SEP> 55 <SEP> 10 <SEP> min <tb> <SEP> 3 <SEP> 2, <SEP> 4-Dichiorophenyl <SEP> 40 <SEP> | <SEP> 51 <SEP> < 20 <SEP> sec <tb> <SEP> 4 <SEP> 2,4,5-Trichlorophenyl <SEP> 41 <SEP> 45 <SEP> < 20 <SEP> sec <tb> <SEP> 5 <SEP> 4-Chloro-3-methylphenyl <SEP> 52 <SEP> 63 <SEP> < 20 <SEP> sec <tb> <SEP> 6 <SEP> 4-Chloro-2-methylphenyl <SEP> 46 <SEP> 59 <SEP> < 30 <SEP> sec <tb> <SEP> 7 <SEP> 4-Chloro-2-isopropyl-5- <SEP> 60 <SEP> 53 <SEP> 5 <SEP> min <tb> <SEP> methylphenyl <tb> <SEP> 8 <SEP> 4-Bromophenyl <SEP> 18 <SEP> 20 <tb> <SEP> 9 <SEP> 4-Methoxyphenyl <SEP> 72 <SEP> : <SEP> 48 <tb> Example 10 A series of liquid/liquid extractions was carried out under the conditions stated in Example 1 but with a purified extraction agent: 2,4-dichlorophenyldithiophosphoric acid. For an extraction agent content of 47 g/litre, the extraction yield was 78% and the stripping yield was 21%. Example 11 A series of liquid/liquid extractions was carried out on monometallic sulphide containing 1 to 5 g/litre of metal at a pH of 1. The organic diluent was a hydrocarbon with an aromatic content of > 938. The extraction agents utilised were non-purified compounds. The aqueous phase (25 ml) and the organic phase (25 ml) were mixed in separating funnels placed on a mechanical agitator. For stripping, the volume ratio of the organic phase to the aqueous phase was 5:1. The operation was carried out using 25 ml of organic phase brought into contact in the same way as before with the aqueous phase. Table 2 EMI9.1 Extraction <tb> <SEP> Extraction <SEP> Agent <SEP> Extra- <SEP> Strip <tb> <SEP> Metal <SEP> Agent <tb> <SEP> (RO)2 <SEP> PSSH <SEP> action <SEP> ping <tb> Content <tb> Nature <SEP> of <SEP> the <SEP> Radical <SEP> R <tb> g/litre <SEP> Nature <SEP> of <SEP> the <SEP> Radical <SEP> R <SEP> g/litre <tb> Copper <tb> <SEP> 3 <SEP> 4-Chlorophenyl <SEP> 21 <SEP> 60 <SEP> 80 <tb> <SEP> 5 <SEP> 2,4,5-Trichlorophenyl <SEP> 94 <SEP> 98 <SEP> nd <tb> <SEP> 5 <SEP> 4-Chloro-4-methylphenyl <SEP> 52 <SEP> 76 <SEP> 36 <tb> <SEP> 5 <SEP> 4-Chloro-2-isopropyl- <SEP> 64 <SEP> 80 <SEP> 2.5 <tb> <SEP> 3-methylphenyl <tb> <SEP> Uranium <tb> <SEP> 1 <SEP> 4-Chloro-3-methylphenyl <SEP> 1 <SEP> 20 <SEP> | <SEP> 100 <tb> Example 12 By operating under the conditions of Example 11 and using the reaction product of Example 1, molybdenum, lead, cadmium and tin were extracted from aqueous solutions. Table 3 EMI10.1 Extraction <tb> <SEP> Extraction <SEP> Agent <SEP> Extra Metal <SEP> Agent <tb> <SEP> (RO)2 <SEP> PSSH <SEP> action <tb> Content <tb> Nature <SEP> of <SEP> the <SEP> Radical <SEP> R <tb> <SEP> g/litre <SEP> Nature <SEP> of <SEP> the <SEP> Radical <SEP> Rg/litre <SEP> % <SEP> <tb> Molybdenum <SEP> 0.89 <SEP> 4-Chlorophenyl <SEP> 1 <SEP> 5 <tb> Lead <SEP> 1.0 <SEP> 4-Chlorophenyl <SEP> 4 <SEP> 98 <tb> Cadmium <SEP> 1.0 <SEP> 4-Chlorophenyl <SEP> 6 <SEP> 98 <tb> Tin <SEP> 1.0 <SEP> 4-Chloro-3-methylphenyl <SEP> 4.5 <SEP> 52 <tb> Example 13 Treatments identical to those of Example 11 were carried out on several bimetallic sulphide solutions. The results are summarised in Table 4. Table 4 EMI11.1 Extra Extraction <SEP> Agent <SEP> Purity <tb> ction <SEP> Extraction <SEP> Stripping <tb> <SEP> Pair <SEP> of <SEP> (RO)2 <SEP> PSSH <SEP> After <tb> pH <SEP> Agent <tb> Metals <SEP> Nature <SEP> of <SEP> the <SEP> Strip Content <tb> Radical <SEP> R <SEP> Org. <SEP> Phase <SEP> Aq. <SEP> Phase <SEP> Org. <SEP> Phase <SEP> Aq. <SEP> Phase <SEP> ping <tb> g/litre <tb> Ni(5g/l) <SEP> / <SEP> Ni <SEP> Co <SEP> Ni <SEP> Co <SEP> Ni <SEP> Co <SEP> Ni <SEP> Co <tb> Ni <SEP> % <tb> Co(1g/l) <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <tb> 4-Chlorophenyl <SEP> 1 <SEP> 45 <SEP> 3.7 <SEP> < 0.05 <SEP> 1.3 <SEP> < 0.95 <SEP> 0.6 <SEP> < 0.05 <SEP> 15.5 <SEP> < 0.01 <SEP> 99.9 <tb> " <SEP> " <SEP> 3 <SEP> 34 <SEP> 2.8 <SEP> 0.5 <SEP> 2.2 <SEP> 0.5 <SEP> 1.88 <SEP> 0.49 <SEP> 4.62 <SEP> 0.05 <SEP> 98.9 <tb> 2,4,5-Trichloro <tb> 1 <SEP> 51 <SEP> 2.4 <SEP> 0.5 <SEP> 2.6 <SEP> 0.5 <SEP> 1.8 <SEP> 0.6 <SEP> 2.94 <SEP> 0.01 <SEP> > 99.7 <tb> phenyl <tb> 4-Chloro-31 <SEP> 28 <SEP> 1.7 <SEP> 0.2 <SEP> 3.3 <SEP> 0.8 <SEP> 1.1 <SEP> 0.19 <SEP> 3 <SEP> 0.05 <SEP> 98.4 <tb> methylphenyl <tb> " <SEP> " <SEP> 2 <SEP> 28 <SEP> 0.9 <SEP> 0.1 <SEP> 4.1 <SEP> 0.9 <SEP> 0.2 <SEP> 0.09 <SEP> 3.5 <SEP> 0.05 <SEP> 98.6 <tb> " <SEP> " <SEP> 3 <SEP> 45 <SEP> 2.5 <SEP> 0.5 <SEP> 2.5 <SEP> 0.5 <SEP> 1.8 <SEP> 0.49 <SEP> 3.5 <SEP> 0.05 <SEP> 98.6 <tb> Cu(3g/l)/ <SEP> Cu <SEP> Fe <SEP> Cu <SEP> Fe <SEP> Cu <SEP> Fe <SEP> Cu <SEP> Fe <tb> Cu <SEP> % <tb> Fe(2g/l) <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <tb> 4-Chlorophenyl <SEP> 1 <SEP> 34 <SEP> 2.9 <SEP> 0.05 <SEP> 0.1 <SEP> 1.95 <tb> " <SEP> " <SEP> 2 <SEP> 9 <SEP> 0.8 <SEP> < 0.01 <SEP> 2.2 <SEP> > 1.99 <SEP> 0.1 <SEP> < 0.01 <SEP> 3.5 <SEP> < 0.01 <SEP> > 97.7 <tb> " <SEP> " <SEP> 3 <SEP> 9 <SEP> 0.9 <SEP> < 0.01 <SEP> 2.1 <SEP> > 1.99 <SEP> 0.1 <SEP> < 0.01 <SEP> 4 <SEP> < 0.01 <SEP> > 99.7 <tb> 4-Chloro-31 <SEP> 7 <SEP> 0.5 <SEP> < 0.01 <SEP> 2.5 <SEP> > 1.99 <SEP> 0.41 <SEP> < 0.01 <SEP> 0.45 <SEP> < 0.01 <SEP> > 97.8 <tb> methylphenyl <tb> 2,4,5-Trichloro1 <SEP> 26 <SEP> 1.5 <SEP> < 0.01 <SEP> 1.5 <SEP> > 1.99 <SEP> 0.45 <SEP> < 0.01 <SEP> 5.25 <SEP> < 0.01 <SEP> > 99.8 <tb> phenyl <tb> Ni(5g/l)/ <SEP> Ni <SEP> Zn <SEP> Ni <SEP> Zn <SEP> Ni <SEP> Zn <SEP> Ni <SEP> Zn <tb> Zn <SEP> % <tb> Zn(1g/l) <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <tb> 4-Chlorophenyl <SEP> 1 <SEP> 1.8 <SEP> < 0.01 <SEP> 0.11 <SEP> > 4.9 <SEP> 0.89 <SEP> < 0.01 <SEP> 0.01 <SEP> < 0.01 <SEP> 0.5 <SEP> > 99.8 <tb> " <SEP> " <SEP> 2 <SEP> 1.8 <SEP> < 0.01 <SEP> 0.16 <SEP> > 4.9 <SEP> 0.84 <SEP> < 0.01 <SEP> 0.06 <SEP> < 0.01 <SEP> 0.5 <SEP> > 99.8 <tb> 4-Chloro-2-isopropyl-3- <SEP> 1 <SEP> 3 <SEP> < 0.01 <SEP> 0.08 <SEP> > 4.9 <SEP> 0.92 <SEP> < 0.01 <SEP> 0.07 <SEP> < 0.01 <SEP> 0.05 <SEP> > 83 <tb> methylphenyl <tb> " <SEP> " <SEP> 2 <SEP> 3 <SEP> < 0.01 <SEP> 0.2 <SEP> > 4.9 <SEP> 0.8 <SEP> < 0.01 <SEP> 0.1 <SEP> < 0.01 <SEP> 0.5 <SEP> > 98 <tb> Example 14 By proceeding in the same manner as that stated in Example 13 with a bimetallic sulphide solution the following results were obtained: Table 5 EMI12.1 <tb> <SEP> Extraction <SEP> Extrac- <SEP> Extraction <tb> <SEP> Pair <SEP> of <SEP> Agent <SEP> pH <SEP> tion <SEP> <tb> <SEP> Metals <SEP> (RO)2 <SEP> PSSH <SEP> pH <SEP> Agent <SEP> Org. <SEP> Phase <SEP> Aq. <SEP> <SEP> Phase <tb> <SEP> Nature <SEP> of <SEP> the <SEP> Content <tb> <SEP> Radical <SEP> R <SEP> g/litre <SEP> g/l <SEP> g/l <SEP> g/l <SEP> g/l <tb> Pb <SEP> (lg/l)/ <SEP> Pb <SEP> Zn <SEP> Pb <SEP> Zn <tb> Zn(lg/l) <tb> <SEP> 4-Chlorophenyl <SEP> 1 <SEP> 11 <SEP> > 0.98* <SEP> 0.64 <SEP> < 0.02 <SEP> 0.36 <tb> Zn(lg/l)/ <SEP> Cd <SEP> Zn <SEP> Cd <SEP> Zn <tb> Cd(lg/l) <tb> <SEP> 4-Chlorophenyl <SEP> 1 <SEP> 14 <SEP> > 0.995* <SEP> 0.7 <SEP> < 0.005 <SEP> 0.3 <tb> w <SEP> (lg/l)/ <SEP> W <SEP> Sn <SEP> W <SEP> Sn <tb> Sn(lg/l) <tb> <SEP> 4-Chlorophenyl <SEP> 1 <SEP> 11 <SEP> 0.8 <SEP> < 0.1 <SEP> 0.2 <SEP> > 0.9 <tb> * The complex is insoluble in the two phases and precipitated out. Example 15 A liquid/liquid extraction was carried out on a quaternary solution of metallic ions: Cu (lg/l) - Co (lg/l) - Zn (lg/l) - Ni (5g/1). The crude reaction product used was the product of the reaction between P2S5 and parachlorophenol The extraction agent contained essentially diparachlorophenyl dithiophosphoric acid. The concentration of the extraction agent was 11 g/litre. The operating conditions were those described in Example 11 (for the diluent, pH = 1, organic phase/aqueous phase = 1/1). The results were as follows: Table 6 EMI13.1 <tb> <SEP> Metal <tb> <SEP> Ni <SEP> I <SEP> Cu <SEP> Co <SEP> Zn <tb> Phase <tb> Extract <SEP> 0.1 <SEP> 0.99 <SEP> 0.1 <SEP> 0.1 <tb> Raffinate <SEP> 4.9 <SEP> 0.01 <SEP> 0.9 <SEP> 0.9 <tb> The extract was the organic phase and the raffinate the aqueous phase. Example 16 Further results obtained with organophosphoric acids under operating conditions as described in Example 11 are set out in the table below: Table 7 EMI13.2 <tb> <SEP> Extraction <SEP> Yield <SEP> After <tb> <SEP> (RO) <SEP> 2 <SEP> POOH <SEP> Metals <tb> Agent <SEP> 10 <SEP> min <tb> <SEP> R <SEP> Represents <tb> Agitation <tb> <SEP> g/litre <SEP> g/litre <tb> 4-Chlorophenyl <SEP> Pb <SEP> 1 <SEP> 1 <SEP> 40% <tb> 4-Chloro-2-isopropyl- <SEP> Mo <SEP> 0.78 <SEP> 8 <SEP> 82% <tb> 3-methylphenyl <tb> 4-Chloro-3-methyl- <SEP> V <SEP> 1 <SEP> 4 <SEP> 99% <tb> phenyl <tb> 4-Chloro-2-isopropyl- <SEP> V <SEP> 1 <SEP> 8 <SEP> 38% <tb> 3-methylphenyl <tb> The diparachlorophenyl phosphoric acid utilised above may be prepared in the following manner: : 67 g of parachlorophenol are introduced into a stirred flask equipped with reflux, and heated to 150 - 1600C and 14 g of phosphorus pentoxide are slowly added over 2 hours. The crude product is obtained by filtering the reaction medium. Depending on the apparatus used, it is sometimes advantageous to dissolve the phosphorus pentoxide in a suitable solvent and to add the alcohol after bringing the temperature to approximately 170 - 180 C. Example 17 The acid of the formula (RO)2 PSOH in which R designates the 4-chloro-3-methylphenyl group was contacted with aqueous solutions containing respectively nickel, copper and molybdenum in the proportions and under the conditions stated in Table 8 below. Table 8 EMI14.1 Extraction <tb> <SEP> Extraction <SEP> Agent <SEP> Extraction <tb> Metal <SEP> Agent <tb> <SEP> (RO)2 <SEP> PSOH <SEP> Agent <tb> Content <tb> <SEP> Nature <SEP> of <SEP> the <SEP> Radical <SEP> R <tb> g/litre <SEP> Nature <SEP> of <SEP> the <SEP> Radical <SEP> R <SEP> litre <SEP> <tb> Ni <SEP> 5 <SEP> 4-Chloro-3-methylphenyl <SEP> 52 <SEP> 61 <tb> Cu <SEP> 5 <SEP> 4-Chloro-2lmethylphenyl <SEP> 54 <SEP> 72 <tb> Mo <SEP> 0.63 <SEP> 4-Chloro-4-methylphenyl <SEP> 52 <SEP> 98 <tb> Example 18 An aqueous solution containing 2 g/litre of ferric iron acidified with sulphuric acid to a pH of 1 was treated as described in Example 11. The extractant used was di(2-chloro-4-nonylphenyl) phosphoric acid prepared by chlorinating 4-nonylphenol with chlorine in an aqueous medium in the presence of a Lewis acid catalyst. The resulting chlorinated phenol was then reacted with phosphorus pentoxide at 170 - 1900C and the product hydrolysed. An organic solution containing 80 g/litre of extractant was used. After 10 minutes stirring, the extraction yield was 808. Example 18 An aqueous solution containing 2 g/litre of zinc acidified with sulphuric acid to a pH of 1 was treated as described in Example 11. The extractant used was di(2-chloro-4-nonylphenyl) dithiophosphoric acid prepared by reacting 2-chloro-4nonylphenol with phosphorus pentasulphide at 1700C. An organic solution containing 20 g/litre of extractant was used. After 10 minutes stirring, the extraction yield was 95%.

Claims: Claims: 1. A process for the liquid/liquid extraction of a metal from an aqueous solution wherein the aqueous solution is brought into contact with an organic solvent containing a water insoluble extractant having the general formula: EMI16.1 wherein Z and Zê represent atoms of oxygen or sulphur and may be the same or different, R and Rê which may be the same or different, represent straight or branched chain alkyl, cycloalkyl, aryl or arylalkyl groups, containing at least one electron acceptor, to extract the metal from the aqueous solution. 2. A process according to Claim 1 wherein at least one of the groups Z1 and z2 represents a sulphur atom. 3. A process according to Claim 1 or 2 whereby the electron acceptor is a halogen, nitro, cyano, hydroxy, amino or alkoxy group. 4. A process according to Claim 3 whereby the electron acceptor is a chlorine atom. 1 2 5. A process according to Claim 1 wherein Z and z2 represent oxygen atoms and the electron acceptor group is a nitro, cyano, hydroxy or amino group. 6. A process according to Claim 1, wherein Z and Zê represent oxygen atoms and R and Rê are phenyl groups substituted by a halogen electron acceptor group and optionally one or more alkyl groups containing 1 to 10 carbon atoms. 7. A process according to any of Claims 1 to 6 whereby the reaction mixture obtained by reaction of an alcohol, a phenol or amixed alcohol-phenol with phosphorus pentasulphide or phosphorus pentoxide is used as the extractant without purification. 8. A process according to any of Claims 1 to 7 wherein the organic solvent is selected from the group consisting of aliphatic and aromatic hydrocarbons, halogenated hydro carbons, water insoluble ketones, esters and high flash point petroleum distillates. 9. A process according to any of Claims 1 to 8 wherein the organic solution containing the metal is contacted with a second aqueous solution to strip the metal from the organic to the second aqueous solution. 10. A process according to any of Claims 1 to 9 whereby the ratio of the volume of the organic to the aqueous phase is between 10:1 and 1:10 for the extraction stage and between 1:5 and 50:1 for the stripping stage. 11. A process according to any of the Claims 1 to 10 wherein an organic polar additive or an inorganic additive is added to the organic solvent. 12. A process according to Claim 11 wherein the organic additive is a phosphate, thiophosphate or polyphosphate of an alcohol and the inorganic additive is a neutral salt of ammonia, an alkali metal or an alkaline earth metal. 13. A process according to any of Claims 9 to 12 wherein the second aqueous solution is acidic. 14. A process according to Claim 13 wherein the pH of the second aqueous solution is less than 3. 15. A process according to any of Claims 1 to 14 wherein the process is carried out at a temperature in the range to 75 0C. 16. A process according to any of Claims 1 to 15 wherein the process is carried out at a pressure in the range 1 to 5 bars. 17. A process according to any ofClaims lto 16wherein the first aqueous solution initially contains one or more of the following metals: nickel, copper, uranium, molybdenum, lead, cadmium, cobalt, iron, zinc, vanadium, tin and tungsten.

Inventors: VENTRON, GILBERT SOCIETE FRANCAISE DES PETROLES BP, Ventron, Gilbert Société Française des Pétroles BP
Applicants: THE BRITISH PETROLEUM COMPANY P.L.C.
Application year: 1980
Main classification: C22B3
IPC codes: B01D11, C22B13, C22B19, C22B15, C22B3, C22B17, C22B34, C22B23, C09K3, C22B25