PROCESS FOR THE PRODUCTION OF HIGH-PURITY IRON OXIDE

Abstract: Described is a process for the production of high-purity iron oxide comprising: A step of contacting an iron ions-containing organic solution containing one or more compounds selected from the group consisting of alkyl phosphoric acids, alkyl and aryl dithio phosphoric acids, carboxylic acids and hydroxyoximes together with a petroleum hydrocarbon as a diluent with an aqueous solution containing one or more compounds selected from the group consisting of HF, NH₄HF₂ and NH₄F to obtain ammonium iron fluoride or iron fluoride, and a step of heating the ammonium iron fluoride or iron fluoride obtained in a gas atmosphere containing oxygen or water.

Description: n Process for the Production of High-Purity Iron Oxide " This invention relates to a process for the production of high-purity iron oxide. High-purity iron oxide (Fe203) is generally obtained by heating high-purity iron sulphate or chloride, or metallic iron, in an oxygen athmosphere. Its production on an industrial scale is not yet economical. It is therefore an object of this invention to provide an economical process of the production of high-purity iron oxide. Thus the invention relates to a process for producing high-purity iron oxide comprising: a step of contacting an iron ions-containing organic solution containing one or more compounds selected from the group consisting of alkyl phosphoric acids, alkyl and aryl dithio phosphoric acids, carboxylic acids and hydroxyoximes and a petroleum hydrocarbon as a diluent with an aqueous solution containing one or more compounds selected from the group consisting of HF, N114HF2 and NII4F to obtain ammonium iron fluoride or iron fluoride; and a step of heating the ammonium iron fluoride or iron fluoride obtained in a gas atmosphere containing oxygen or water. The particle size of the high-purity iron oxide produced by the process of this invention depends on the crystal size of ammonium iron fluoride or iron fluoride prior to thermal decomposition and consequently uniformity and sizing of the particle can be unrestrictedly attained. Moreover, starting materials are not particularly limited due to utilization of any aqueous solution containing iron ions and economical advantages can be obtained because waste acid is regenerated by removal of iron ions therefrom. Starting materials are also obtained from the iron removal step of nonferrous metallnrgy or the reprocessing step of sludge or slag. These starting materials are subjected to solvent extraction and the resulting ammonium iron fluoride or iron fluoride is subjected to repeated recrystallization to obtain the desired degree of purity. Ammonium iron fluoride and iron fluoride used as a starting material in the present invention are obtained in the following sequential steps: 1. The first step in which iron ions in feed solutions are extracted into an organic phase by contact with an organic solution containing one or more compounds selected from the group of alkyl phosphoric acids, alkyl or aryl dithio phosphoric acids, carboxylic acids and hydroxyoximes (hydroximes) together with a petroleum hydrocarbon (a liquid hydrocarbon solvent) as a diluent. 2. The second step in which ammonium iron fluoride and iron fluoride are formed by bringing the resulting organic solutionne. the extract,into contact with a stripping agent containing one or more compounds selected from HF, sa4HF2 and NH4F and then those are filtered off. The reactions can be illustrated by the following equation: R3Fe + 3HF # 3R H + FeF3+ R3Fe + 3NH4HF2 # 3R H + (NH4)3FeF6# R3Fe + 6NH4F # 3R NH4 + (NH4)3FeF6+ where R-H and R-µH4 indicate proton-type and NE4-type extractants. Ammonium iron fluoride used in this invention is not limited to be in the form of (NH4)3FeF6, but also includes (NH4)2FeF5 and other cbmpositions containing + different ratios of NH4 ions to F ions or mixed crystals of iron fluoride and ammonium fluoride It is preferred to use the following aqueous solutions for extracting iron ions from the organic solution: (1) Solutions containing not less than 40 g/t of HF; (2) Solutions containing not less than 30 g/t of NE4F; and (3) Solutions containing not less than 40 g/l of NH4HF2. Needless to say the solution may contain HF, NH4F and NH4HF2 in mixture. The temperature does not influence the stripping operation to a significant degree. Iron ion extraction into the organic solution defined in this invention can be performed by bringing an aqueous HC1, H2S04, HNO, CE3COOH or HNO) + HF solution containing iron ions into contact with an organic solution containing one or more compounds selected from the group of alkyl phosphoric acids, alkyl or aryl dithio phosphoric acids, carboxylic acids and hydroxyoximes (hydroximes) together with a petroleum hydrocarbon as a diluent. The pH value of the aqueous feed solution for extraction of iron ions generally ranges from -1 to 7. The extraction from strongly acidic aqueous solutions is preferred for the production of high-purity iron oxide because extraction of heavy metall ions other than iron ions is negligible in this case. Of course, the purity of iron product extracted at a pH range of 2 to 7 can be maintained at high levels by repeated scrubbing or washing prior to back-extracting the iron ions present in the organic solvent. Furthermore, the purity can be improved by repeated dissolution and crystallization of the crystalline-ammonium iron fluoride or iron fluoride after stripping with HF, NH4HF2 or NH F This is especially remarkable in the case of ammonium iron fluoride having high crystallization tendency. As shown in the following equation, iron oxide is obtained by thermal decomposition of ammonium iron fluoride or iron fluoride in a water or oxygen containing gas stream. 3 1 (NH4)3FeF6 + 4 92 # 3NH4F# + 3F + 2 Fe2O3 3 1 (NH4)3FeF6 + 2 H2O # 3NH4F# + 3flF+ + 2 Fe2O3 FeF3 + 2 O2 # 3F# + 1Fe3O4 3 3 3 1 FeF3 + 2 H20 + 3HFf + 2 Fe203 It is noted that the above equations show one example of iron oxides obtained by the present invention and the chemical species of iron oxide obtained in the process of this invention are not limited to the above example. The extractants usable to extract iron ions in this invention are as follows: The alkyl phosphoric acids are selected from the compounds (A) - (F) shown below: EMI5.1 where R is an alkyl group containing from about 4 to 14 carbon atoms. D2SHPA (di-2-ethyl hexyl phosphoric acid) shown in the example set forth hereinafter belongs to the (A) group having as an alkyl group the C8H17 group. The -alkyl or aryl dithio phosphoric acids used in this invention include the compounds (G) shown below: EMI5.2 where R is an alkyl group having from about 4 to 18 carbon atoms or an aryl radical having up to 18 carbon atoms. D2EHD?PA (di-2-ethyl hexyl dithio phosphoric acid) shown in the example set forth hereinafter has the C8H17 group. The carboxylic acids used in this invention include the compounds (H) and (I) shown below: EMI6.1 where R is an alkyl group having from about 4 to 18 carbon atoms. Versatic acid 10 (V-i 0) shown in the example belongs to the (H) group having alkyl groups with 9 to 11 carbon atoms. The hydroxyosimes used in this invention include compounds (J) shown below: EMI6.2 where R is EMI6.3 or EMI6.4 and X is Cl or H. where R is a hydrogen atom, a methyl, phenyl or benzyl group and X is a chlorine or hydrogen atom. Of course similar salicylaldoximes may be used. SME-529 (tradename, produced by Shell Chemical Cho. 3 used in the example is a hydroxyoxime of the formula (J) in which R = CH3. The liquid petroleum hydrocarbons used in the process this of/invention are aliphatic, alicyclic, aromatic or aromatic-aliphatic hydrocarbons or mixtures of these compounds. Technical mixtures of various liquid petroleum base hydrocarbons such as kerosene are often used. Although the concentration of the extractant in the organic solvent depends on the iron ion concentration and the kind or concentration of anions and heavy metal ions extracted other-than iron ions in the solution to be treated, it usually lies in the range of 2 to 90 volume %. Iron ions to be extracted into an organic solution according to the process of this invention are obtained by contacting any desired aqueous solution from various sources such as iron removal processes in nonferrous extraction hydrometallurgy or waste acids obtained from surface treatment processes (pickling) of metallic materials and products with an drganic solution containing one or more compounds selected from the group of alkyl phosphoric acids, alkyl or aryl dithio phosphoric acids, carboxylic acids and hydroxyoximes and a liquid petroleum base hydrocarbon as a diluent. Brief Description of the Drawings: Fig. 1 is a flow-sheet of the process for the production of high-purity iron oxide according to the present invention. Fig. 2 is a flow-sheet of the process for the production of high-purity iron oxide from various aqueous solutions containing iron ions according to the present invention. Fig. 3 is a graph showing a thermal decomposition curve of ammonium iron fluoride in an oxygen gas stream. Fig. 4 is a graph showing the ratio of the amount of 4HF2 contained in a stripping agent and the iron tripping percentage by one contact. The present invention will be described in more detail with reference to the accompanying drawings. Of course, this invention is not limited to these embodiments. As shown in the flow-sheet of Fig. 1, high-purity iron oxide (S) is obtained by bringing an organic solvent (A) containing iron ions into contact with a stripping agent (B) containing at least one of NH4HF2, HF and NH4F in the stripping zone (H) and then by heating ammonium iron fluoride or iron fluoride obtained in the separation stage (C) in a water or oxygen containing gas stream in the thermal decomposition zone (E). The flow-sheet shown in Fig. 2 illustrates the production of high-purity iron oxide from an aqueous solution containing iron ions. Iron ions are extracted into an organic phase by by aging the aqueous solution (J) containing iron ions into contact with the organic solvent (A) in the extraction zone (K). The resulting organic solution into which iron ions have been extracted is stripped or back-extracted by contacting with a stripping solution (B) in the stripping zone (H) and ammonium iron fluoride or iron fluoride formed in the separation stage (C) is filtered off. Iron oxide is produced by heating the separated ammonium iron fluoride or iron fluoride in a water or oxygen containing gas stream in the thermal decomposition zone (E) according to the following equation: 3 1 (NH4)3FeF6 + 2 H20 3NH4F+ + 3HF+ + 2 Fe2O3 2 3 1 FeF3 + 2 O t 3Ff + 2 Fe2O3 NH4F, HF and F gases generated in the thermal decomposition zone are absorbed in water and reused for extracting iron ions from the organic phase. The present invention has the following advantages. (1) Production of high-purity iron oxide is simplified, thus enlarging its utility as electronic material (2) Removal of iron in nonferrous extractive hydrometallurgy can be economically carried out and recovery efficiency can be enhanced by controlling loss of other coexisting metals. (3) When applied to treatments of industrial wastes containing large amounts of iron and other valuable metals, the metal values can be recovered with great economical advantage. (4) When applied to recovery of waste acids used in surface treatments of metallic-materials and products, it facilitates control of pickling processes and it makes recycle of acids economically possible. The following examples illustrate preferred embodiments. Example 1 The thermal decomposition curve was investigated by gradually heating 100 mg of ammonium iron fluoride ftNH4)3FeF in a gas stream (air) containing oxygen. The observed change in weight at a temperature rising rate of 7 C/min. is shown in Fig. 3.Iron oxide of a purity at least of 99.999% was quantitatively obtained by heating up to 60000. As shown in Fig. 3, the thermal decomposition starts at about 180 - 2300C and iron fluoride is formed. Thermal decomposition proceeds further at 280 - 320 C and iron oxide is formed at 350 - 45O0C. The ammonium iron fluoride used in this example was prepared by the following process. Fe ions in inorganic acids are extracted into an organic solvent comprising 30% i2EHPA as an extractant together with 70% of an isoparaffine as a diluent. Then crystalline ammonium iron fluoride is precipitated by contacting the resultant organic solution with a stripping solution containing 100 g/l of NH4HF2. The precipitate is filtered off. The ammonium iron fluoride obtained is washed successively with isopropyl alcohol, ethanol and acetone, in that order and is left in a desiccator maintained at 1100C for one hour. Analysis of this sample after dissolving it in hydrochloric acid is shown below: Fe g NH4 H20 Mole number 1 5.72 2.68 0.88 Mole ratio 1 : 6 : 3 : 1 Although D2EHPA is used as the extractant in this example, (NR4)3FeF6 can be obtained by using other organic solutions from which the iron ions can be extracted with a stripping solution containing NH4HF2. An example is shown in Table 1. Stripping conditions are as follows: Stripping agent: 100% NH4HF2 Temperature: 28.50C Contact time: 10 minutes O/A = 1.0 Table 1 Concentration of 20% X2EHPA extractant 50% OPPA 40% V-10 + 308 OPPA* Fe concentration in organic phase after stripping 0.2 g/Q < 0.01 g/l 0.3 g/l Stripping percentage 97.1% about 100% 90.7%. Concentation of 10% OPPA 10% SME-529** extractant 30% D2EHDTPA + 30% V-10 + 30% D2EHPA Fe- concentration in organic phase after stripping 1.4 g/l < 0.01 g/Q 0.3 g/l Stripping percentage 79.7% about 100% 89.6% * OPPA (octyl phenol phosphoric acid) ** SME-529 (tradename, produced by Shell Chemical Co., hydroxime) It is proved from the analysis that the precipitate obtained by these operations is ammonium iron fluoride. As shown in Fig. 4, the solubility of ammonium iron fluoride is dependent on the concentration on NE4HF2 and consequently the total amount of iron stripped from the organic phase is not converted into ammonium iron fluoride. Example 2 Iron ions in the organic solvent can be transferred into the aqueous phase by contacting with an aqueous solution containing only HF, as shown in the following equation: R3Fe + 3HF ' 3RH + FeF3+ HF concentration of at least 40 g/l is suitable for the precipitation of FeF3. The thermal decomposition of the obtained FeF3 starts around 250 - 280 C in oxygen or water containing gas stream and the reaction is completed during heating up to 600 C. The accomplishment of thermal decomposition at around 400 C was proven experimentally by repeated tests. The thermal decomposition reaction proceeds according to the following equation. The form or modification-of the iron oxide obtained is not limited to be in form of Fe203 as shown in this equation. FeF3 + 3 O2 + 3Ft + 1 Fe203 4 2 FeF3 + H2O c 3HF +1 Fe 203 2 2 HF gas generated in the thermal decomposition is absorbed in water and reused for further stripping of iron ions from the organic solution. FeF3 used in this example is prepared by the following process. Fe3+ ions in an aqueous solution are extracted into an organic solvent comprising 30 volume % D2SHPA together with an isoparaffine as a diluent. Then crystalline iron fluoride is precipitated by contacting the resulting organic solution with stripping solutions containing 50 g/l HF, 75 g/l HF and 100 g/l HF, respectiviy. The results are shown in Table 2. Table 2 EMI13.1 <tb> <SEP> Extractant <tb> <SEP> 30% <SEP> V-10 <SEP> 30% <SEP> D2EHPA <SEP> 30% <SEP> D2EHDTPA <tb> Strippingagen <tb> HF <SEP> 50 <SEP> g/Q <SEP> < 0.1 <SEP> gtQ <SEP> 1.2 <SEP> g/Q <SEP> 1s55 <SEP> git <tb> <SEP> (about <SEP> 100%) <SEP> (61.4%) <SEP> (20.496) <tb> HF <SEP> 75 <SEP> g/Q <SEP> < 0.1 <SEP> g/Q <SEP> 0,1 <SEP> g/Q <SEP> 1.0 <SEP> g/g <tb> <SEP> (about <SEP> 11)O%) <SEP> (96.8%) <SEP> (53.2%) <tb> HF <SEP> 100 <SEP> g/Q <SEP> -.C0.1 <SEP> ( <SEP> (0.1 <SEP> g/± <SEP> 0.15 <SEP> g/g <tb> <SEP> (about <SEP> 100%). <SEP> .(about <SEP> 100%) <SEP> (926) <tb> Stripping conditions: Contact time: 10 minutes O/A = 1.0 The data indicate the iron content in the organic phase after stripping. As shown in Table 2, V-10 and D2EHD2PA as an extractant besides D2EHPA can be used for the preparation of FeF3. Furthermore, Fe?3 can be prepared.as a white precipitate by an alternative process in which an iron containing starting material is dissolved in an aqueous solution containing HF followed by an oxidation process. This white precipitate is analyzed as BeS3.nE20. As described above, the preparation of FeF3 and (NR4)3FeF6 is not limited to the solvent extraction technique. Example 3 Extraction results of iron ions from the following aqueous solutions using various extractants are shown in Table 3. Extraction conditions: Initial iron concentration in the aqueous phase: 18.1 - 18.4 g/l Contact time: 10 minutes Temperature: 28.5 C O/A = 1.0 The contact time has a considerable influence on the amount of extracted iron ions. Table 3 EMI14.1 <tb> <SEP> 300 <SEP> g/l <SEP> H2SO4 <SEP> 210 <SEP> g/l <SEP> HCl <SEP> 150 <SEP> g/l <SEP> HNO3 <SEP> + <SEP> <tb> <SEP> 30 <SEP> g/l <SEP> HF <tb> <SEP> Extracted <SEP> Extracted <SEP> Extracted <SEP> <tb> <SEP> amount(g/l) <SEP> % <SEP> amount(g/l) <SEP> % <SEP> amount(g/l) <SEP> % <SEP> <tb> 30% <SEP> D2EHPA <SEP> + <tb> <SEP> 708 <SEP> n-paraffine <SEP> 10.2 <SEP> 56.4 <SEP> 8.3 <SEP> 43.9 <SEP> 10.4 <SEP> 57.1 <tb> 30% <SEP> D2EHDTPA <SEP> + <tb> <SEP> 70% <SEP> n-paraffine <SEP> 17.2 <SEP> 95.0 <SEP> 17.0 <SEP> 89.9 <SEP> 17.4 <SEP> 95.6 <tb> 208 <SEP> D2EHPA <SEP> + <SEP> 30% <SEP> OPPA <tb> <SEP> + <SEP> 50% <SEP> kerosene <SEP> 9.1 <SEP> 50.3 <SEP> 4.9 <SEP> 25.9 <SEP> 9.2 <SEP> 50.5 <tb> 20% <SEP> D2EHDTPA <SEP> + <tb> <SEP> 308 <SEP> V-10 <SEP> + <tb> <SEP> 50% <SEP> kerosene <SEP> 9.6 <SEP> 53.0 <SEP> 7.9 <SEP> 41.8 <SEP> 8.9 <SEP> 48.9 <tb> 50% <SEP> OPPA <SEP> + <tb> <SEP> 50% <SEP> isparaffine <SEP> 9.9 <SEP> 54.7 <SEP> 4.1 <SEP> 21.7 <SEP> 9.2 <SEP> 50.5 <tb> 10% <SEP> V-10 <SEP> + <tb> <SEP> 30% <SEP> D2EHPA <SEP> + <tb> <SEP> 60% <SEP> isoparaffine <SEP> 10.2 <SEP> 56.4 <SEP> 8.2 <SEP> <SEP> 43.4 <SEP> 10.5 <SEP> 57.7 <tb> The data shown in Table 3 indicate the amount of iron extracted into the organic phase and its extraction percentage. As explained above iron ions extracted into an organic phase are stripped into an aqueous phase by means of the same method described in Examples 1 and 2 and iron oxide can be obtained by heating the resultant ammonium iron fluoride or iron fluoride in gas stream containing oxygen or 1120. The present invention thus relates to a process for the production of iron oxide according to the following sequential steps: (1) Iron ions contained in any aqueous solution are extracted into an organic phase with contact of an organic solvent containing one or more compounds selected from the groups of alkyl phosphoric acids, alkyl or aryl dithio phosphoric acids, carboxylic acids and hydroxyoximes together with a petroleum base hydrocarbon as a diluent; (2) ammonium iron fluoride or iron fluoride is obtained by stripping iron ions in the resulting organic solution with a stripping agent containing one or more compounds selected from HF, NH4HF2 and NR4F; ; (3) iron oxide is produced by heating the resulting ammonium iron fluoride or iron fluoride in gas stream containing oxygen or 1120. NE4B, HF, KH3 and F gases generated in the thermal decomposition may be absorbed in water and this absorption solution is reused for stripping the iron ions present in the organic phase. Lowering of the reagent cost, which is required for stripping iron ions in the organic phase, achieved by recycling HF, NH4? and NH4HF2 as described above and control of water balance in the stripping solution decrease the production costs for iron oxide from the iron ions and consequently make this invention an economical process.

Claims: What is claimed is: 1. A process for producing high-purity iron oxide comprising: A step of contacting an iron ions-containing organic solution containing one or more compounds selected from the group consisting of alkyl phosphoric acids, alkyl and aryl dithio phosphoric acids, carboxylic acids and hydroxyoximes and a petroleum hydrocarbon as a diluent with an aqueous solution containing one or more compounds selected from the group consisting of HF, NE4HF2 and NR4F to obtain ammmonium iron fluoride or iron fluoride; and a step- of heating the ammonium iron fluoride or iron fluoride-obtained in a gas atmosphere containing oxygen or water. 2. A process according to Claim 1 in which an aqueous solution of ECl, 112SO4, HE03, CH3COOH or HNO3 + H? containing iron ions is brought into contact with an organic solution containing one or more compounds selected from the group consisting of alkyl phosphoric acids, alkyl and aryl dithio phosphoric acids, carboxylic acids and hydroxyoximes together with a petroleum hydrocarbon as n diluent to obtain the iron ionscontaining organic solution.

Inventors: NISHIMURA, SANJI, WATANABE, MORIO
Applicants: SOLEX RESEARCH CORPORATION OF JAPAN
Application year: 1981
Main classification: C01G49
IPC codes: C21B15, C01G49, B01D11