Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
  • C07F7/00—Compounds containing elements of Groups 4 or 14 of the Periodic Table
  • C07F7/22—Tin compounds
  • C07F7/2208—Compounds having tin linked only to carbon, hydrogen and/or halogen
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
  • C07F7/00—Compounds containing elements of Groups 4 or 14 of the Periodic Table
  • C07F7/22—Tin compounds
  • C07F7/2296—Purification, stabilisation, isolation

Definitions

• the present invention relates to an improved process for purifying monooctyltin trichloride.
• monoalkyltin trichlorides RSnCI 3
• RSnCI 3 monoalkyltin trichlorides
• methyltin, butyltin, and octyltin compounds are technically particularly important.
• the monoalkyltin compounds (RSnX 3 , with only one alkyl group bound to tin) have generally the lowest toxicity, and are considered non-toxic based on present standards.
• diorganotin compounds R 2 SnX 2
• triorganotin compounds R 3 SnX
• the European Union restricted the maximum tolerated concentration of triorganotin compounds in all consumer goods to a maximum level of 0.1 % (by weight) as from July 1 , 2010.
• the European Union decided to specifically restrict the maximum tolerated concentration of dibutyltin and dioctyltin compounds in some types of consumer goods to 0.1 % (by weight) as from January 1 , 2012, and in further types of consumer goods to 0.1 % (by weight) as from January 1 , 2015.
• monoalkyltin compounds comprising very low levels of undesired diorganotin and triorganotin compounds. More specifically, monooctyltin compounds comprising levels of less than 0.3 % of dioctyltin dichloride and less than 0.1 % trioctyltin chloride impurities are required.
• a first step wherein higher alkylated tin compounds (di- tri-, ortetraorganotin compounds, or mixtures of them) are formed by alkylation of inorganic tin compounds;
• alkylated alkyl tin compounds are reacted with tin tetrachloride (stannic (IV) chloride, SnCI 4 ) in order to form mixtures containing monoalkyltin trichlorides (this general procedure is sometimes called redistribution, scrambling, or comproportionation).
• tin tetrachloride stannic (IV) chloride, SnCI 4
• a fundamental drawback of this process is that it does not yield monoalkyltin trichlorides comprising low levels of diorganotin and triorganotin compounds.
• redistribution does not start from diorganotin, but from tri- or tetraorganotin compounds, stoichiometric amounts of diorganotin compounds are formed as byproducts, and remain in the product mixture.
• the amount of dibutyltin dichloride by-product is at least 33 %.
• US 6 768 017 suggests adding transition metal-based catalysts in order to facilitate a kinetically hindered redistribution of diorganotin compounds with SnCU so as to form monoalkyltin trichlorides.
• the only catalysts demonstrated to work according to US 6 768 017 are compounds of precious metals (Pd or Pt). It remained, however, unproven that said catalysts could be satisfactorily recovered after reaction and be re-used. This process appears economically unattractive, because reported yields are unsatisfactory, reported selectivity is low, reported reaction times are long, and it requires expensive catalysts.
• US 7 592 472 suggests producing monoalkyltin trichlorides by reaction of SnCI 2 , alkenes and HCI in the presence of transition metal-based catalysts.
• the only catalysts demonstrated to work are compounds of precious metals (Pd or Pt) used in a high concentration, and it remained unproven that said catalysts could be satisfactorily recovered after reaction, and re-used. This process appears economically unattractive, because reported yields are unsatisfactory, reported selectivity is low, and it requires expensive catalysts.
• GB 1 501 673 and US 6 846 944 teach that mixtures of monoalkyltin trichlorides and diorganotin dichloride compounds can be prepared by partial alkylation of SnCU with aluminum alkyl donor complexes.
• preferred aluminum alkyl donor complexes are complexes of trialkylaluminum compounds (AIR 3 ) with ethers. Also the method described in these documents does not allow direct production of monoctyltin trichloride with the desired low levels of dioctyltin and trioctyltin compounds.
• a preferred method of separation is a fractional distillation (this is possible, because the vapor pressure of monobutyltin trichloride is acceptably high and separation factors of dibutyltin dichloride are high). But it is also possible to selectively dissolve the monobutyltin trichloride in water and to recover it later from the aqueous solution (this is possible, because monobutyltin trichloride is miscible with water, while dibutyltin dichloride is practically insoluble in water).
• monooctyltin trichloride comprising very low levels of dioctyltin and trioctyltin compounds can be obtained from organotin chloride mixtures comprising monooctyltin trichloride, said process comprising the following steps:
• phase separation step (2) separating the resulting aqueous phase which is rich in monooctyltin chloride from the organic phase containing most of the dioctyltin and trioctyltin compounds (in the following this step will also be referred to as "phase separation" step);
• the present invention provides a process for producing monooctyltin trichloride comprising very low levels of dioctyltin and trioctyltin compounds, said process comprising the following steps:
• phase separation step (2) separating the resulting aqueous phase which is rich in monooctyltin chloride from the organic phase containing most of the dioctyltin and trioctyltin compounds (in the following this step will also be referred to as "phase separation" step);
• monooctyltin trichloride can be produced by monoalkylation of tin
• tetrachloride with trioctyl aluminum in form of a donor complex with an ether or a tertiary amine.
• monooctyltin trichloride can also be produced by a redistribution reaction of tin tetrachloride with tetraoctyltin, such as by a process as described in US 3 248411.
• Suitable aluminum trioctyl aluminum compounds to be used according to the present invention are e.g., tri-n-octylaluminum, and tri-iso-octylaluminum.
• Suitable donor complexes of the trioctyl aluminum compound include, for example, complexes with symmetrical or asymmetrical, saturated or unsaturated, linear or branched aliphatic, aromatic or cyclic ethers or amines.
• Factors for choosing the appropriate ether or amine are, e.g.: commercial availability, costs, safety properties (flammability, flash point, toxicity, tendency to form hazardous peroxides), physical properties (water solubility, freezing point, boiling point, vapor pressure), ease of separation form the products, and ease of recycling.
• Suitable ethers and amines are diethyl ether, di-n-butyl ether, methyl- tert.-butyl ether, tetrahydrofuran, dioxane, anisole, and triethylamine, pyridine and dimethyl-aniline.
• Some donor complexes for example, those with tetrahydrofuran or pyridine, alkylate SnCI 4 to form a mixture of products RnSnCU-n wherein n represents 1 to 4 and R represents an alkyl group as defined above, but in which the alkyl-tin trichloride is the main constituent.
• SnC starting material is also used as an etherate complex.
• Complexes of SnCU with other ethers or with amines may also be used.
• the reaction usually is carried out in such a way that the tin tetrachloride is initially placed in the reaction vessel, whereupon the donor complex of the trioctyl aluminum compound is added thereto.
• the tin tetrachloride is initially placed in the reaction vessel, whereupon the donor complex of the trioctyl aluminum compound is added thereto.
• the solvent may be an inert organic solvent, such as hexane, isooctane, benzene, toluene, kerosene, cyclohexane, chlorobenzene etc.
• a suitable other solvent e.g., an ether, such as tetrahydrofuran, diethylether, or dibutylether, may also be used.
• a catalyst may or may not be included in the reaction. In a preferred embodiment, no catalysts, such as precious metal catalysts, are included in the reaction medium.
• the reaction is usually conducted at a temperature range of from 5 °C to less than 35 °C, preferably at a temperature range of from 10 to 30 °C, especially 20 to 25 °C, more especially 22 to 25 °C.
• the tin tetrachloride starting material is transformed into the octyltin trichloride product.
• Any suitable type and amount of tin tetrachloride compound may be used from any suitable source.
• the tin tetrachloride may be used neat or pre-dissolved in a solvent, e.g., alkanes, such as hexanes, or aromatics, such as toluene.
• the solvent may be an inert organic solvent, such as hexane, isooctane, benzene, toluene, kerosene, cyclohexane, chlorobenzene etc.
• a suitable other solvent e.g., an ether, such as tetrahydrofuran, diethylether, or dibutylether, may also be used, although ethers are less preferred.
• a catalyst may or may not be included in the reaction. In a preferred embodiment, no catalysts, such as precious metal catalysts, are included in the reaction medium.
• the trioctyl aluminum compound is mixed with the desired donor in a manner known per se in a suitable apparatus under a protective gas.
• the octyl- aluminum complex compound so formed is then reacted, also under a protective gas, with the tin chloride or, if desired, with a mixture of the tin chloride and donor, e.g. din-butyl ether, in a molar ratio such that there is no more than one octyl group for each Sn atom.
• the SnCI 4 is first placed in the apparatus and the octyl-aluminum complex compound is run in while mixing well.
• the reaction is carried out at a temperature in the range of from 20 to 30 °C, especially 20 to 25 °C, more especially 22 to 25 °C.
• the halide ions present in the aqueous phase usually are chloride ions.
• suitable sources of chloride ions present in the aqueous phase are hydrochloric acid and/or soluble chloride salts of non-toxic metals, which do not interact with monooctyltin trichloride in an undesired way.
• chloride salts to be used include aluminum chloride and sodium chloride.
• An especially preferred source of chloride ions is hydrochloric acid.
• the amount of halide ions contained in the aqueous phase is such that the molar amount of halide present in the aqueous phase, is equal to or less than the molar amount of monooctyltin trichloride to be extracted, more preferably the amount of halide ions is in a range of from 100 to 300%, even more preferably 200 to 270% of the molar amount of monooctyltin trichloride to be extracted.
• the monooctyltin trichloride extracted into the aqueous phase may exist in the form of hydrated octyltin
• the halide ions are typically dissolved in demineralized water so as to form the aqueous phase containing halide ions.
• the organotin chloride mixture is contacted with the aqueous phase
• halide ions at a temperature of from 0°C to 100°C, more preferably at a temperature of from 20°C to 50°C, most preferably at a temperature of from 40 to 50°C.
• organic solvents which are immiscible with water
• organic solvents are aromatic, aliphatic and cyclo-aliphatic hydrocarbons, ethers and ketones, preferably, ethers or aliphatic and cyclo-aliphatic hydrocarbons with 5-9 carbon atoms, and mixtures of these, more preferably di-n- butyl ether, hexane, heptane, and octane, even more preferably hexane, heptane, and octane.
• One typical example of such an organic solvent is "Exxsol 100-120".
• the organotin chloride mixture is contacted with the aqueous phase containing halide ions, as a dispersion or solution in an organic solvent, the organotin chloride mixture is present in the organic solvent in a concentration of 10 to 90 % by weight, preferably 20 to 60 % by weight, based on the amount of organic solvent used.
• di-n-butyl ether has little solubility in water, aqueous phases containing halide ions, are capable of dissolving some amounts of di-n-butyl ether.
• monooctyltin chloride with an aqueous phase containing halide ions is effected by adding an aqueous phase containing halide ions to the organotin chloride mixture and mixing said organotin chloride mixture with said aqueous phase containing halide ions for 1 to 60 minutes, preferably, for 5 to 30 minutes, more preferably for 5 to 15 minutes.
• Said mixing step can be effected in any way known to a person skilled in the art, and typically comprises using
• an organotin chloride mixture comprising monooctyltin chloride with an aqueous phase containing halide ions according to the present invention as described above, typically the mixing is stopped whereby two phases (an organic phase and an aqueous phase) are formed. Thereafter, the aqueous phase can be separated.
• a separation can be effected in any way known to a person skilled in the art such as decanting or separation by using a separating funnel.
• monooctyltin trichloride containing aqueous phase can be effected, for example, in order to remove by-products from the aqueous phase.
• dioctyltin dichloride and/or trioctyltin chloride The most important by-product to be removed from the aqueous phase, is dioctyltin dichloride and/or trioctyltin chloride. It is noteworthy that although dioctyltin dichloride and trioctyltin chloride are practically insoluble in water, aqueous phases comprising halide ions, are capable of extracting some dioctyltin dichloride and/or trioctyltin chloride.
• Suitable organic solvents to be used according to the present invention for purifying the aqueous phase are organic solvents immiscible with water, but capable of dissolving undesired by-products, such as dioctyltin dichloride.
• suitable organic solvents to be used in said scrubbing step are aromatic, aliphatic and cyclo-aliphatic hydrocarbons, ethers and ketones, preferably ethers or aliphatic and cyclo-aliphatic hydrocarbons having 5 to 9 carbon atoms, and mixtures of these, more preferably hexane, heptane, and/or octane.
• a suitable extracting solvent is "Exxsol 100-120" sold by Exxon.
• the organic solvent to be used for said purification is also capable of dissolving monooctyltin chloride (such as for example di-n-butyl ether)
• the organic solvent should be used in a way that undesired re-extraction of monooctyltin trichloride from the aqueous phase is avoided or at least limited.
• Suitable ways to limit or even to avoid extraction of monooctyltin trichloride from the aqueous phase are for example to use only small amounts of solvent, i.e., to use a low weight ratio of organic solvent to aqueous phase, and/or to carry out said purification step at low temperatures of from 20 to 50 °C.
• the purification step according to the present invention is carried out at a temperature of from 20 to 50°C in such a way that the weight ratio of organic solvent/aqueous phase 10 to 20/100 based on the weight of both phases.
• said purification step is repeated one or more times, more preferably two to three times.
• monooctyltin trichloride is recovered from the aqueous phase comprising monooctyltin trichloride. Such a recovery can be done in any way known to a person skilled in the art.
• step (1 ) outlined above the source of halide ions in step (1 ) outlined above is hydrochloric acid
• water and hydrochloric acid can be simply distilled off, in order to obtain monooctyltin trichloride. It is also possible to recover monooctyltin trichloride from the aqueous phase with a suitable amount of organic solvent, and subsequently to distill off the organic solvent in order to obtain the pure monooctyltin trichloride product.
• Non-limiting examples of suitable solvents to be used for the recovery according to the present invention are aromatic, aliphatic and cyclo-aliphatic hydrocarbons, ethers and ketones.
• Preferred solvents according to the present invention are ethers, more preferably din-butyl ether.
• recovery of the monooctyltin trichloride product can be done at a temperature in a range of from 0 to 100°C, preferably at a temperature in a range of from 40 to 70°C.
• monooctyltin trichloride dissolved in the aqueous phase can be recovered by chemically converting monooctyltin trichloride into another stable monooctyltin compound.
• the aqueous phase can be neutralized with a suitable base, such as sodium hydroxide, ammonium hydroxide, or ammonia, so that monooctyltin oxide and/or hydroxyoctyloxostannane will be formed.
• a suitable base such as sodium hydroxide, ammonium hydroxide, or ammonia
• monooctyltin oxide and/or hydroxyoctyloxostannane is a solid material, it can be easilv separated from the aqueous phase by filtration.
• Monooctyltin oxide and hydroxyoctyloxostannane are well known esterification catalysts, and raw materials for producing PVC heat stabilizers.
• the aqueous phase can be neutralized with a suitable base in the presence of stoichiometric amounts of mercaptides, such as isooctyl
• other tin compounds refers to organotin compounds containing alkyl groups other than n-octyl, which are common by-products in technical octyltin mixtures, as well as inorganic tin tetrachloride. All tin species composition analytics were performed by GC (gas chromatography).
• This Example demonstrates the extraction of mono-n-octyltin trichloride from a mixture of organotin chlorides into an aqueous phase comprising hydrochloric acid, the fact that some di-n-butyl ether is soluble in an aqueous phase comprising mono- n-octyltin trichloride, the scrubbing of the aqueous phase with small amounts of di-n- butyl ether, and the re-extraction of mono-n-octyltin trichloride from aqueous phase by larger amounts of di-n-butyl ether.
• a technical raw organotin chloride mixture had a tin species composition of 64.2 % mono-n-octyltin trichloride, 33.8 % di-n-octyltin dichloride, 0.2 % tri-n-octyltin chloride, and 1.8 % other tin compounds.
• Step 1 Aqueous extraction:
• the upper (organic) phase had a weight of 33.3 g; it had a tin species composition of 25.6 % mono-n-octyltin trichloride, 71.7 % di-n-octyltin dichloride, 0.5 % tri-n-octyltin chloride, and 2.2 % other tin compounds.
• the lower (aqueous) phase was further treated as described below.
• Step 2 Scrubbing of the aqueous phase to remove dioctyl and trioctyltin chlorides:
• Second scrubbing To the resulting aqueous phase obtained from the first scrubbing, another 5 g of di-n-butyl ether were added, and the mixture was stirred at room temperature. After the stirring was terminated, 2 phases appeared; they were allowed to settle, and subsequently separated.
• the upper (organic) phase had a weight of 7.7 g; it comprised a tin species composition of 84.7 % mono-n-octyltin trichloride, 13.6 % di-n-octyltin dichloride, 0.0 % tri-n-octyltin chloride, and 1.7 % other tin compounds.
• the lower (aqueous) phase was further treated as described below.
• Step 3 Recovery of monooctyltin trichloride from the aqueous phase:
• Second re-extraction To 57.6 g of the aqueous phase resulting from the first re- extraction, 19.0 g of di-n-butyl ether were added, and the mixture was stirred at room temperature. After the stirring was terminated, 2 phases appeared; they were allowed to settle, and subsequently separated.
• the upper (organic) phase had a weight of 29.9 g; it had a tin species composition of 98.2 % mono-n-octyltin trichloride, 0.2 % di-n-octyltin dichloride, 0.0 % tri-n-octyltin chloride, and 1.6 % other tin compounds.
• This Example demonstrates the extraction of mono-n-octyltin trichloride from a mixture of organotin chlorides and n-heptane as organic solvent added to an aqueous phase comprising hydrochloric acid, the scrubbing of the aqueous phase with small amounts of n-heptane, and the recovery of mono-n-octyltin trichloride from aqueous phase by di-n-butyl ether.
• a technical raw organotin chlorides mixture had a tin species composition of 61.8 % mono-n-octyltin trichloride, 32.9 % di-n-octyltin dichloride, 0.2 % tri-n-octyltin chloride, and 3.5 % other tin compounds.
• Step 1 Aqueous extraction:
• the upper (organic) phase had a weight of 92.0 g; it had a tin species composition of 22.4 % mono-n-octyltin trichloride, 69.9 % di-n-octyltin dichloride, 0.5 % tri-n-octyltin chloride, and 7.2 % other tin compounds.
• the lower (aqueous) phase was treated further as described below.
• Step 2 Scrubbing of the aqueous phase to remove dioctyl and trioctyltin chlorides:
• Second scrubbing To the resulting aqueous phase from the first scrubbing, another 14 g of n-heptane were added, and the mixture was stirred at room temperature. After the stirring was terminated, 2 phases appeared; they were allowed to settle, and subsequently separated.
• the upper (organic) phase had a weight of 13.311 g; it had a tin species composition of 86.2 % mono-n-octyltin trichloride, 10.8 % di-n- octyltin dichloride, 0.0 % tri-n-octyltin chloride, and 3.0 % other tin compounds.
• the lower (aqueous) phase was treated further as described below.
• Step 3 Recovery of monooctyltin trichloride from the aqueous phase:
• Second re-extraction To 117.8 g of the aqueous phase resulting from the first re- extraction, 23.6 g of di-n-butyl ether were added, and the mixture was stirred at room temperature. After the stirring was terminated, 2 phases appeared; they were allowed to settle, and subsequently separated.
• the upper (organic) phase had a weight of 58.4 g; it had a tin species composition of 99.0 % mono-n-octyltin trichloride, 0.07 % di-n-octyltin dichloride, 0.0 % tri-n-octyltin chloride, and 1.9 % other tin compounds.
• the upper (organic) phase had a weight of 17.2 g; it had a tin species composition of 94.1 % mono-n-octyltin trichloride, 0.3 % di-n-octyltin dichloride, 0.0 % tri-n-octyltin chloride, and 5.6 % other tin compounds.
• the lower (aqueous) phase was analyzed by ICP for residual metal; it had a content of 0.7 % tin.
• This Example demonstrates the extraction of mono-n-octyltin trichloride from a mixture of organotin chlorides into an aqueous phase comprising hydrochloric acid, the scrubbing of the aqueous phase with small amounts of n-heptane, and the recovery of monooctyltin trichloride from the aqueous phase by distillation of the aqueous HCI.
• a technical raw organotin chlorides mixture had a tin species composition of 60.7 % mono-n-octyltin trichloride, 36.9 % di-n-octyltin dichloride, 0.3 % tri-n-octyltin chloride, and 2.1 % other tin compounds; by elementary analysis it contained 36.9 % tin.
• Step 1 Aqueous extraction.
• Step 2 Scrubbing of the aqueous phase to remove dioctyl and trioctyltin chlorides.
• Second scrubbing To the resulting aqueous phase from the first scrubbing, another 12.5 g of n-heptane were added, and the mixture was stirred at 50°C. After the stirring was terminated, 2 phases appeared; they were allowed to settle, and subsequently separated.
• the upper (organic) phase had a weight of 14.5 g; it had a tin species composition of 51.8 % mono-n-octyltin trichloride, 46.1 % di-n-octyltin dichloride, 0.3 % tri-n-octyltin chloride, and 1.9 % other tin compounds; by
• the resulting lower (aqueous) phase had a weight of 123.5 g; it had a tin species composition of 98.5 % mono-n-octyltin trichloride, 0.06 % di-n-octyltin dichloride, 0.0 % tri-n-octyltin chloride, and 1.4 % other tin compounds; by elementary analysis it contained 14.1 % tin. It was treated further as described below.
• Step 3 Recovery of monooctyltin trichloride by distillation of the aqueous HCI:
• the resulting product had a weight of 35.5 g; it had a tin species composition of 98.6 % mono-n-octyltin trichloride, 0.04 % di-n-octyltin dichloride, 0.0 % tri-n-octyltin chloride, and 1.4 % other tin compounds; by elementary analysis it contained 35.1 % tin, and 31.3 % CI.
• This Example demonstrates how the solubility of mono-n-octyltin trichloride in aqueous aluminum chloride phase and its extraction from organic phase depends on the chloride concentration.
• a mixture was prepared, consisting by weight of 55.7 % mono-n-octyltin trichloride, 10.7 % di-n-butyl ether, 26.2 % n-heptane, 7.3 % AICI 3 . 10 g of this mixture were transferred into a graduated glass cylinder.
• a mixture was prepared, consisting by weight of 55.7 % mono-n-octyltin trichloride, 10.7 % di-n-butyl ether, 26.2 % n-heptane, 7.3 % AICI 3 .
• the temperature in the glass cylinder was adjusted to 20°C, and the phases were allowed to settle and separate for 30 minutes.
• the resulting volume of the organic phase was 8 mL.
• the temperature in the glass cylinder was adjusted to 40°C, and the phases were allowed to settle and separate for 30 minutes.
• the resulting volume of the organic phase was 10 mL.
• the temperature in the glass cylinder was adjusted to 60°C, and the phases were allowed to settle and separate for 30 minutes.
• the resulting volume of the organic phase was 14 mL.

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