Classifications

• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
  • C01C3/00—Cyanogen; Compounds thereof
  • C01C3/003—Cyanogen

Definitions

• the invention relates to a production method of ethane dinitrile (CN) 2 from hydrogen cyanide HCN by oxidation thereof on a Fe ra+ /Cu ll+ catalytic system supported on a polymeric organic cation exchanger, in which m + has the value of 2 or 3, n + has the value of 1 or 2.
• Ethane dinitrile (CN) 2 (Herbert E. Williams, H. E.: The Chemistry of Cyanogen Compounds and Their Manufacture and Estimation, General Books, 2009.), termed also dicyan, (di)cyanogene, oxalyl (di)nitrile or oxalyl cyanide, is a chemical compound with a very small difference between the boiling point (-21 °C) and melting point (-28 °C), showing the second highest known combustion temperature (4640 °C) (Thomas, N., Gaydon, A. G., Brewer, L., A.
• the yield of the raw ethane dinitrile is stated as 97.6 %; the product contains 98.1 % of ethane dinitrile, 0.2 % of oxygen, and 1.7 % of nitrogen.
• the salts were used in the reaction mixture in the concentrations from 10 % by weight to 20 % by weight with the equimolar ratio of Cu 2+ and Fe 3+ ; the concentration of sulfolane in the reaction mixture is shown according to this patent as 0 to 80 % by volume.
• the sulfolane acts as a stabilizer for the salts of iron and copper and the bromide form of both salts suppresses undesirable side reactions, such as the formation of a mixture of oxides of both metals, elimination of elementary metals, and formation of halocyanogen.
• the metal bromides in comparison with chlorides, sulfates and nitrates, these provided the highest 5 conversion of hydrogen cyanide and the yield of ethane dinitrile.
• the disadvantage of said solution is the use of relatively expensive metal bromides, their corrosiveness in the technological equipment, toxicity including environmental toxicity, and further the fact that the long-term stability of the system is relatively low.
• a 10 significant disadvantage of said solution is the fact that the addition of 35 % of hydrogen peroxide increases the volume of the aqueous reaction mixture hence it reduces the concentration of both salts and of sulfolane, which leads to reduction of the efficiency of the process and to reduction of stability of the system. It is then necessary to discontinue the process to remove water by distillation, which further increases the operating costs.
• the invention provides a method of production of ethane dinitrile (CN) 2 by oxidation of hydrogen cyanide HCN, wherein hydrogen cyanide is oxidized on a catalytic system
• n has the value of 1 or 2, optionally in the presence of bidentate oxygen or nitrogen ligand, wherein the catalytic system is supported on a polymeric organic cation exchanger, wherein the oxidation reaction is carried out in an organic solvent, which is preferably methanol, or in a homogeneous or heterogeneous mixture of an organic solvent with water, at the temperature of 5 °C to
• an oxygen-containing oxidizing agent selected from the group containing oxygen, air, hydrogen peroxide or its mono- or di-substituted alkyl or acyl derivates selected from the group including r/-butyl hydroperoxide, benzoyl hydroperoxide, dibenzoyl peroxide, di-tert-butyl peroxide, di-(2-ethylhexyl) peroxydicarbonate.
• the oxygen-containing oxidizing agent is hydrogen peroxide.
• the oxidizing agent is hydrogen peroxide in the concentration in the range of 3 to 40 % by weight.
• hydrogen peroxide and liquid hydrogen cyanide are dosed in the molar ratio in the range of 1 : 3 to 3 : 1, the dosage rate is controlled by the conversion of hydrogen cyanide to ethane dinitrile and further by the concentration of carbon dioxide, an undesired by-product, in the mixture with the product and the unreacted hydrogen cyanide.
• the products which are the desired ethane dinitrile, undesired carbon dioxide, which is formed by its oxidative hydrolysis, and the unreacted hydrogen cyanide are then removed from the reaction zone to further processing, that is to the separation of the components of the gaseous mixture by fractional distillation, to the adjustment of the ethane dinitrile, and to the recycling of hydrogen cyanide.
• hydrogen cyanide is used in liquid form.
• the molar ratio of the ions Fe m+ : Cu n+ supported on the cation exchanger is in the range of 1 : 4 to 4 : 1.
• the polymeric organic cation exchanger used for the support of the catalytic system Fe m+ /Cu n+ is preferably an organic synthetic polymer, co-polymer, or an organic polycondensate bearing strongly acidic, that is -SO 3 H, -O-SO 3 H, or medium acidic, that is -P(0)(OH) 2 , -P(0)H(OH), -0-P(0)(OH) 2 , or weakly acidic, that is -COOH, -alkyl- COOH, -aryl-COOH, -aryl-OH, functional groups.
• the polymeric organic cation exchanger used for the support of the catalytic system Fe m+ /Cu + is a polyacrylate or polymethacrylate weakly acidic cation exchanger, or a strongly acidic cation exchanger on the basis of sulfonated copolymer of styrene and divinylbenzene, which are synthetic resins commonly used for example for industrial purification of water.
• These polymeric organic cation exchangers can be used in a gel or macroporous form.
• the catalytic system is prepared by chemisorption of both iron and copper cations in the form of a salt or complex to the polymeric organic cation exchanger.
• the chemisorption can be performed for example by washing an aqueous solution of a metal salt or metal complex through a column filled with the cation exchanger or by mixing an aqueous solution of a metal salt or metal complex with the cation exchanger until the desired saturation of the cation exchanger is achieved.
• the salt or complex used for the chemisorption may be any soluble salt or complex of copper or iron. Preferably, it is selected from chloride, bromide, sulfate, nitrate and acetate.
• the organic solvent is preferably an aliphatic alcohol containing 1 to 3 carbon atoms, preferably methanol, or optionally its mixture with water.
• the bidentate nitrogen ligand is preferably selected from the group containing 2,2'- bipyridine, 1 , 10-phenanthroline, N,N,N ' ,N ' -tetramethyl-l,2-ethylenediamine, 1 ,2- ethylenediamine, 1,3-propylenediamine, N,N, N ' ,N ' -tetramethyl-l ,3-propylenediamine.
• the content of the bidentate ligand in the supported catalyst is preferably 0 to 10 % by weight.
• An advantage of the invention is the substitution of a homogenous catalyst with a supported heterogeneous catalytic system.
• Water with the addition of sulfolane used in the state-of-the-art process as the solvent was replaced in one preferred embodiment of the invention with methanol.
• the reaction using the supported heterogeneous catalyst is slower and it does not need cooling; the optimum temperature mode is about 50 °C.
• Methanol is separated from the reaction environment after the reactor shutdown by distillation; the advantage is that it does not form an azeotrope with water, and further the fact that its boiling temperature is approximately two thirds of the boiling temperature of water, which is energetically advantageous.
• the catalyst is significantly more stable in methanol or in its mixture with water than in water alone. Stability of the catalyst can be further supported by addition of free cation exchanger, used for the support of the catalytic system Fe m+ /Cu n+ .
• the bidentate ligand present helps to stabilize Fe and Cu against the reduction to elementary metals during the process, which deteriorates the catalytic system, and it suppresses the possible hydrolytic oxidation of ethane dinitrile to carbon dioxide, which decreases the selectivity of the process.
• the process according to the present invention does not have to use the expensive and toxic copper and iron bromides. More available and cheaper salts of copper and iron than bromides can be used for preparation of the catalyst.
• Cation exchanger is an industrial resin used for treatment of water, it is easily available and cheap, and it forms a highly stable complex with the copper and iron cations. Further advantages of the solution according to the present invention are easier modification of the reaction mixture during the process, especially elimination of waste solvent from the heterogeneous system of catalyst, absence of metal ions from the catalyst in the waste solvent, and lower energy demands on processing of the liquid mixture; see the above- mentioned advantages of methanol versus water.
• the reaction medium has minimum corrosive effects on the technological equipment, in particular because water is not contaminated with copper and iron ions.
• the system according to the invention shows a 5 higher efficiency than the known systems used in the industry, which leads to lower consumption of the hydrogen peroxide used.
• the catalyst was prepared in the following manner: 75 g of weakly acidic polyacrylate 20 cation exchanger of macroporous type in ionized Na + form, with the minimum total capacity of 4.5 mol / liter and powder density of 750 g / liter, was mixed in 300 ml of water, 42.5 g (250 mmol) of copper(II) chloride dihydrate and 32.4 g (120 mmol) of iron(III) chloride hexahydrate were added and the mixture was stirred for 30 min. After that, 2.5 g (25 mmol) of acetyl-acetone was added to the solution, and the mixture was 25 stirred for further 1 h. Then the aqueous phase was removed and the solid phase was washed twice by 100 ml of water, then subsequently twice by 150 ml of methanol, and the catalyst was used into the following reaction.
• the entire process was running at the temperature of 50 °C for the period of 3 hours, the gaseous products, that is the ethane dinitrile, carbon dioxide and the unreacted 5 hydrogen cyanide were led off through the condenser to the apparatus for cryoscopic fractional distillation; ethane dinitrile was purified and adjusted, hydrogen cyanide was recycled backward into the process.
• the composition of gases at the output from the equipment in their total volume conveyed out from the reaction vessel for the period of three hours (as monitored by the gas chromatography using the area ratio of the peaks) 10 was: 0.7 rel % of carbon dioxide, 48.2 rel % ethane dinitrile, 37.4 rel % of unreacted hydrogen cyanide and methanol to 100 rel %.
• the catalyst was prepared in the following manner: 78 g of strongly acidic sulfonated poly(styrene-divinylbenzene) cation exchanger of macroporous type in ionized Na + form, with the minimum total capacity of 1.8 mol / liter and with the powder density 780 g / liter, was mixed in 300 ml of water, 34.0 g (200 mmol) of copper(II) chloride dihydrate and 48.6 g (180 mmol) of iron(III) chloride hexahydrate were added and the
• composition of gases at the output from the equipment in their total volume conveyed out from the reaction vessel for the period of five hours was: 2.2 rel % of carbon dioxide, 36.9 rel % ethane dinitrile, 50.1 rel % of unreacted hydrogen cyanide and methanol to 100 rel %.
• the catalyst was prepared in the following manner: 84 g of strongly acidic sulfonated poly(styrene-divinylbenzene) cation exchanger of a gel type in ionized Na + form, with the minimum total capacity of 2.2 mol / liter and with the powder density of 840 g / liter, was stirred with 300 ml of water, 17.0 g (100 mmol) of copper(II) chloride dihydrate and 67.5 g (250 mmol) of iron(III) chloride hexahydrate were added and the mixture was stirred for 30 min. Then the aqueous phase was poured off and the solid phase was washed twice by 100 ml of water, then subsequently twice by 150 ml of methanol, and the catalyst was used into the following reaction.
• the entire process was running at the temperature of 55 °C for the period of 24 hours, its constant volume was maintained using methanol, the gaseous products, that is the ethane dinitrile, carbon dioxide and unreacted hydrogen cyanide, and the methanol vapors were conveyed through the condenser to the apparatus for cryoscopic fractional distillation; ethane dinitrile was purified and adjusted, hydrogen cyanide was recycled backward into the process.
• composition of gases at the output from the equipment in their total volume conveyed out from the reaction vessel for the period of 24 hours was: 2.9 rel % of carbon dioxide, 40.2 rel % ethane dinitrile, 40.8 rel % of non-reacted hydrogen cyanide and methanol to 100 rel %.
• the catalyst was prepared in the following manner: 84 g of strongly acidic sulfonated poly(styrene-divinylbenzene) cation exchanger of a gel type in ionized Na + form, with the minimum total capacity of 2.2 mol / liter and with the powder density of 840 g / liter, was stirred in 300 ml of water, 17.0 g (100 mmol) of copper(II) chloride dihydrate and 27.8 g (100 mmol) of iron(II) sulfate heptahydrate were added, and the mixture was stirred for 30 min.
• composition of gases at the output from the equipment in their total volume conveyed out from the reaction vessel for the period of four hours was: 1.1 rel % of carbon dioxide, 59.8 rel % ethane dinitrile, 29.2 rel % of unreacted hydrogen cyanide and methanol to 100 rel %.
• the catalyst was prepared in the following manner: 84 g of strongly acidic sulfonated poly(styrene-divinylbenzene) cation exchanger of a gel type in ionized Na + form, with the minimum total capacity of 2.2 mol / liter and with powder density of 840 g / liter, was mixed in 300 ml of water, 25.5 g (150 mmol) of copper(II) chloride dihydrate and 21.6 g (80 mmol) of iron(III) chloride hexahydrate were added, and the mixture was stirred for 30 min, then dipivaloylmethane (1.84 g, 10 mmol) was added to the mixture, and the mixture was stirred for another 60 min. Then the aqueous phase was poured off and the solid phase was washed twice by 100 ml of water, then subsequently twice by 150 ml of methanol, and the catalyst was used into the following reaction.
• the entire process was running at the temperature of 50 °C for the period of 5 hours, the gaseous products, that is ethane dinitrile, carbon dioxide and unreacted hydrogen cyanide, and methanol vapors were conveyed through the condenser to the apparatus for cryoscopic fractional distillation; ethane dinitrile was purified and adjusted, hydrogen cyanide was recycled backward into the process.
• composition of gases at the output from the equipment in their total volume conveyed out from the reaction vessel for the period of five hours was: 0.7 rel % of carbon dioxide, 75.8 rel % ethane dinitrile, 10.8 rel % of unreacted hydrogen cyanide and methanol to 100 rel %.

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• 2011
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