METHOD OF MANUFACTURING HYDROGEN PEROXIDE

Abstract: A process for producing hydrogen peroxide wherein a gaseous mixture comprising hydrogen and oxygen is con­ tacted with a catalyst in the presence of water and an organic solvent wherein: i) the organic solvent is immiscible with water and unreactive with hydrogen peroxide under the contacting con­ ditions; ii) the distribution coefficient for hydrogen peroxide between the water and the organic solvent is greater than 1; iii) the catalyst is of the formula L₂MX₂ wherein L is a ligand represented by the formula A R₁ R₂ R₃ wherein R₁ R₂ and R₃ are alkyl, cycloalkyl or aryl groups, hydrogen or halogen, A is a Group 5b element selected from the group consisting of nitrogen, phosphorous and arsenic, M is a Group 8 metal and X is halogen, said catalyst being soluble in said organic solvent and insoluble in water; and iv) the gaseous mixture is non-ignitable under the pro­ cess conditions characterized in that the organic solvent is selected from the group consisting of fluorocarbons, halofluorocarbons and mixtures thereof.

Description: This invention relates to a method of manufacturing hydrogen peroxide from its constituent elements, hydrogen and oxygen. In our US Patent Specification No. 4,128,627 we have described a process for producing hydrogen peroxide wherein a gaseous mixture comprising hydrogen and oxygen is contacted with a catalyst in the presence of water and an organic solvent wherein: i) the organic solvent is immiscible with water and unreactive with hydrogen peroxide under the contacting conditions; ii) the distribution coefficient for hydrogen peroxide between the water and the organic solvent is greater than 1; ; iii) the catalyst is of the formula L2MX2 wherein L is a ligand represented by the formula A R1 R2 R3 wherein R1 R2 and R3 are alkyl, cycloalkyl or aryl groups, hydrogen or halogen, A is a Group 5b element selected from the group consisting of nitrogen, phos phorous and arsenic, M is a Group 8 metal and X is halogen, said catalyst being soluble in said organic solvent and insoluble in water; and iv) the gaseous mixture is non-ignitable under the process conditions. In the description of this patent specification we suggested that suitable organic solvents could comprise 1,2-dichlorobenzene, chlorobenzene and xylene. We have now discovered that substantial and unexpected advantages are obtained when the organic solvent is selected from the group consisting of fluorocarbons, halofluorocarbons and mixtures thereof. In particular, in at least preferred embodiments we have observed (compared with our previous work): 1) high catalyst activity at low concentrations of catalyst in the organic solvent; 2) a high rate of production of hydrogen peroxide in the aqueous phase per unit partial pressure of oxygen and per unit concentration of catalyst; and 3) the production of high concentrations of hydrogen peroxide in the aqueous phase. The fluorocarbon and/or halofluorocarbon is preferably aliphatic and should preferably be fully substituted by halogens with at least 25% of the halogen atoms, and possibly all of the halogen atoms, being fluorine. Examples of suitable perfluorocarbons include perfluoroaliphatic ethers, perfluoroalkyl tertiary amines, perfluoropentane, perfluoro-l, 3-dimethylcyclohexane and mixtures thereof. Examples df suitable halofluorocarbons include 1,1,2-trichlorotrifluoroethane, 1,2-dichlorotetrafluoroethane, 1,2-dibromotetrafluoroethane and mixtures thereof. The phase volume ratio of water to halofluorocarbon or perfluorocarbon is preferably in the range 10:1 to 1:10, the range 2:1 to 1:3 being more preferred. As indicated in US Patent Specification No. 4,128,627: 1) The ligand L is preferably selected from the group consisting of tri (pentafluorophenyl) phosphine, tricyclohexylphosphine and triphenylarsine. 2) The Group 8 metal is preferably palladium. 3) The halogen is preferably chlorine. 4) The catalyst is preferably selected from the group consisting of bis(tri(pentafluorophenyl)phos phine) palladium dichloride, bis(tricyclohexylphos phine) palladium dichloride and bis(triphenylarsine) palladium dichloride. 5) The gaseous mixture can comprise oxygen, hydrogen and a gas which is inert under the reaction conditions, for example nitrogen and/or methane. 6) The gaseous mixture may consist of oxygen and hydrogen wherein the ratio of oxygen to hydrogen does not exceed 4 parts oxygen per 100 parts hydrogen (by volume). Overall we recommend the use of the complex Pd C12 (P(C6F5)3)2 as catalyst in combination with a halofluorocarbon as organic solvent. In this embodiment we have found that the rate of hydrogen peroxide production is relatively independent of catalyst concentration in the organic phase down to 5x10 5M. Industrially useful rates of production may be achieved using catalyst concentrations between 5x10 5M and 2.5x10 4M, a factor of up to 100 less than is necessary when using previously recommended solvents, leading to a considerable reduction in capital cost. The catalyst activity factor expressed in weight % H202/hour/psi O2/10 1M catalyst is increased to 10-40 compared with 0.2 1 using the previously recommended solvents. In addition there is a reduced tendency for the rate of hydrogen peroxide production to decrease with increasing hydrogen peroxide concentration in the aqueous phase thereby enabling higher hydrogen peroxide concentrations, for example 4.7 wt. % to be achieved whilst regularly sampling and making up the aqueous phase with deionised water. When a halofluorocarbon is used as organic solvent the addition of 1-50,000 ppm by volume of perfluorocarbon, for example perfluoro-1,3-dimethylcyclohexane or polymeric halofluorocarbon of molecular weight greater than 300 g, for example polychlorotrifluoroethylene (Kel F oil), or up to 50 ppm (by weight) of a C10 -C30 straight chain hydrocarbon, hydrocarbon salt, carboxylic acid, ester of a carboxylic acid or salt of a carboxylic acid or a fluorinated equivalent thereof, for example n-eicosane, stearic acid and potassium perfluorooctane sulphonate, facilitates maintaining high rates of hydrogen peroxide synthesis which are linear over extended periods. The additives must, of course, be resist ant to reaction with hydrogen peroxide under the conditions of the process and may be used in combination if desired. The aqueous and organic phases should be brought into intimate contact over a large contact area to facilitate extraction of the hydrogen peroxide into the aqueous phase as it is formed. Such contract can conveniently be achieved by a mechanical stirrer or, preferably, by sparging a gaseous mixture containing hydrogen and oxygen through the liquid. The process is advantageously operated at superatmospheric pressure, for example 0-5000 psig and preferably at temperatures between the freezing point of the aqueous phase and 15 C, and generally between 0 and 10 0C. Without wishing to be bound by theory, it appears that in the present invention, hydrogen peroxide is synthesized at a surface active film at the interface between the organic and aqueous phases. The surface active film is formed in 'situ from the catalytic complex solution in the organic phase when mixed with water and contacted with the gas mixture containing hydrogen and oxygen. This leads to better utiliz ation of low concentrations of the catalytic complex and high catalytic activity. EXAMPLES The following examples illustrate embodiments of the present invention and embodiments of the invent ion disclosed in our US Patent Specification No. 4,128,627. The experimental procedure was as follows. A cylindrical reactor was constructed of pyrex glass and equipped with a perforated Teflon (R.T.M) disc gas distributor, pyrex reflux condenser, pyrex enclosed thermocouple and pyrex inlet and outlet lines. Into this reactor was loaded 180 ml. of a solution of known concentration of the catalytic complex Pd C12 (P (C6F5)3 )2 in the test organic solvent together with 90 ml. deiqnised water, and the temperat ure of the reactor contents was maintained between 1 and 100C by external refrigeration. The following solvents were obtained from BDH Chemicals Ltd., Poole, England: 1,1,2-trichlorotri- fluoroethane, and Analar grade 1,2-dichlorobenzene, benzene and xylene. For the tests of the effects of additions (Examples 22-26), the 1,1,2-trichlorotrifluoroethane was distilled before use. The perfluoro-l , 3-dimethylcyclohexane was obtained from Fluorochem Ltd., Glossop, England. A non-f lammable gas mixture containing, in Examples 8, 9, 10 and 21: 3.5% 02, 48.3% H2, 48.2% N2 and in the remaining Examples: 2.5 to 3.5% 2 in H2, was sparged through the reactor at a specified flow rate using a recirculating gas pump. Both inlet pressure and inlet oxygen concentration in the gas mixture were maintained automatically. The hydrogen peroxide concentration in the aqueous phase was measured periodically during the course of each run by temporarily stopping the gas flow for 30 seconds, which allowed the liquid phases to separate, withdrawing a measured volume of the aqueous phase and pumping back into the reactor via a stainless steel diaphragm pump an equal volume of deionised water. The aqueous phase sample was then analysed for hydrogen peroxide by titration with ceric sulphate solution. The aqueous phase samples obtained in this manner were free of catalyst and entrained organic phases. Selectivity was determined either by liquid mass balance in the reactor or by the decline of oxygen concentration in the recirculated gas mixture with the oxygen supply turned off. Referring to the drawings: Examples 1-5 (Fig 1) illustrate embodiments of the present invention at 1800 psig total pressure using 1,1,2-trichlorotrifluoroethane. As the concentration of Pd (C12 (P (C6F5)3)2 is decreased from 6.8x10 to 9.1x10 5M, the maximum rate of hydrogen peroxide production and the specific rate/psi O2 vary by factors of only 1.8 and 2.4. High catalyst activity factors of 16.4 and 8.9 (units in wt. %/h/psi O2/10 1M catalyst) are achieved in examples 1 and 2. The linearity of example 2 together with its high maximum rate of 1.36 wt %/h enabled 4.7 wtF hydrogen peroxide to be produced in 5 hours, even when the aqueous phase was sampled and diluted during the course of the run. Examples 6-10 (Fig 2) 'illustrate embodiments of the present invention using 1,1,2-trichlorotrifluoroethane at 900 and 600 psig, and catalyst concentrations over the range 4.56x10 4M to 7.4x105M. Again the results show high catalyst utilisation factors in the range of 5 to 30, and aqueous phase hydrogen peroxide concentrations up to 2 wt% obtainable in 5 hours with sampling and dilution. It will also be apparent from examples 1-10 that the specific maximum rate expressed in wt%/h/psi O2 obtained is nearly constant, varying only by a factor of 2.7 over the range of operating pressures and catalyst concentrations illustrated. Selectivities were in the range 70-80 mole %. Examples 11-14 (Fig 3)and 15-17 (Fig 4) illustrate the results obtained under identical conditions using the method of US Patent Specification No. 4,128,627 at 1100 and 1800 psig respectively, with l,2-dichlorobenzene as the organic solvent. They show that higher catalyst concentrations are needed to obtain results comparable with the other examples, i.e. at least 3-5x10 M to obtain similar rates and specific rates. This is also illustrated by the lower catalyst activity factors. Only at catalyst concentrations of the order of 6x10 3M do the catalyst activity factors of the present invention fall to the same range. In addition, the rate of hydrogen peroxide production using 1,2-dichlorobenzene as solvent falls more rapidly with increasing hydrogen peroxide concentration greater than 1.5wt%, so that the maximum obtained in these Examples was only 1.8 wt%. Examples 18-19 (Fig 4) show that the results obtained with two other solvents of the type specified in US Patent Specification No. 4,128,627, benzene and xylene, are no better. The following table compares examples with similar catalyst concentrations and pressures using 1,1,2-trichlorotrifluoroethane and 1,2-dichlorobenzene, and lists the improvement factors obtained by the method of the present invention. Improvement Factors Ratio d Compared Catalyst Ratio Cf Ratio Cf Example Concentration Ratio of Specific Catalyst Numbers Range 10 no Max. Rate -Rate Activity ration 7 11 4.6 - 6.3 3.7 3.1 4.1 1.9 4 18 18 - 19 4.1 4.0 4.0 1.9 5 16 56 68 1.2 1.4 0.8 1.5 Examples 20-21 (Fig 5) illustrate embodiments of the present invention with respect to a fluoro carbon, perfluoro-1,3-dimethylcyclohexane, in which the solubility of Pd C12 (P (C6F5)3)2 is limited to about 5x10-5M. Although the results are not as good in terms of hydrogen peroxide concentration achieved as with 1,1,2-trichlorotrifluoroethane, the specific maximum rate in wt%/h/psi O2 and catalyst activity are of similar values. Using 1,1,2-trichlorotrifluoroethane as the halofluorocarbon solvent, Examples 22-26 (Fig 6) illustrate embodiments of the present invention with respect to the effect certain types of additives have on the linearity of the rate of production of hydrogen peroxide over extended periods. In these examples, sparging was stopped after 6 hours and the reactor contents left quiescent under full gas pressure over night before restarting sparging 16 hours later. The examples are however plotted as continuous curves that represent the variation in rate of hydrogen peroxide production (adjusted for the dilution following sampling) over the actual time in which gas was sparged through the reactor. The concentration of hydrogen peroxide in the aqueous phase fell during the quiescent period but in the case of the more linear examples 23-27 was reproduced during the subsequent 6 hour sparging period. It can be seen that excellent results in terms of specific rate/psi 02, linearity and reproducibil ity, and catalyst activity are obtained using a halo fluorocarbon organic phase and a polymeric halofluoro carbon, or more preferably, a perfluoracarbon, additive. Whilst a survey of the examples is included in this description, details of each'of the examples are included alongside the relevant graphs to assist the reader. In this connection it is noted that the vertical axis are not drawn to the same scale in each graph. SUMMARY: EXAMPLES 1 to 14 EMI9.1 No. <SEP> 1 <SEP> 2 <SEP> 3 <SEP> 4 <SEP> 5 <SEP> 6 <SEP> 7 <SEP> 8 <SEP> 9 <SEP> 10 <SEP> 11 <SEP> 12 <SEP> 13 <SEP> 14 <tb> Catalyst <SEP> concent. <tb> 0.91 <SEP> 2.42 <SEP> 6.23 <SEP> 18.0 <SEP> 68.2 <SEP> 1.28 <SEP> 4.56 <SEP> 0.74 <SEP> 1.36 <SEP> 1.50 <SEP> 6.33 <SEP> 13.2 <SEP> 20.7 <SEP> 47.6 <tb> 10-4M <tb> Pressure <SEP> pstg <SEP> 1780 <SEP> 1800 <SEP> 1800 <SEP> 1780 <SEP> 1780 <SEP> 890 <SEP> 990 <SEP> 600 <SEP> 600 <SEP> 600 <SEP> 1110 <SEP> 1140 <SEP> 1080 <SEP> 1180 <tb> @O2 <SEP> in <SEP> gas <SEP> 3.4 <SEP> 3.5 <SEP> 2.6 <SEP> 2.6 <SEP> 2.6 <SEP> 3.3 <SEP> 3.5 <SEP> 3.5 <SEP> 3.5 <SEP> 3.5 <SEP> 2.5 <SEP> 2.7 <SEP> 2.6 <SEP> 3.0 <tb> Flow <SEP> Rate <SEP> act <tb> 5.3 <SEP> 5.0 <SEP> 5.8 <SEP> 5.8 <SEP> 5.8 <SEP> 5.6 <SEP> 5.4 <SEP> 5.3 <SEP> 5.2 <SEP> 5.7 <SEP> 11.0 <SEP> 10.0 <SEP> 10.0 <SEP> 11.0 <tb> l/min <tb> Max. <SEP> Rate <SEP> wt%/h <SEP> 0.91 <SEP> 1.36 <SEP> 1.38 <SEP> 1.68 <SEP> 1.43 <SEP> 0.@5 <SEP> 0.70 <SEP> 0.53 <SEP> 0.55 <SEP> 0.80 <SEP> 0.21 <SEP> 0.31 <SEP> 0.44 <SEP> 0.55 <tb> Rate/psi <SEP> O2 <SEP> .015 <SEP> .022 <SEP> .029 <SEP> .036 <SEP> .031 <SEP> .020 <SEP> .022 <SEP> .025 <SEP> .026 <SEP> .041 <SEP> .007 <SEP> .010 <SEP> .014 <SEP> .015 <tb> Rate/psl <SEP> O2/ <tb> 16.4 <SEP> 8.9 <SEP> 4.7 <SEP> 2.0 <SEP> 0.4 <SEP> 21.9 <SEP> 4.9 <SEP> 33.3 <SEP> 18.0 <SEP> 27.4 <SEP> 1.2 <SEP> 0.7 <SEP> 0.5 <SEP> 0.3 <tb> 10-1M <SEP> catalyst <tb> H2O2 <SEP> concent. <tb> 3.2 <SEP> 4.7 <SEP> 3.5 <SEP> 2.5 <SEP> 2.7 <SEP> 1.7 <SEP> 1.5 <SEP> 1.2 <SEP> 1.7 <SEP> 2.0 <SEP> 0.8 <SEP> 1.0 <SEP> 1.5 <SEP> 1.1 <tb> wt% <tb> Organtc <SEP> Solvent <SEP> CF2ClCCl2F <SEP> CF2ClCCl2F <SEP> 1.2-C6H4Cl2 <tb> SUMMARY: EXAMPLES 15 to 27 EMI10.1 <tb> <SEP> Ih' <SEP> O <tb> <SEP> , <SEP> ¯ <SEP> C <SEP> - <SEP> c <SEP> c <SEP> t <SEP> i¯ <SEP> e- <SEP> E <tb> <SEP> C <tb> <SEP> U <SEP> 16 <SEP> 17 <SEP> = <SEP> 20 <SEP> 2.1 <SEP> 22 <SEP> 23 <SEP> 24 <SEP> 25 <SEP> 26 <SEP> 27 <tb> <SEP> .h' <SEP> C <SEP> ra <SEP> 56.1 <SEP> 09.2 <SEP> 62.9 <SEP> 63.0 <SEP> 0.5 <SEP> C <SEP> LN <SEP> > ' <SEP> a <tb> 10 <SEP> M <tb> Pp..-rtice <SEP> p-.,Ig <SEP> 1790 <SEP> 1000 <SEP> 1790 <SEP> 1010 <SEP> 1000 <SEP> 1700 <SEP> 600 <SEP> 090 <SEP> 930 <SEP> 900 <SEP> 920 <SEP> 920 <SEP> 900 <tb> D' <SEP> In <SEP> ga. <SEP> 2.5 <SEP> 2.5 <SEP> 2.5 <SEP> 2.6 <SEP> 2.7 <SEP> 2.6 <SEP> i" <tb> Flow. <SEP> fltp. <SEP> 'Ct <tb> <SEP> I <tb> <SEP> G <SEP> c <SEP> e <SEP> L; <SEP> q <SEP> ti <SEP> 0.41 <SEP> C <SEP> j <SEP> i <SEP> S <SEP> <tb> ? <SEP> 02 <SEP> .009 <SEP> .026 <SEP> .017 <SEP> .015 <SEP> .010 <SEP> .021 <SEP> .023 <SEP> .015 <SEP> .017 <SEP> .020 <SEP> .010 <SEP> .01.0 <SEP> .007 <tb> <SEP> N! <SEP> Ot <SEP> Y) <SEP> 0.2 <SEP> rX <SEP> Ln <SEP> c <SEP> c <SEP> | <SEP> s <tb> ii <SEP> e <SEP> z <SEP> z(3 <tb> <SEP> I <SEP> 1.3 <SEP> 1.0 <SEP> 1.0 <SEP> 1.0 <SEP> 1.7 <SEP> 1.3 <SEP> 0.0 <SEP> 1.6 <SEP> 2.0 <SEP> 2.0 <SEP> 1.9 <SEP> 1.9 <SEP> 0.9 <tb> <SEP> í <SEP> - <SEP> Lt <SEP> C <SEP> C <SEP> )Il.r. <tb> . <SEP> Solvent <SEP> 1p2C6II4C12 <SEP> C6116 <SEP> C01I10 <SEP> , <SEP> , <SEP> ,.- <SEP> v <SEP> cF2clc(:I.'.r. <tb> <SEP> 6 <tb> <SEP> C <SEP> - <SEP> C-r. <tb> <SEP> oi <SEP> C; <SEP> Lq, <SEP> <SEP> . <SEP> .-.-.- <SEP> - <SEP> <tb> . <SEP> 2% <SEP> ct <tb> <SEP> C0F16 <SEP> o <SEP> Kei-r' <SEP> o <SEP> ., <tb> <SEP> ¯¯¯¯ <SEP> I <SEP> I <SEP> - <SEP> -oIl. <SEP> ane <tb> <SEP> ni <SEP> om <SEP> tq <SEP> C <SEP> js <tb> <SEP> Lq <SEP> ¯, <SEP> f <SEP> Cs <SEP> C <SEP> i <SEP> 'j <SEP> U <SEP> l' <SEP> <tb> <SEP> . <SEP> I <SEP> li <SEP> < <tb> <SEP> v <SEP> c <SEP> q <SEP> Ts <SEP> i <SEP> C <SEP> Uq <SEP> o} <tb> <SEP> c <SEP> c: <SEP> c <SEP> c <SEP> r <SEP> E <SEP> c <tb> <SEP> '- <SEP> 9 <SEP> al <SEP> > <SEP> e <SEP> W <SEP> <SEP> rF <SEP> z <tb> <SEP> }' <SEP> i <SEP> = <SEP> tt <SEP> 3¯ <SEP> * <SEP> eX <tb> <SEP> DI <SEP> C <SEP> <SEP> C <SEP> E <SEP> x <SEP> 4 <SEP> XI <SEP> C <SEP> t <SEP> r <tb> <SEP> . <SEP> t:; <SEP> C <SEP> W <SEP> C <SEP> \ <SEP> z <SEP> tC <SEP> XD <SEP> C <SEP> ¯' <SEP> W <SEP> ms <tb> <SEP> I <SEP> x <SEP> S <SEP> C <SEP> C <SEP> ¯' <SEP> = <SEP> 3 <SEP> 0 <tb>

Claims: CLAIMS 1. A process for producing hydrogen peroxide wherein a gaseous mixture comprising hydrogen and oxygen is contacted with a catalyst in the presence of water and an organic solvent wherein: i) the organic solvent is immiscible with water and unreactive with hydrogen peroxide under the contacting conditions; ii) the distribution coefficient for hydrogen peroxide between the water and the organic solvent is greater than 1; iii) the catalyst is of the formula L2MX2 wherein L is a ligand represented by the formula A R1 R2 R3 wherein R1 R2 and R3 are alkyl, cycloalkyl or aryl groups, hydrogen or halogen, A is a Group 5b element selected from the group consisting of nitrogen, phos phorous and arsenic, M is a Group 8 metal and X is halogen, said catalyst being soluble in said organic solvent and insoluble in water; and iv) the gaseous mixture is non-ignitable under the process conditions characterized in that the organic solvent is selected from the group consisting of fluorocarbons, halofluorocarbons and mixtures thereof. 2. A process according to Claim 1, characterized in that the fluorocarbon and/or halofluorocarbon is aliphatic. 3. A process according to Claim 1 or 2, characterized in that the halofluorocarbon is fully substituted by halogens with at least 25% of the halogen atoms being fluorine. 4. A process according to Claim 3, characterized in that said halofluorocarbon is selected from the group consisting of l,l,2-trichlorotrifluoroethane, 1,2-dichlorotetrafluoroethane, 1,2-dibromotetrafluoroethane and mixtures thereof. 5. A process according to Claim 1, 2, 3 or 4, wherein the organic solvent comprises a halofluorocarbon and an additive selected from the group consisting of: i) 1 to 50,000 ppm by volume perfluorocarbon; ii) polymeric halofluorocarbon of molecular weight greater than 300g; iii) up to 50 ppm by weight of a C10 - C30 straight chain hydrocarbon, hydrocarbon salt, carboxylic acid, ester of a carboxylic acid or salt of a carboxylic acid or a fluorinated equivalent thereof; and mixtures thereof. 6. A process according to Claim 1 or 2, characterized in that the fluorocarbon is perfluorinated. 7. A process according to Claim 6, characterized in that the fluorocarbon is selected from the group consisting of perfluoroaliphatic ethers, perfluoroalkyl tertiary amines, perfluoropentane, perfluoro-1,3-dimethylcyclohexane and mixtures thereof. 8. A process according to any preceding Claim characterized in that the phase volume ratio of water to halofluorocarbon and/or perfluorocarbon is in the range 10:1 to 1:10. 9. A process according to Claim 8, characterized in that said ratio is in the range 2:1 to 1:3. 10. A process according to any preceding Claim characterized in that the catalyst is selected from the group consisting of bis(tri(pentafluorophenyl)phosphine) palladium dichloride, bis(tricyclohexylphosphine) palladium dichloride and bis (triphenylarsine) palladium dichloride.

Inventors: DYER, PAUL NIGEL, MOSELEY, FRED
Applicants: AIR PRODUCTS AND CHEMICALS, INC.
Application year: 1981
Main classification: C01B15
IPC codes: C01B15, B01J31