The present invention relates to processes useful in the production of hydro(chloro)fluoroolefins, for example in relation to the cleaning and/or purification of intermediate and product streams. In particular, the invention provides methods for cleaning and/or purifying product streams comprising fluoropropenes such as 1 ,3,3,3- tetrafluoropropene (HFO-1234ze) and 2,3,3,3-tetrafluoropropene (HFO-1234yf).

(Hydro)halocarbons are typically used as refrigerant or propellant materials and as blowing agents. Over the last 20 years, the variety of (hydro)halocarbons used in these applications has changed as it has been discovered that some such materials (such as difluorodichloromethane, R12) deplete the earth's ozone layer, while others (such as 1 ,1 , 1 ,2-tetrafluoroethane, R134a) have an unacceptably high action as a greenhouse gas. Hydro(chloro)fluoroolefins have emerged as a class of compounds which may address these problems by providing good performance as refrigerants, propellant materials and as blowing agents, while also having a low ozone depletion potential and a low global warming potential. Various methods have been proposed for the production of hydro(chloro)fluoroolefins. Such methods require the removal of unused reagents and reaction by-products before the resulting product is in a condition fit for sale. Scrubbing techniques which have previously been used in the production of hydrofluorocarbon compounds have been found to degrade the hydro(chloro)fluoroolefin products such that the number and quantity of by- products is increased and the overall product yield falls.

Accordingly, there is a need for a process of cleaning and/or purifying a hydro(chloro)fluoroolefin product stream which is both effective and provides for a minimal degradation of the relevant product, which reduces product yield and may create waste streams which contain hazardous materials and/or are difficult or expensive to dispose of. The present invention provides such a process.

There is also a need for an efficient method for removing unwanted water from a hydro(chloro)fluoroolefin product stream as, for example, methods of cleaning and/or purifying the product stream may introduce water to the product stream. The present invention provides such a process. In a first aspect, the present invention provides a method comprising a first drying stage which comprises contacting a first fluid stream comprising one or more hydro(chloro)fluoroolefins and water with a source of sulphuric acid to produce a first treated fluid stream comprising the hydro(chloro)fluoroolefin(s) and a first spent sulphuric acid stream, wherein the first treated fluid stream comprises a lower concentration of water than the first fluid stream.

Preferably, the first treated fluid stream comprises less than 1wt% water, for example less than about 500 ppm water. More preferably, the first treated fluid stream contains less than about 250 ppm water, less than 100 ppm water or less than 10 ppm water.

Preferably, the first fluid stream comprises less than about 20wt% HF, for example less than 10wt% HF, less than 5wt% HF or less than 1wt% HF. In some embodiments the first fluid stream comprises no more than trace quantities of HF.

Preferably, the first fluid stream comprises less than about 20wt% HCI, for example less than 10wt% HCI, less than 5wt% HCI or less than 1wt% HCI. In some embodiments the first fluid stream comprises no more than trace quantities of HCI. Preferably the first drying stage is performed in a first sulphuric scrubbing vessel. Preferably, the residence time of the first fluid stream in the first scrubbing vessel is between about 1s and about 60s. Preferably, the residence time of the first source of sulphuric acid in the first sulphuric scrubbing vessel is between about 5s and 10000s. Preferably, at least 50wt% of the first fluid stream comprises the hydro(chloro)fluoroolefin(s). More preferably, at least 60wt%, 70wt% or 80wt% of the first fluid stream comprises hydro(chloro)fluoroolefin(s). In certain preferred embodiments, at least 50wt% of the first fluid stream comprises one hydro(chloro)fluoroolefin. More preferably, at least 60wt%, 70wt% or 80wt% of the first fluid stream comprises one hydro(chloro)fluoroolefin.

In some preferred embodiments, at least 50wt% of the first fluid stream comprises a hydro(chloro)fluoroolefin selected from the group hydrofluoropropenes, hydrochlorofluoropropenes, hydrofluoroethylenes, hydrofluorobutenes and hydrochlorofluorobutenes. More preferably, at least 60wt%, 70wt% or 80wt% of the first fluid stream comprises a hydro(chloro)fluoroolefin selected from the group hydrofluoropropenes, hydrochlorofluoropropenes, hydrofluoroethylenes, hydrofluorobutenes and hydrochlorofluorobutenes. Preferred hydro(chloro)fluoroolefins include HFO-1234yf, HFO-1234ze, 1-chloro-3,3,3-trifluoropropene (HCFO-1233zd), 2- chloro-3,3,3-trifluoropropene (HCFO-1233xf), 1 , 1 , 1-4,4,4-hexafluoro-but-2-ene (HFO- 1336mzz) and 1 , 1-difluoroethylene (HFO-1132a).

In preferred embodiments, the first source of sulphuric acid comprises aqueous sulphuric acid at a concentration between around 60wt% and around 98wt%. More preferably, the first source of sulphuric acid comprises aqueous sulphuric acid at a concentration between around 75wt% and around 95wt%, for example between around 78wt% and about 94wt%. In certain embodiments, the first source of sulphuric acid comprises aqueous sulphuric acid at a concentration between about 78wt% and about 90wt%. The inventors have found that even small reductions in the concentration of the sulphuric acid as compared to concentrated sulphuric acid provide significant reductions in the degradation of the hydro(chloro)fluoroolefin(s), thereby providing greater final product yields and reducing the concentration of potentially hazardous organic material in the spent sulphuric acid stream.

It is preferred that the first fluid stream is in the vapour phase when contacted with the source of sulphuric acid. Preferably, the first fluid stream is contacted with the source of sulphuric acid at a temperature between about 10°C and about 70°C, for example between about 20°C and about 60°C. Most preferably, the first fluid stream is contacted with the source of sulphuric acid at a temperature between about 20°C and 40°C, for example between about 25°C and 35°C, e.g. around 30°C. It is preferred that the first fluid stream is contacted with the source of sulphuric acid at a sufficiently high temperature to minimise or prevent condensation of the hydro(chloro)fluoroolefin.

Preferably, the first spent sulphuric stream comprises less than about 20000 ppm fluoride, for example less than about 15000 ppm fluoride, e.g. less than about 10000 ppm fluoride, less than about 8000 ppm fluoride, less than about 5000 ppm fluoride, less than about 4000 ppm fluoride, less than about 3000 ppm fluoride or less than about 2000 ppm fluoride. In some embodiments, the first spent sulphuric stream comprises less than about 1000 ppm fluoride, for example less than about 500 ppm fluoride. In most preferred embodiments, the first spent sulphuric stream comprises less than about 100 ppm fluoride, for example less than about 80 ppm fluoride, less than about 50 ppm fluoride, less than about 40 ppm fluoride or less than about 25 ppm fluoride.

In preferred embodiments, the first spent sulphuric stream comprises less than about 10000 ppm total organic carbon. For example, in some embodiments, the first spent sulphuric stream comprises less than about 8000 ppm total organic carbon, less than about 5000 ppm total organic carbon, less than about 4000 ppm total organic carbon, less than about 3000 ppm total organic carbon or less than about 2000 ppm total organic carbon. In some embodiments, the first spent sulphuric stream comprises less than about 1000 ppm total organic carbon. In most preferred embodiments, the first spent sulphuric stream comprises less than about 500 ppm total organic carbon, for example less than about 250 ppm total organic carbon, less than about 100 ppm total organic carbon, less than about 50 ppm total organic carbon or less than about 25 ppm total organic carbon. In some embodiments, the method comprises a second drying step comprising contacting the first treated fluid stream with a second source of sulphuric acid to produce a second treated fluid stream comprising the hydro(chloro)fluoroolefin(s) and a second spent sulphuric acid stream, wherein the second treated fluid stream comprises a lower concentration of water than the first treated fluid stream. In such an embodiment it is preferred, though not essential, that the first source of sulphuric acid comprises aqueous sulphuric acid in a concentration between about 78wt% and about 90wt%.

The inventors have found that providing a second drying step, it is possible to perform the first drying step under milder conditions, allowing for the removal of significant quantities of water from the first fluid stream while minimising reaction with the hydro(chloro)fluoroolefin(s).

Preferably the second drying stage is performed in a second sulphuric scrubbing vessel. Preferably, the residence time of the first treated fluid stream in the second scrubbing vessel is between about 1 s and about 60s. Preferably, the residence time of the second source of sulphuric acid in the second sulphuric scrubbing vessel is between about 5s and 10000s. Where a second drying step is included, it is preferred that the residence time of the first source of sulphuric acid in the first sulphuric scrubbing vessel is between about 5s and 500s.

Preferably, the second treated fluid stream comprises less than about 500 ppm water. More preferably, the second treated fluid stream contains less than about 250 ppm water, less than 100 ppm water or less than 10 ppm water. In preferred embodiments, the second source of sulphuric acid comprises aqueous sulphuric acid at a concentration between around 60wt% and around 98wt%. More preferably, the second source of sulphuric acid comprises aqueous sulphuric acid at a concentration between around 75wt% and around 95wt%, for example between around 78wt% and about 94wt%. In certain embodiments, the second source of sulphuric acid comprises aqueous sulphuric acid at a concentration between about 90wt% and about 94wt%.

It is preferred that the first treated fluid stream is in the vapour phase when contacted with the second source of sulphuric acid. Preferably, the first fluid stream is contacted with the source of sulphuric acid at a temperature between about 10°C and about 70°C, for example between about 20°C and about 60°C. Most preferably, the first treated fluid stream is contacted with the second source of sulphuric acid at a temperature between about 20°C and 40°C, for example between about 25°C and 35°C, e.g. around 30°C. It is preferred that the first fluid stream is contacted with the source of sulphuric acid at a sufficiently high temperature to minimise or prevent condensation of the hydro(chloro)fluoroolefin.

Preferably, the second spent sulphuric stream comprises less than about 20000 ppm fluoride, for example less than about 15000 ppm fluoride, e.g. less than about 10000 ppm fluoride, less than about 8000 ppm fluoride, less than about 5000 ppm fluoride, less than about 4000 ppm fluoride, less than about 3000 ppm fluoride or less than about 2000 ppm fluoride. In some embodiments, the second spent sulphuric stream comprises less than about 1000 ppm fluoride, for example less than about 500 ppm fluoride. In most preferred embodiments, the second spent sulphuric stream comprises less than about 100 ppm fluoride, for example less than about 80 ppm fluoride, less than about 50 ppm fluoride, less than about 40 ppm fluoride or less than about 25 ppm fluoride.

In preferred embodiments, the second spent sulphuric stream comprises less than about 10000 ppm total organic carbon. For example, in some embodiments, the second spent sulphuric stream comprises less than about 8000 ppm total organic carbon, less than about 5000 ppm total organic carbon, less than about 4000 ppm total organic carbon, less than about 3000 ppm total organic carbon or less than about 2000 ppm total organic carbon. In some embodiments, the second spent sulphuric stream comprises less than about 1000 ppm total organic carbon. In most preferred embodiments, the second spent sulphuric stream comprises less than about 500 ppm total organic carbon, for example less than about 250 ppm total organic carbon, less than about 100 ppm total organic carbon, less than about 50 ppm total organic carbon or less than about 25 ppm total organic carbon. Preferably, the first and/or, if produced, second treated fluid stream(s) comprise the hydro(chloro)fluoroolefin(s) in a substantially pure state or as part of a mixture of hydro(chloro)fluoroolefins and/or other halogenated organic compounds. In preferred embodiments, the first and/or, if produced, second treated fluid stream is contacted with an adsorbent material. The adsorbent material removes or reduces the concentration of one or more components selected from residual acid (e.g. residual HF and/or residual HCI), residual water and/or residual impurities such as residual organic impurities.

In some embodiments, the adsorbent material comprises soda lime. In other embodiments, the adsorbent material comprises one or more molecular sieves, for example one or more zeolites having pores sizes in the region of 2A to 10A, e.g. about 3A to about 6A.

In some embodiments, the second treated fluid stream, optionally having been contacted with the adsorbent material, is subjected to distillation to separate some or all of the remaining components, for example to provide a substantially pure product stream. In certain preferred embodiments, the method comprises a preceding acid removal step. The acid removal step preferably comprises the treatment of a crude product stream to remove at least a portion of any HF and/or HCI in the crude product stream to provide the first fluid stream. Preferably, the crude product stream is the product stream of a dehydrohalogenation reaction (e.g. a dehydrofluorination and/or dehydrochlorination reaction). More preferably, the dehydrohalogenation reaction provides the one or more hydro(chloro)fluoroolefins. As such, the crude product stream may contain HF and/or HCI in a molar concentration of around 0.5 to 1.5 times (e.g. 0.8 to 1.2 times) the molar concentration of the hydro(chloro)fluoroolefin(s) in the crude product stream. The crude product stream may also comprise one or more (hydro)haloalkanes, which may represent by-products of the dehydrohalogenation reaction and/or one or more unreacted starting materials.

In one preferred embodiment, the acid removal step comprises contacting the crude product stream with water to produce a spent stream of aqueous acid (e.g. HF and/or HCI) and a treated product stream, the treated product stream having a lower acid concentration (e.g. a lower HF and/or HCI concentration) than the crude product stream. In an alternative embodiment, the acid removal step comprises contacting the crude product stream with a source of aqueous acid, e.g. a source of aqueous HF and/or HCI to produce a spent stream of aqueous acid (e.g. HF and/or HCI) and a treated product stream, the treated product stream having a lower acid concentration (e.g. a lower HF and/or HCI concentration) than the crude product stream. Preferably, the source of aqueous acid comprises aqueous HF in a concentration of at least about 40wt% or at least about 50wt%. Most preferably, the source of aqueous acid comprises aqueous HF in a concentration between about 40wt% and about 60wt%. In an alternative embodiment, the source of aqueous acid comprises aqueous sulphuric acid, for example in a concentration less than about 98wt%, e.g. less than about 95wt% or less than about 90wt%.

In certain embodiments, HF and/or HCI is recovered from the spent stream of aqueous acid, for example by flash separation and/or distillation. In some embodiments, the treated product stream is provided directly to the first drying stage, for example in the form of the first fluid stream. In other embodiments, the treated product stream is subjected to one or more further treatment steps before being provided to the first drying stage. Preferably, the treated product stream is subjected to a second acid removal step. The second acid removal step preferably comprises contacting the treated product stream with an aqueous alkali to produce a second treated product stream and a spent aqueous alkali stream, the second treated product stream having a lower acid concentration than the treated product stream. In preferred embodiments, the source of aqueous alkali comprises aqueous caustic, for example aqueous NaOH or KOH. Preferably the aqueous NaOH or KOH is provided at a concentration of less than about 20wt%, for example less than about 15wt%, less than about 10wt% or less than about 5wt%.

In some embodiments, the second treated product stream is provided directly to the first drying stage, for example in the form of the first fluid stream. In other embodiments, the second treated product stream is subjected to one or more further treatment steps before being provided to the first drying stage.

In a further aspect of the invention, there is provided an integrated process for producing one or more hydro(chloro)fluoroolefins comprising:

(i) dehydrohalogenating one or more hydro(chloro)fluoroalkanes to form a crude product stream; (ii) subjecting the crude product stream to a first acid removal step comprising contacting the crude product stream with water or a source of aqueous acid to produce a treated product stream and a spent aqueous acid stream;

(iii) optionally subjecting the treated product stream to a second acid removal step comprising contacting the treated product stream with a source of aqueous alkali to produce a second treated product stream and a spent aqueous alkali stream;

(iv) subjecting the treated product stream or, if produced, the second treated product stream, in the form of a first fluid stream, to a first drying stage comprising contacting the first fluid stream with a source of sulphuric acid to produce a first treated fluid stream comprising the hydro(chloro)fluoroolefin(s) and a first spent sulphuric acid stream.

In a further aspect, the invention provides a method for removing acid from a crude product stream of a dehydrohalogenation reaction, the crude product stream containing one or more hydro(chloro)fluoroolefins, the method comprising:

(i) subjecting the crude product stream to a first acid removal step comprising contacting the crude product stream with water or a source of aqueous acid to produce a treated product stream and a spent aqueous acid stream;

(ii) optionally subjecting the treated product stream to a second acid removal step comprising contacting the treated product stream with a source of aqueous alkali to produce a second treated product stream and a spent aqueous alkali stream.

In some embodiments, the method comprises subjecting the treated product stream or, if produced, the second treated product stream, in the form of a first fluid stream, to a first drying stage comprising contacting the first fluid stream with a source of sulphuric acid to produce a first treated fluid stream comprising the hydro(chloro)fluoroolefin(s) and a first spent sulphuric acid stream.

In another aspect, the invention provides a spent scrubbing liquor comprising aqueous sulphuric acid in a concentration of less than around 98wt% (for example less than around 95wt%, 90wt%, 85wt%, 80wt%, 75wt%, 70wt%, 65wt%, 60wt%, 55wt% or 50wt%) and at least one compound selected from fluoracrylic acid, polyfluoracrylic acid, formic acid and fluoroformaldehyde, and/or one or more unsaturated fluorine containing oligomers. Preferably, the spent scrubbing liquor comprises sulphuric acid in a concentration between 50wt% and 98wt%, for example between 75wt% and 95wt%, e.g. between 75wt% and the or a concentration of sulphuric acid in a scrubbing step which produces the spent liquor. Preferably, the spent liquor comprises less than about 20000 ppm fluoride, less than about 15000 ppm fluoride, less than about 10000 ppm fluoride, less than about 8000 ppm fluoride, less than about 5000 ppm fluoride, less than about 4000 ppm fluoride, less than about 3000 ppm fluoride, less than about 2000 ppm fluoride, less than about 1000 ppm fluoride, less than about 500 ppm fluoride, less than about 100 ppm fluoride, less than about 80 ppm fluoride, less than about 50 ppm fluoride, less than about 40 ppm fluoride or less than about 25 ppm fluoride.

Preferably, the spent liquor comprises less than about 10000 ppm total organic carbon, less than about 8000 ppm total organic carbon, less than about 5000 ppm total organic carbon, less than about 4000 ppm total organic carbon, less than about 3000 ppm total organic carbon or less than about 2000 ppm total organic carbon, less than about 1000 ppm total organic carbon, less than about 500 ppm total organic carbon, less than about 250 ppm total organic carbon, less than about 100 ppm total organic carbon, less than about 50 ppm total organic carbon or less than about 25 ppm total organic carbon.

In another aspect of the invention, there is provided the use of a spent scrubbing liquor as described above in the production of a regenerated scrubbing liquor comprising sulphuric acid having a concentration between around 60wt% and around 98wt% (for example 75wt% and around 95wt%, for example between around 78wt% and about 94wt% or between about 78wt% and about 90wt%) for use in a scrubbing method as described herein.

In another aspect, the invention provides for the use of a regenerated scrubbing liquor as described herein in a scrubbing method as described herein.

In other embodiments, the spent liquor may be processed to be neutralised and to remove at least partially any fluoride and or organic compounds to allow for safe disposal. As will be understood by the skilled person, any of the preferred and alternative embodiments presented above may be applicable to any of the described aspects of the invention.

Embodiments of the present invention will now be described with reference to the following examples and drawings: Figure 1 shows a schematic diagram of a scrubbing train for performing a method in accordance with the present invention;

Figures 2 to 7 show response surface plots of fluoride and total organic carbon produced by contacting HFO-1234ze with sulphuric acid.

An embodiment of the present invention is shown in Figure 1 , which shows a scrubbing train 10 for treating the crude product of a dehydrohalogenation reaction. The crude product contains HFO-1234ze, though the scrubbing train may also be utilised in the production of other hydro(chloro)fluoroolefins such as HFO-1234yf, HCFO-1233zd, HFO- 1233xf, HFO-1 132a and HFO-1336mzz. The crude product stream, in addition to HFO- 1234ze, also contains HF and/or HCI, as has been produced by the dehydrohalogenation, unreacted starting materials such as 1 , 1 , 1 ,3,3-pentafluoropropane (HFC-245fa) and/or 1- chloro-1 ,3,3,3-tetrafluoropropane (HCFC-244fa), together with other organic materials, such as those produced as by-products of the dehydrohalogenation reaction.

In brief, the crude product stream is passed into a first scrubbing column 20 through a feed line 22, while water is supplied to the scrubbing column 20 through scrubbing line 24. The scrubbing line 24 provides a mass flow of water sufficient to produce an effluent flow which has a HF concentration of around 5wt%. The bulk of the HF and/or HCI present in the crude product stream is dissolved or otherwise absorbed in the water in the scrubbing column 20 to produce a first spent stream of aqueous HF and/or HCI, which is passed from the scrubbing column 20 through a first effluent line 26. A first treated product stream, having substantially reduced HF and/or HCI content, exits the first scrubbing column 20 through a second feed line 28 to be passed to a second scrubbing column 30.

In the second scrubbing column 30, the first treated product stream is contacted with a supply of aqueous caustic material, for example aqueous KOH, which is supplied to the scrubbing column 30 through a second scrubbing line 34. The concentration of the preferred aqueous KOH may be around 20wt%. The aqueous caustic material reacts with remaining traces of HF and/or HCI in the treated product stream to produce a spent caustic stream which passes from the scrubbing column 30 through a second effluent line 36. A second treated product stream is passed from the second scrubbing column 30 through a third feed line 38 to a third scrubbing column 40. The third scrubbing column 40, is adapted to remove water introduced to the second treated product stream during treatment in the first and second scrubbing columns 20, 30. In the third scrubbing column the second treated product stream is contacted with a supply of aqueous sulphuric acid at a concentration of around 78wt% to around 90wt%, which is supplied to the scrubbing column 40 through a third scrubbing line 44. The aqueous sulphuric acid acts to remove a portion of the water present in the second treated product stream, while the concentration of the sulphuric acid is sufficiently low to reduce the risk of significant degradation of the desired end product of HFO-1234ze. The spent aqueous sulphuric acid is removed from the third scrubbing column 40 through a third effluent line 46, while a third treated product stream is passed from the third scrubbing column 40 through a third feed line 48 to a fourth scrubbing column 50. The fourth scrubbing column 50 provides for the further removal of water from the third treated product stream. In the fourth scrubbing column 50 the third treated product stream is contacted with a supply of aqueous sulphuric acid at a concentration of around 90wt% to around 98wt%, most preferably around 90wt%, which is supplied to the scrubbing column 50 through a third scrubbing line 54. The aqueous sulphuric acid acts to provide a high degree of removal of the remaining water present in the third treated product stream. The relatively high concentration of sulphuric acid ensures that the rate of removal of water is higher than in the third scrubbing column 30, however lower starting concentration of water in the third treated product stream compared to the second product stream allows for a lower contact time and/or volume of acid, thereby reducing the risk of significant degradation of the desired end product of HFO-1234ze. The spent aqueous sulphuric acid is removed from the fourth scrubbing column 50 through a fourth effluent line 56, while a fourth treated product stream is passed from the fourth scrubbing column 50 through a fourth feed line 48 to a polishing bed 60. The polishing bed 60 comprises an adsorbent material such as Sofnolime (RTM) soda lime or a molecular sieve such as a zeolite having a pore diameter in the region of 2k to 6A. The polishing bed removes any residual water, acids and impurities from the fourth treated product stream. The resulting product stream may be subjected to further distillation.

All effluent streams 26, 36, 46, 56 may be disposed of or be sent to recovery to ensure further use of any commercially valuable components, such as HF and/or HCI and/or any organic components they may contain. However, in some embodiments, the effluent stream 56 of the fourth scrubbing column 50 may be recycled by supplying it to the third scrubbing line 30 for use in the third scrubbing column 40. In some embodiments, the first scrubbing column 20 may be replaced by one or more columns where the scrubbing fluid comprises aqueous HF, for example in a concentration around 50wt%. In such embodiments, the concentration of HF in the effluent fluid would be expected to be greater than that of the scrubbing fluid and allows effective recovery of HF therefrom, for example by absorbing the HF into the scrubbing liquid to increase the HF concentration to around 70wt%, followed by distillation of the around 70wt% HF into a stream of essentially anhydrous HF that can be recovered for use in other processes and a stream comprising around 50wt% HF which can be returned to the column replacing column 20.

Reference Examples

Batchwise experiments were performed in 100ml Hastelloy autoclaves with 30ml sulphuric acid of varying concentrations. After evacuating the headspace, the reaction vessels were then charged with HFO-1234zeE to reach a pressure of lObarg (approx. 1.2g HFO- 1234zeE). The autoclaves were submerged in a water bath at varied temperatures and stirred at 500rpm for varying periods of time, all as shown in Table 1.

Fluoride measurements

The spent liquor from each autoclave was tested for its fluoride content by use of an ion selective electrode. Prior to measurement, the solutions were adjusted to pH 5.5 with buffer solution. The original sulphuric acid solution did not contain any fluoride. The results are shown in Table 1.

Total organic carbon measurement

The spent liquor from each autoclave was also tested for its total organic carbon (TOC) content before and after sparging with compressed air for 30 minutes. The original sulphuric acid solution did not contain any organic carbon. The results are shown in Table 1. Table 1

The results were plotted into a series of response surface plots as shown in Figures 2 to 5. Figure 2 shows the fluoride level versus temperature and contact time after reaction with HFO-1234zeE at a constant sulphuric acid concentration of 98wt%. Increasing time and temperature each individually appear to increase the fluoride content in the spent solution, but the combination of both has the greatest influence, as shown by the upwards slope of the surface towards the highest temperatures and longest contact times in the far corner of the plot. Figure 3 shows the TOC levels measured at different temperatures and contact times of H2SO4 at a concentration of 98wt% with HFO-1234zeE. Again, increasing temperature and time each individually increase the TOC content, but the combination of both has the greatest influence. The overall TOC levels appear high, indicating a relatively severe reaction of the organic with H2SO4.

The sparging of a sample of each solution with air was designed to remove any medium to low boilers produced as a result of decomposition, and highlight an option for treatment of the solutions prior to disposal. The results however, show no statistical difference within the 95% confidence limits between samples before and after sparging.

A response surface plot in Figure 4 shows how the fluoride content remaining in solution changes with contact time and the concentration of sulphuric acid between 78wt% and 98wt% at a constant temperature of 30°C. At low sulphuric acid concentration and short contact times, there are only very low levels of fluoride, which increase very slowly with increasing contact times and sulphuric acid concentration. As the sulphuric acid concentration approaches 98wt%, the fluoride levels suddenly increase sharply, particularly at high contact times.

The TOC results (see Figure 5) obtained for sulphuric acid concentration varying from 78wt% to 98wt% at a constant temperature of 30°C show a similar trend to the fluoride results, in that there is very little TOC present at low sulphuric acid concentrations and short contact times, but as the concentration reaches 98wt%, the TOC levels appear to rise rapidly, regardless of contact time.

Further experiments were conducted to investigate the effect of sulphuric acid concentrations in excess of 90wt% on the stability of the HFO-1234zeE, the results of which are shown in Table 2. No investigation of TOC was performed in these experiments. Table 2

Figure 6 shows a response surface plot of fluoride concentrations against sulphuric acid concentration between 90wt% and 98wt% at a constant temperature of 30°C. As can be seen, there is a gradual increase in fluoride with increasing contact time and sulphuric acid concentrations. There appear to be acceptably low levels of fluoride at the lower concentrations. Figure 7 shows a similar plot focussed on sulphuric acid concentrations between 94wt% and 98wt%. The concentration of water in HFO-1234zeE is a function of the concentration of sulphuric acid with which it contacts and the efficiency of the scrubber. Data demonstrating the partial pressure of water above sulphuric acid solutions of varying concentrations can be used to determine the equilibrium concentration. This data suggests that the concentration of sulphuric acid provided to the final (or only) sulphuric acid scrubber should be above 80wt% to achieve a concentration of water in HFO-1234zeE below 100 ppm. The present results show that at 94wt% sulphuric acid the fluoride levels range from 37-76 ppm over the different contact times. As the sulphuric acid concentration is increased from 94wt%, the fluoride concentration in the spent sulphuric acid quickly starts to rise. It thus appears that an optimum sulphuric acid concentration for drying hydro(chloro)fluoroolefins such as HFO-1234ze would be between about 90wt% and about 94wt%. As can also be seen from the results presented above, concentrations of sulphuric acid below 90wt%, for example between 78wt% and 90wt%, provide manageable levels of fluoride and TOC (and thus product degradation) and as such concentrations in that range are considered optimal for the first of two sulphuric acid drying stages. As can also be seen from the results presented above, concentrations of sulphuric acid below 90wt%, for example between 78wt% and 90wt%, provide manageable levels of fluoride and TOC (and thus product degradation) and as such concentrations in that range have been found to be optimal for the first of two sulphuric acid drying stages. Reference Example 56

A further experiment was performed using 30 ml_ of 94wt% H2SO4 warmed to 30°C and stirred at 500 rpm. After evacuating the headspace the autoclave was charged to 2.0 barg with HFO-1234yf (1.2g) and reacted for 60 min before analysing the spent H2SO4 liquors for fluoride concentration. The spent sulphuric acid solution contained no detectable fluoride.

Example 57

Drying of hydrofluoroolefins with high and reduced concentrations of sulphuric acid.

300g of either HFO-1234ze(E) or HFO-1234yf was added to a 500 ml_ Whitey bomb and doped with -300 ppm of water. The moisture content of the composition was analysed before and after the addition of the water. 30g of the wet hydrofluoroolefin was added to a Whitey bomb containing 50 ml_ of sulphuric acid (at a concentration of either 98wt% (aq) or 80wt% (aq)) and shaken for 10 minutes. The dried hydrofluoroolefin was subsequently isolated from the Whitey bomb at 10 °C and analysed for moisture content. The results of drying with 98wt% H2SO4 (aq) are presented in Tables 3 and the results of drying 80wt% H2SO4 (aq) are presented in Table 4. Table 3

It is clear from this direct comparison that the drying performance of sulphuric acid remains sufficiently high at a lower concentration for a range of hydrofluoroolefins. The high performance at a reduced concentration results in reduced degradation of the desired hydrofluoroolefin and thus greater final product yields. The reduced concentration of sulphuric acid also reduces the concentration of potentially hazardous organic material in the spent sulphuric acid stream.

Example 58

A water containing sample of (E)-1234ze was dried [by agitating] at 60°C in [contact with] a scrubbing medium comprising 98 % wt sulphuric acid. The mixture was then neutralised and extracted with a solvent. The solvent extract was dried, filtered and concentrated. Samples of the concentrated extract were taken and analysed by 1-D NMR ( ¹ H, ¹³ C and ¹⁹ F), 2-D NMR ( ¹ H- ¹ H COSY and ¹ H- ¹³ C HSQC), gas chromatography and ISE to identify the decomposition products and pathways.

Several decomposition products were identified in the spent scrubbing solution, including fluoracrylic acid, polyfluoracrylic acid, formic acid and fluoroformaldehyde, together with several unsaturated fluorine containing oligomers.

Preferences and options for a given aspect, feature or parameter of the invention should, unless the context indicates otherwise, be regarded as having been disclosed in combination with any and all preferences and options for all other aspects, features and parameters of the invention.

Where a molecule, for example HFO-1234ze, may take the form of E and Z isomers, the general disclosure of that molecule is intended to refer equally to both the E and Z isomers.