Process for producing trifluoroethylene and recycling a chlorotrifluoroethylene stream

Abstract

The present invention relates to a process for producing trifluoroethylene in a reactor having a fixed catalyst bed comprising a catalyst, the process comprising the steps of: a) reacting chlorotrifluoroethylene with hydrogen in an aqueous phase in the presence of a catalyst to produce a stream A comprising trifluoroethylene; b) treating said stream A under conditions sufficient to produce a stream D1 comprising 1,1,2-trifluoroethane with a content of less than 15% by weight, based on the total weight of stream D1; and c) recycling stream D1 to step a).

Description

[Technical field]

[0001] The present invention relates to a method for producing hydrofluoroolefins. In particular, the present invention relates to a method for producing trifluoroethylene (VF) by hydrogenolysis of chlorotrifluoroethylene. 3 ) [Background technology]

[0002] VF 3 Fluorinated olefins such as these are known and used as monomers or comonomers for the preparation of fluorocarbon polymers which exhibit particular properties, particularly excellent chemical resistance and good heat resistance.

[0003] Trifluoroethylene is a gas under standard pressure and temperature conditions. The main risks associated with the use of this product, as can be inferred from other halogenated olefins, relate to its flammability, tendency to self-polymerize if not stabilized, explosiveness due to chemical instability, and supposed susceptibility to peroxidation. Trifluoroethylene has the peculiarity of being extremely flammable, with a lower explosion limit (LEL) of about 10% and an upper explosion limit (UEL) of about 30%. However, the main danger is the decomposition of VF, which decomposes violently and explosively under certain pressure conditions in the presence of an energy source, even in the absence of oxygen. 3 This is related to the trend.

[0004] Considering the above main risks, VF 3 The synthesis of and its storage poses particular problems and imposes strict safety regulations throughout these processes. A known route for the preparation of trifluoroethylene uses chlorotrifluoroethylene (CTFE) and hydrogen as starting materials in the gas phase in the presence of a catalyst. A process for producing trifluoroethylene by hydrogenolysis of CTFE in the presence of a catalyst based on a metal from group VIII in the gas phase at atmospheric pressure and at relatively low temperatures is known from WO2013 / 128102. Summary of the Invention

[0005] According to a first aspect, the present invention relates to a process for producing trifluoroethylene in a reactor having a fixed catalyst bed comprising a catalyst, the process comprising the steps of: a) reacting chlorotrifluoroethylene with hydrogen in the vapor phase in the presence of a catalyst to produce a stream A comprising trifluoroethylene; b) treating said stream A under conditions sufficient to produce a stream D1 comprising 1,1,2-trifluoroethane in a content of less than 15% by weight, based on the total weight of stream D1; c) recycling stream D1 into step a); The present invention relates to a method comprising the steps of:

[0006] According to a preferred embodiment, stream A also contains, in addition to trifluoroethylene, unreacted chlorotrifluoroethylene and 1,1,2-trifluoroethane.

[0007] According to a preferred embodiment, stream D1 also contains chlorotrifluoroethylene with a content by weight of more than 60% by weight, based on the total weight of said stream D1.

[0008] According to a preferred embodiment, stream D1 is in the form of an azeotropic or near-azeotropic composition comprising chlorotrifluoroethylene and 1,1,2-trifluoroethane.

[0009] The presence and formation of azeotropes or quasi-azeotropes between chlorotrifluoroethylene and 1,1,2-trifluoroethane has been identified. The presence of azeotropes complicates the processes for purifying trifluoroethylene and in particular for recycling chlorotrifluoroethylene. Surprisingly, however, it has been observed that recycling a portion of the azeotrope is not detrimental to the production of trifluoroethylene. In fact, it has been observed that the yield of the hydrocracking reaction is not affected by a 1,1,2-trifluoroethane content of less than 15% in the reaction stream. It is therefore not necessary to completely remove 1,1,2-trifluoroethane from the recycle stream. This allows the purification operations of the recycle stream to be simplified, which therefore represents a significant economic benefit.

[0010] According to a preferred embodiment, stream A comprises trifluoroethylene, chlorotrifluoroethylene and 1,1,2-trifluoroethane, and step b) comprises b1) purifying said stream A comprising trifluoroethylene, chlorotrifluoroethylene and 1,1,2-trifluoroethane to form a stream C1 comprising trifluoroethylene, and a stream C2 comprising chlorotrifluoroethylene and 1,1,2-trifluoroethane; b2) purifying stream C2 to produce stream D1 and stream D2 comprising 1,1,2-trifluoroethane; Includes.

[0011] According to a preferred embodiment, step b2) is carried out by distillation at a pressure below 8 bara, preferably below 6 bara.

[0012] According to a preferred embodiment, step b2) is carried out by distillation, the temperature at the top of the distillation column being below 40°C.

[0013] According to a preferred embodiment, said catalyst is a catalyst based on a metal from groups 8 to 10 of the periodic table of the elements, preferably deposited on a support, in particular an aluminium-based support.

[0014] According to a preferred embodiment, the catalyst comprises palladium supported on alpha-alumina.

[0015] According to a preferred embodiment, the chlorotrifluoroethylene and hydrogen are in anhydrous form. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0016] The present invention relates to a process for producing trifluoroethylene, which comprises a step of hydrogenolysis reaction of chlorotrifluoroethylene (CTFE) with hydrogen in the gas phase, preferably in the presence of a catalyst.

[0017] According to a preferred embodiment, the method according to the invention described in this application is carried out continuously.

[0018] According to a preferred embodiment, in the method described in the present application, hydrogen is in anhydrous form.

[0019] According to a preferred embodiment, in the process described in the present application, the chlorotrifluoroethylene is in anhydrous form.

[0020] By carrying out the process according to the invention in the presence of anhydrous hydrogen and / or chlorotrifluoroethylene, the catalyst life and therefore the overall productivity of the process can be effectively increased.The term anhydrous refers to a water content by weight of less than 1000 ppm, advantageously less than 500 ppm, preferably less than 200 ppm, in particular less than 100 ppm, based on the total weight of the compound considered.

[0021] catalyst Preferably, the catalyst is based on a metal from columns 8 to 10 of the periodic table of the elements, in particular, the catalyst is based on a metal selected from the group consisting of Pd, Pt, Rh and Ru, preferably palladium.

[0022] Preferably, the catalyst is supported. The support is preferably selected from the group consisting of activated carbon, aluminum-based supports, calcium carbonate and graphite. Preferably, the support is based on aluminum. In particular, the support is alumina. The alumina may be alpha-alumina. Preferably, the alumina comprises at least 90% alpha-alumina. It has been observed that when the alumina is alpha-alumina, the conversion of the hydrocracking reaction is improved. Thus, the catalyst is more particularly palladium supported on alumina, advantageously palladium supported on alumina comprising at least 90% alpha-alumina, preferably palladium supported on alpha-alumina.

[0023] Preferably, palladium comprises from 0.01% to 5% by weight based on the total weight of the catalyst, preferably from 0.1% to 2% by weight based on the total weight of the catalyst.

[0024] In particular, the catalyst comprises 0.01% to 5% by weight palladium supported on alumina, the alumina preferably comprising at least 90% alpha-alumina, more preferably the alumina is alpha-alumina.

[0025] catalyst activation The catalyst is preferably activated before being used in step a). Preferably, the activation of the catalyst is carried out at high temperature and in the presence of a reducing agent. According to a particular embodiment, the reducing agent is hydrogen, carbon monoxide, nitric oxide, formaldehyde, C 1 ~C 6 Alkanes and C 1 ~C 10 Hydrohalocarbons, or mixtures thereof; preferably hydrogen or C 1 ~C 10In particular, the catalyst is activated at a temperature between 100° C. and 400° C., in particular at a temperature between 150° C. and 350° C.

[0026] Catalyst Regeneration The catalyst used in the method of the present invention can be regenerated. This regeneration step can be carried out within a catalyst bed temperature range of 90°C to 450°C. Preferably, the regeneration step is carried out in the presence of hydrogen. By carrying out the regeneration step, the reaction yield can be improved compared to the initial yield before regeneration.

[0027] According to a preferred embodiment, the regeneration step may be carried out at a catalyst bed temperature of 90° C. to 300° C., preferably at a catalyst bed temperature of 90° C. to 250° C., more preferably at a catalyst bed temperature of 90° C. to 200° C., particularly at a catalyst bed temperature of 90° C. to 175° C., more particularly at a catalyst bed temperature of 90° C. to 150° C. In particular, by carrying out the regeneration step at low temperatures, for example at 90° C. to 200° C. or 90° C. to 175° C. or 90° C. to 150° C., it is possible to desorb compounds harmful to the activity of the catalyst and / or to limit phase transitions that distort the structure of the catalyst.

[0028] According to another preferred embodiment, the regeneration step may be carried out at a catalyst bed temperature of more than 200°C, advantageously more than 230°C, preferably more than 250°C, in particular more than 300°C. The regeneration step may be carried out periodically depending on the productivity or conversion obtained in step a). The regeneration step may advantageously be carried out at a catalyst bed temperature of 200°C to 300°C, preferably 205°C to 295°C, more preferentially 210°C to 290°C, in particular 215°C to 290°C, more particularly 220°C to 285°C, preferably 225°C to 280°C, more preferably 230°C to 280°C. Alternatively, the regeneration step may be carried out at a temperature of 300°C to 450°C, preferably 300°C to 400°C. The regenerated catalyst may be reused in step a) of the process of the invention.

[0029] Hydrogenolysis Reaction The invention comprises, as mentioned above, a step of hydrocracking reaction of chlorotrifluoroethylene (CTFE) with hydrogen to produce a stream containing trifluoroethylene. The hydrocracking step is carried out in the gas phase in the presence of a catalyst. The hydrocracking step is preferably carried out in the gas phase in the presence of a preactivated catalyst. The hydrocracking step consists in simultaneously introducing hydrogen, CTFE and optionally an inert gas, such as nitrogen, in the gas phase in the presence of said catalyst, preferably an activated catalyst.

[0030] Preferably, said step a) is carried out at a fixed catalyst bed temperature of 50° C. to 250° C. Said step a) may also be carried out at a fixed catalyst bed temperature of 50° C. to 240° C., advantageously 50° C. to 230° C., preferably 50° C. to 220° C., more preferentially 50° C. to 210° C., in particular 50° C. to 200° C. Said step a) may also be carried out at a fixed catalyst bed temperature of 60° C. to 250° C., advantageously 70° C. to 250° C., preferably 80° C. to 250° C., more preferentially 90° C. to 250° C., in particular 100° C. to 250° C., more particularly 120° C. to 250° C. Said step a) may also be carried out at a temperature of the fixed catalyst bed between 60°C and 240°C, advantageously between 70°C and 230°C, preferably between 80°C and 220°C, more preferentially between 90°C and 210°C, in particular between 100°C and 200°C, more particularly between 100°C and 180°C, advantageously between 100°C and 160°C and particularly preferably between 120°C and 160°C.

[0031] H 2 The S / CTFE molar ratio is 0.5 / 1 to 2 / 1, preferably 1 / 1 to 1.2 / 1. If an inert gas such as nitrogen is present in step a), the nitrogen / H 2 The molar ratio is 0 / 1 to 2 / 1, preferably 0 / 1 to 1 / 1.

[0032] Step a) is preferably carried out at a pressure between 0.05 MPa and 1.1 MPa, more preferentially between 0.05 MPa and 0.5 MPa, in particular at atmospheric pressure.

[0033] The contact time, calculated as the ratio of the volume in liters of catalyst to the total flow rate of the gas mixture in standard liters per second at the inlet of the reactor, is between 1 and 60 seconds, preferably between 5 and 45 seconds, in particular between 10 and 30 seconds, more particularly between 15 and 25 seconds.

[0034] Processing the Reaction Stream The hydrocracking step (step a)) of the process of the present invention results in the production of a stream A comprising trifluoroethylene. Said stream A may also comprise unreacted hydrogen and unreacted chlorotrifluoroethylene. Stream A may also comprise 1,1,2-trifluoroethane as a by-product of the hydrocracking reaction. Stream A may also comprise HCl or HF or a mixture of both. Optionally, said stream A may also comprise 1,1-difluoroethane.

[0035] As mentioned above, step b) comprises: b1) purifying said stream A comprising trifluoroethylene, chlorotrifluoroethylene and 1,1,2-trifluoroethane to form a stream C1 comprising trifluoroethylene, and a stream C2 comprising chlorotrifluoroethylene and 1,1,2-trifluoroethane; b2) purifying stream C2 to produce stream D1 and stream D2 comprising 1,1,2-trifluoroethane; Includes.

[0036] Said stream C1 containing trifluoroethylene may also contain small amounts of chlorotrifluoroethylene and 1,1,2-trifluoroethane. Preferably, the content by weight of chlorotrifluoroethylene in stream C1 is less than 10% by weight, preferably less than 5% by weight, in particular less than 1% by weight, based on the total weight of stream C1. Preferably, the content by weight of 1,1,2-trifluoroethane in stream C1 is less than 10% by weight, preferably less than 5% by weight, in particular less than 1% by weight, based on the total weight of stream C1.

[0037] Depending on the composition of stream A, its purification (step b1)) may comprise several steps. Thus, if stream A contains acid compounds, such as HF or HCl, the following steps i) and ii) may be performed to remove them.

[0038] When said stream A comprises hydrogen and optionally an inert gas, the following step iii) may be carried out.

[0039] According to a particular embodiment, step b1) of the method of the invention comprises i) removing HF and / or HCl from the stream A recovered in step a) to form a gas mixture B; ii) drying mixture B from step i); iii) treating the stream B dried in step ii) to remove hydrogen and optionally inert gases to form a gas stream C; iv) distilling said stream C to form a stream C1 comprising trifluoroethylene and a stream C2 comprising chlorotrifluoroethylene and 1,1,2-trifluoroethane; may include:

[0040] The following paragraphs detail steps i) to iv).

[0041] Stream A is recovered at the reactor outlet in gaseous form. Preferably, at the outlet of the hydrocracking reactor, stream A is first treated to remove HCl and HF. Stream A is passed through water in a wash tower and then washed with a dilute base such as NaOH or KOH. The unconverted reactants (H 2The remainder of the gas mixture consisting of ethylene glycol tetrafluoroethylene (and CTFE), diluent nitrogen (if present), trifluoroethylene, 1,1,2-trifluoroethane is directed to a dryer to remove traces of washing water. Drying can be carried out using products such as calcium, sodium or magnesium sulfate, calcium chloride, potassium carbonate, silica gel or zeolites. In one embodiment, molecular sieves (zeolites) such as silipolite are used for drying. Stream B thus dried is subjected to a step of separation of hydrogen and inert substances from the remainder of the other products present in mixture B by absorption / desorption in the presence of an alcohol containing 1 to 4 carbon atoms, preferably ethanol, at atmospheric pressure and at a temperature below ambient temperature, preferably below 10°C, even more preferably below -25°C. In one embodiment, the absorption of the organic substances is carried out in a countercurrent column with ethanol cooled to -25°C. The ethanol flow rate is adjusted according to the flow rate of the organic substances to be absorbed. Hydrogen and inert gases, which are insoluble in ethanol at this temperature, are removed at the top of the absorption column. The organic substances are then recovered in the form of a gas mixture C by heating ethanol to its boiling point (desorption) for subsequent distillation. Mixture C is then purified, preferably distilled, to form a stream C1 containing trifluoroethylene and a stream C2 containing chlorotrifluoroethylene and 1,1,2-trifluoroethane. Stream C2 containing chlorotrifluoroethylene and 1,1,2-trifluoroethane is recovered at the bottom of the column. Streams A, B, C and C2 may also contain 1,1-difluoroethane.

[0042] Purification (step b2)) of said mixture C2 makes it possible to produce said stream D1 and a stream D2 comprising 1,1,2-trifluoroethane. As mentioned above, said stream D1 comprises 1,1,2-trifluoroethane with a content by weight of less than 15% based on the total weight of stream D1. In addition to 1,1,2-trifluoroethane, said stream D1 comprises chlorotrifluoroethylene and optionally 1,1-difluoroethane. Preferably, step b2) of the process of the invention is carried out by distillation. Thus, stream D1 is recovered at the top of a distillation column, while stream D2 is recovered at the bottom of the distillation column.

[0043] Step b2) is preferably carried out in order to obtain a stream D1 comprising chlorotrifluoroethylene and 1,1,2-trifluoroethane, the content by weight of 1,1,2-trifluoroethane being less than 15% based on the total weight of said stream, preferably the content by weight of 1,1,2-trifluoroethane being between 0.01% and 15% based on the total weight of said stream. More preferentially, said stream D1 comprises a content by weight of 1,1,2-trifluoroethane of less than 10% based on the total weight of said stream D1, in particular a content by weight of 1,1,2-trifluoroethane of between 0.01% and 10% based on the total weight of said stream D1.

[0044] According to a preferred embodiment, said stream D1 comprises a content by weight of chlorotrifluoroethylene of more than 60%, advantageously more than 70%, preferably more than 80%, more preferentially more than 85% and in particular more than 90%, based on the total weight of said stream D1.

[0045] Preferably, step b2) is carried out by distillation at a pressure of less than 8 bara, preferably less than 6 bara. More preferentially, step b2) is carried out at a pressure of between 1 and 6 bara.

[0046] Preferably, step b2) is carried out by distillation and the temperature at the top of the distillation column is below 40°C, in particular the temperature at the top of the distillation column is between -40°C and 40°C, more particularly the temperature at the top of the distillation column is between -35°C and 30°C.

[0047] Under these operating conditions, stream D1 is preferably in the form of an azeotropic or near-azeotropic composition comprising chlorotrifluoroethylene and 1,1,2-trifluoroethane.

[0048] Stream D1 described in this application is recycled to step a) of the process of the invention. The steps of the process of the invention are repeated. After recycling of stream D1, a suitable CTFE / H 2 To maintain the ratio, a fresh CTFE stream is mixed with stream D1. EXAMPLES

[0049] 25cm 3 The catalyst (0.2% palladium supported on α-alumina) was introduced into a tubular reactor consisting of a jacketed stainless steel tube 1200 mm long and 25 mm in diameter. The catalyst thus loaded was then activated as follows: the reactor tube was placed in a tubular furnace and fed with a stream of hydrogen (0.05-0.1 moles per gram of catalyst). The catalyst bed was heated to a temperature of 200°C-250°C with a temperature gradient of 0.2°C / min. After this activation period, the tube was cooled to ambient temperature and then isolated for installation in a hydrocracking test bed.

[0050] Four test beds were used in parallel, each with a reactor prepared as described above. The four beds were fed with 1 mole / h of starting composition and 1 mole / h of hydrogen in anhydrous form. The temperature of the reactor jacket was 25° C. The contact time, calculated as the ratio of the volume in liters of catalyst to the sum of the flow rates of the reactants in standard liters per second, was about 22 seconds. Tests were carried out using different starting compositions. Comparative Example 1 was used starting from chlorotrifluoroethylene. Example 2 according to the invention was carried out starting from the chlorotrifluoroethylene used in the comparative example, to which 1,1,2-trifluoroethane (3.9%) was added.

[0051] The results are shown in Table 1 below. [Table 1] TIFF2024522563000001.tif27170

[0052] The productivity mentioned corresponds to the sum of the productivity obtained for all four hydrocracking beds. As can be seen, the productivity of trifluoroethylene is significantly improved starting from the composition according to the invention compared to the chlorotrifluoroethylene composition without additional compounds.

Claims

1. 1. A process for producing trifluoroethylene in a reactor having a fixed catalyst bed containing a catalyst, comprising: a) reacting chlorotrifluoroethylene with hydrogen in the vapor phase in the presence of a catalyst to produce a stream A comprising trifluoroethylene; b) treating said stream A under conditions sufficient to produce a stream D1 comprising 1,1,2-trifluoroethane in a content of less than 15% by weight, based on the total weight of stream D1; c) recycling stream D1 to step a); and The method includes:

2. 2. The process of claim 1, wherein stream A also contains, in addition to trifluoroethylene, unreacted chlorotrifluoroethylene and 1,1,2-trifluoroethane.

3. 2. The process according to claim 1, characterized in that stream D1 also contains chlorotrifluoroethylene with a content by weight of more than 60% by weight, based on the total weight of said stream D1.

4. 2. The process according to claim 1, characterized in that stream D1 is in the form of an azeotropic or near-azeotropic composition comprising chlorotrifluoroethylene and 1,1,2-trifluoroethane.

5. Stream A comprises trifluoroethylene, chlorotrifluoroethylene and 1,1,2-trifluoroethane, and step b) comprises b1) purifying said stream A comprising trifluoroethylene, chlorotrifluoroethylene and 1,1,2-trifluoroethane to form a stream C1 comprising trifluoroethylene, and a stream C2 comprising chlorotrifluoroethylene and 1,1,2-trifluoroethane; b2) purifying stream C2 to produce said stream D1 and a stream D2 comprising 1,1,2-trifluoroethane; The method of claim 1 , comprising:

6. 6. The process according to claim 5, characterized in that step b2) is carried out by distillation at a pressure below 8 bara, preferably below 6 bara.

7. 6. The process according to claim 5, characterized in that step b2) is carried out by distillation and the temperature at the top of the distillation column is below 40°C.

8. 2. The method according to claim 1, characterized in that the catalyst is a catalyst based on a metal from groups 8 to 10 of the periodic table of the elements, preferably deposited on a support, in particular an aluminium-based support.

9. 9. The process of claim 8, wherein the catalyst comprises palladium supported on alpha-alumina.

10. 2. The process according to claim 1, characterized in that the chlorotrifluoroethylene and hydrogen are in anhydrous form.