METHOD FOR THE REMOVAL OF BENZOLE AND CHLOROPRENE FROM A VINYL CHLORIDE-CONTAINING PROCESS STREAM

Description

[0001] The invention relates to a process of removing by-products from a vinyl chloride comprising process stream from a 1,2-dichloroethane thermal cracking process. The invention also relates to the use of a specific heterogeneous iron-aluminium(oxide)-catalyst in a process of removing by-products from such process stream following a 1,2-dichloroethane thermal cracking process.

[0002] Vinyl chloride is a valuable commercial product used foremost for the production of polyvinyl chloride, one of the most important synthetic polymer plastics. Vinyl chloride is, therefore, also referred to as vinyl chloride monomer (VCM). One process for producing VCM involves the thermal cracking (thermal dehydrochlorination or "cracking") of 1,2-dichloroethane (EDC), wherein EDC splits, at temperatures of about 450 to 600 °C, into VCM and hydrogen chloride. The obtained VCM and the hydrogen chloride are subsequently separated in respective distillation units, after which the hydrogen chloride is recycled, for instance for EDC production. The cracking of EDC is incomplete and yields a process stream comprising a mixture of the main products mentioned above, along with uncracked EDC and by-products of various chemicals. The uncracked EDC can be recycled and send back for thermal cracking. However, the by-products, if circulated back to the thermal cracking process, are known to have severe adverse effects on the reaction kinetics, such as to increase coke formation and, consequently, to increase maintenance costs. This leads to the problem of effectively separating the uncracked EDC from the by-products.

[0003] The by-products comprise low-boiling compounds, such as chloroprene and benzene, and high-boiling compounds. Some of these low-boiling compounds can be removed by distillation, whilst others, especially benzene, have very close boiling temperatures to EDC; to avoid their difficult and energy-consuming separation, these low-boiling compounds have to be converted to high-boiling compounds, which then can easily be removed through distillation.

[0004] Generally, these low-boiling compounds can be converted to high-boiling compounds by chlorination. In this respect, low-boiling compounds refer to compounds having a boiling temperature of below the boiling temperature of EDC, which is around 84 °C (at 1.01325 bar), while high-boiling compounds refer to compounds having a boiling temperature of above the boiling temperature of EDC. Chloroprene can be converted to high-boiling chlorobutane by thermal chlorination, whilst benzene requires a catalyst for its chlorination. However, excess chlorination of benzene needs to be avoided to reduce the cost of the chlorination process, but also because the presence of hexachlorbenzene interferes with the subsequent distillation step due to its sublimation. Homogenous catalysts, such as iron(III) chloride, which can be produced in situ by chlorination of iron fillers, are usually employed since the cracking of EDC produces coke that can cause a blocking and deactivation of heterogeneous catalysts. When using iron(III) chloride, only a partial flow of the process stream can be chlorinated, as otherwise too much iron would be introduced into the process. Hence, following the thermal chlorination, whereby chloroprene is converted to chlorobutane, a partial flow of the product mixture comprising uncracked EDC, benzene and remaining unconverted chloroprene is catalytically chlorinated using iron(III) chloride, whereby benzene is converted to chlorobenzene. These high-boiling compounds are separated from the uncracked EDC, which then can be used for further thermal cracking.

[0005] It has been found that the use of homogenous iron catalysts, in particular of iron(III) chloride, causes serious problems downstream of the chlorination. In an undesired reaction, iron(III) chloride leads to chlorination of EDC to trichlorethene (TCE). Further, iron catalyses the cracking of EDC to coke, leading to blocking of reactors and columns in subsequent process steps. Iron is also flushed out and accumulates downstream, additionally leading to the blocking of reactors and columns.

[0006] In US 5,068,475 A, a process is described for chlorinating benzene in the presence of an iron catalyst, being finely divided iron turnings, iron baskets or steel wool, that fills the entire reaction space and produces minimal amount of active iron(III) chlorine.

[0007] In DE 40 33 047 A1, a process is described wherein, following the separation of VCM and hydrogen chloride, the process stream is first divided into a process stream (I), containing no high-boiling compounds, and a process stream (II), containing high-boiling compounds. The process stream (I) is treated with chorine in the presence of metallic iron. Alternatively, the process stream (II) can also be chlorinated. Both process streams are then reunited and EDC is recovered. In DE 41 39 632 A1, the process described in DE 40 33 047 A1 is modified by treating the reunited process streams once more with chlorine before EDC is recovered. In DE 41 29 391 A1, the process described in DE 40 33 047 A1 is further modified as it has been found that the used iron catalyst still leads to severe downstream problems by causing for instance deposits on heat exchangers. To circumvent the use of metallic iron, a γ-aluminium(oxide) catalyst, preferably as moulding such as spheres, cylinders or rings, is employed for chlorinating the process stream (I).

[0008] The prior art processes known to us have, however, the disadvantage that the catalytical chlorination is not selective enough, producing unwanted chlorinated products such as hexachlorbenzene and TCE.

[0009] Therefore, it is an object of this invention to provide a new or improved process of removing by-products from a vinyl chloride comprising process stream from a 1,2-dichloroethane thermal cracking process.

[0010] This object is solved by the present invention, namely a process of removing by-products from a vinyl chloride comprising process stream from a 1,2-dichloroethane thermal cracking process comprising the steps of: (a) providing a starting material comprising 1,2-dichloroethane; (b) thermally cracking 1,2-dichloroethane by heating the starting material to obtain a product mixture comprising vinyl chloride, hydrogen chloride, uncracked 1,2-dichloroethane and by-products; (c) separating the hydrogen chloride and separating the vinyl chloride from the product mixture thereby obtaining a process stream comprising uncracked 1,2-dichloroethane and by-products; (d) chlorinating the obtained process stream by adding liquid and / or gaseous chlorine to the process stream in the presence of a heterogeneous catalyst, thereby obtaining a process stream comprising the uncracked 1,2-dichloroethane, chlorinated by-products and, optionally, still by-products from step c); (e) recovering the uncracked 1,2-dichloroethane from the process stream by separating the chlorinated by-products; (f) optionally regenerating the catalyst through backflushing; and wherein the heterogeneous catalyst is an iron-aluminium(oxide)-catalyst with a formula FeaAlbOc.

[0011] It has been found that using a heterogeneous iron-aluminium(oxide)-catalyst with a formula Fe a Al b O c has the advantage of converting chloroprene and benzene in a single process step. This allows for a considerable reduction of plant size and complexity. Further, chloroprene and benzene are converted in a highly selective reaction, hence benzene is not or scarcely converted to unwanted hexachlorbenzene. Even more, the loss of uncracked EDC through unwanted chlorination is minimized, and, as a consequence, less coke is formed. Another advantage of the heterogeneous iron-aluminium(oxide)-catalyst is that it is not flushed out compared to a homogeneous catalyst; and, thus, less iron accumulates in the downstream processes, leading to an increase runtime of the downstream reactors and columns and reduced maintenance costs.

[0012] The iron-aluminium(oxide)-catalyst with the formula Fe a Al b O c has preferably the formula Fe (1-5) Al (1-25) O (1-30) .

[0013] The starting material EDC of step (a) is optionally provided by direct chlorination and / or oxychorination, both reactions being exothermic. Direct chlorination is conducted at a temperature of, for example, 40 to 130 °C at 2.6 bar, preferably 100 °C at 2.6 bar, wherein chlorine and ethylene are catalytically converted:         C 2 H 4 + Cl 2 → C 2 H 4 Cl 2

[0014] Direct chlorination has the advantage of producing, in a single reactor, EDC that can be used directly for step (b) thermally cracking the EDC, without any further purification necessary. Alternatively, oxychorination can be used to produce EDC in a reaction, at a temperature of, for example, above 200 °C at 2.8 bar, preferably 230 °C at 2.8 bar, wherein ethylene, hydrogen chloride and oxygen are catalytically converted:         C 2 H 4 + 2HCI + ½ O 2 → C 2 H 4 Cl 2 + H 2 O

[0015] EDC produced in this way must be purified, for instance by distillation, before being used for step (b) of the process. EDC can be providing by direct chlorination, oxychlorination, or a combination thereof, or in any other suitable way. Preferably, the starting material in step (a) comprises 70 wt.% or more, 80 wt.% or more or 90 wt.% or more EDC. Further preferably, the starting material consists of EDC.

[0016] In the next process step (b), EDC is thermally cracked, in an endothermic reaction, by a temperature ranging from, for example, 450 to 650 °C, preferably 450 to 600 °C, further preferably 450 to 550 °C, preferably 480 °C. Thereby a product mixture is obtained comprising vinyl chloride and hydrogen chloride:         C 2 H 4 Cl 2 → C 2 H 3 Cl + HCl

[0017] The cracking reaction in step (b) is incomplete, having a conversion rate of, for example, 20 to 99 wt.%, preferably 40 to 70 wt.%, further preferably 50 to 60 wt.% based on the total throughput of EDC. The product mixture obtained in step (b) further comprises uncracked 1,2-dichloroethane and by-products.

[0018] The by-products of the obtained product mixture of step (b) preferably comprise one or more hydrocarbons selected from the list comprising benzene, chloroprene and other hydrocarbons.

[0019] In step (c), the vinyl chloride and the hydrogen chloride are separated from the product mixture, preferably through distillation. Thereafter, hydrogen chloride may be recycled and, for instance, fed to the oxychlorination reaction for EDC production, while the vinyl chloride is optionally stored.

[0020] Following the removal of vinyl chloride and hydrogen chloride, a process stream is obtained that comprises the uncracked 1,2-dichloroethane and the by-products, wherein the by-products preferably comprise one or more hydrocarbons selected from the list comprising benzene, chloroprene and other hydrocarbons.

[0021] In step (d), this process stream is chlorinated by adding liquid and / or gaseous chlorine in the presence of a heterogeneous catalyst being an iron-aluminium(oxide)-catalyst with a formula Fe a Al b O c . Thereby, a process stream comprising the uncracked 1,2-dichloroethane, chlorinated by-products and, optionally, still by-products from step (c) is obtained.

[0022] In an embodiment, in step (d) the chlorinated by-products comprise high-boiling chlorinated by-product, having a boiling temperature of at least 85°C, such as high-boiling chlorobenzene and high-boiling chlorobutane.

[0023] Surprisingly, by employing the iron-aluminium(oxide)-catalyst with the formula Fe a Al b O c , it is possible to chlorinate by-products in a single step, without the need to divide the process stream in a partial stream. The required plant size and complexity is therefore reduced. Moreover, this chlorination step is shown to be highly selective, resulting in chlorinated by-products, such that EDC is not further chlorinated in an undesired side reaction and such that no hexachlorbenzene is generated. Preferably, EDC is not converted to 1,1,2-trichloroethene. Preferably, benzene is not converted to hexachlorbenzene. In consequence, less coke is produced and runtime between decoking and maintenance intervals can be increased.

[0024] Furthermore, the iron-aluminium(oxide)-catalyst with a formula Fe a Al b O c is preferably not flushed out and does not accumulate in downstream reactors or columns, advantageously leading to even longer runtimes and lower maintenance costs.

[0025] The iron-aluminium(oxide)-catalyst can be used preferably in a catalytic fixed bed reactor, but may also be used in other suitable reactors.

[0026] A suitable temperature for carrying out the chlorination in step (d) is, for example, 20 to 100 °C, preferably 40 to 90 °C, further preferably 60 to 80 °C. A suitable pressure is, for example, 0.5 to 3 bar, preferably 0.5 to 2 bar.

[0027] A suitable amount of chlorine per kg EDC for carrying out the chlorination of step (d) is preferably 0.1 to 20 g, preferably 1.5 to 15 g, further preferably 2 to 4 g. In a preferred embodiment, in step (d) the chlorine is provided as a gaseous chlorine.

[0028] The benzene conversion rate to high-boiling chlorobutane is preferably 99%, further preferably 100 %.

[0029] Following the catalytic chlorination in step (d), the process stream contains below 2000 ppm, preferably below 1000 ppm, further preferably 500 ppm, low-boiling benzene and / or low-boiling chloroprene.

[0030] In the subsequent process step (e), the uncracked EDC is recovered by separating the chlorinated by-products.

[0031] In a preferred embodiment, in step (e) the uncracked EDC is recovered by separating the chlorinated by-products through distillation. Preferably, the chlorinated by-products comprise high-boiling chlorinated by-products, having a boiling temperature of at least 85°C.

[0032] In process step (f), the heterogeneous iron-aluminium(oxide)-catalyst with a formula Fe a Al b O c can optionally be regenerated through backflushing. This backflushing can be conducted by flushing the catalyst using a gaseous composition and / or a liquid, which do not react with the catalyst surface. In a preferred embodiment, the catalyst is backflushed one or more times with a flush-liquid / flush gas. The flush-liquid / flush gas can be a process stream and / or a liquid / gas comprising preferably chlorinated or non-chlorinated saturated hydrocarbons and / or chlorinated or non-chlorinated unsaturated hydrocarbons with / without additives. The backflushing is preferably conducted at a temperature of 20 to 150 °C, preferably 30 to 100 °C.

[0033] It is another object of the invention to provide the use of a heterogeneous iron-aluminium(oxide)-catalyst in the process described above. In particular, the use of a heterogeneous iron-aluminium(oxide)-catalyst for removing by-products from a vinyl chloride comprising process stream from a 1,2-dichloroethane thermal cracking process characterized in that the catalyst is an iron-aluminium(oxide)-catalyst with a formula Fe a Al b O c , preferably with the formula Fe (1-5) Al (1-25) O (1-30) .

[0034] Through this use the by-products are preferably chlorinated by adding liquid and / or gaseous chlorine to the process stream in the presence of the iron-aluminium(oxide)-catalyst according to the process and its preferred embodiments as described above.Examples Example 1: Chlorination using iron(III) chloride as catalyst

[0035] The catalytic tests were carried out according to the method defined under experimental procedures. The results of the screening are listed in table 1. Table 1: Chlorination using iron(III) chloride as catalystCatalyst [mol%]T [°C]Time [h]2-CP peak area [%]EDC peak area [%]BE peak area [%]TCE peak area [%]CB peak area [%]HCB peak area [%]Crude EDC0.398.081.050.040.070.00blank6030.084.980.4912.790.180.000.1 mol% FeCl 3 5030.096.230.000.860.041.650.1 mol% FeCl 3 6030.095.370.001.830.040.740.1 mol% FeCl 3 7030.093.480.064.200.051.270.1 mol% FeCl 3 8030.091.540.005.970.221.380.05 mol% FeCl 3 6030.091.670.005.850.300.130.01 mol% FeCl 3 6030.080.200.0816.920.760.00

[0036] Chloroprene (2-CP) was completely converted into higher chlorinated products in all experiments carried out. Benzene (BE) was almost completely reacted in most cases, but were also chlorinated to hexachlorobenzene (HCB) at high FeCl 3 concentrations (0.1 mol%). At low Fe concentrations, the chlorination of benzene resulted in the formation of chlorobenzene (CB) and dichlorobenzene. In all experiments, chlorination of dichloroethane (EDC) to trichloroethene (TCE) was also observed, possibly followed by the formation of still higher chlorinated products. The formation of TCE increased as expected as the temperature increased. But that the TCE formation increased already at low Fe concentrations and without using a catalyst was surprising. FeCl 3 was effective for the chlorination of benzene even at low concentrations (0.01 mol%). However, a high Fe concentration has a positive effect of suppressing the free-radical chlorination of EDC to TCE.Example 2: Chlorination using iron-aluminium(oxide) as catalyst

[0037] The catalytic tests were carried out according to the method defined under experimental procedures. The results of the screening are listed in table 2. Table 2: Chlorination using iron-aluminium(oxide) as catalystCatalyst [mg]T [°C]Time [h]X CP [%]X B [%]EDC peak area [%]BE peak area [%]TCE peak area [%]CB peak area [%]HCB peak area [%]500 mg Alumnia (46105)7011007297.550.300.660.660.00500 mg Fe a Al b O c 701100>9997.60<0.010.260.000.00250 mg Fe a Al b O c 701100>9998.12<0.010.120.370.00250 mg Fe a Al b O c 80110010097.940.000.140.440.00

[0038] A commercial γ-alumina (Alfa Aesar, 46105) with a BET surface area of 380 m 2< / g, a mean pore diameter of 4 nm and a pore volume of 0.5 ml / g was tested for comparison. The sample was crashed and sieved. The fraction of granules <100 µm was used for the experiments without any additional pre-treatment. With 0.50 g alumina, the benzene conversion was 72 % at 70°C and after 1 h, while the chloroprene was fully converted.

[0039] The best catalyst was the iron-aluminium(oxide)-catalyst containing 10 wt.% Fe with a surface area of 183 m 2< / g. The catalyst has a mean pore diameter of 10 nm and a pore volume of about 0.6 ml / g. With 500 and 250 mg of the catalyst, benzene was completely converted, mainly to 1,2- and 1,4-dichlorobenzene. An extra experiment using the same catalyst was done at 80°C, and benzene as fully converted as it is shown in table 2. The conversion (X) of benzene (B) and chloroprene (CP) were calculated based on the peak area % from the GC analysis.

[0040] In conclusion, the iron-aluminium(oxide) as catalyst is highly selective and active, whilst commercial γ-alumina is less active and iron(III) chloride is less selective.Experimental procedures Catalyst preparation

[0041] The iron-aluminium(oxide)-catalyst was synthesized using a commercial water dispersible alumina (Disperal P2, Sasol). First a dispersion of alumina was prepared by stirring 80 g of water with 20 g of the alumina source in a 200 ml beaker at room temperature (at 22°C). After 1 h stirring, 10 g of Triton X100 was added and stirred for another 30 minutes. The magnet was removed and then a solution of 13.5 g of Fe(NO 3 )3·9H 2 O in 25 g of water was added to the dispersion and homogenized using a spatula.

[0042] The formed brown gel was left to dry in air until a weight loss of 50 %. The paste was homogenized and shaped using a syringe of 2 mm opening diameter. Then this was left for drying at room temperature for two days. Then, it was dried overnight at 80 °C. The calcination was done inside a tubular furnace with a heating rate of 1 K / min under the flow of air (150 ml / min) up to 300 °C, and then a portion of this catalyst was calcined again at 800 °C for 3 h (heating rate 10 K / min). Finally, 10 wt.% of iron supported on aluminium(oxide) was yielded.GC-MS Analysis

[0043] For GC analyses, the conditions used for separation are listed in table 3. Both GC (Agilent 6890) and GC-MS (Agilent 6890) devices were used for the analysis using similar columns. The temperature program of GC started at 50 °C for 6 min, and then the temperature was increased by 20 K / min up to 250 °C (holding time 7 min); the total run time was 23 min. For GC-MS, the temperature program started with 40°C for 5 min and then the temperature was raised with 20 K / min to 160 °C (no holding time), followed by a temperature ramp of 45 K / min to 250 °C (holding time 17 min); the total run time was 30 min. In both cases, the pure sample was injected without any dilution. 1 µl of the product solution was injected into the GC and 0.2 µl was used for the GC-MS analysis. Table 3: Conditions of GC and GC / MS used for analysis of productsMethod Column name Detector Injector Column temperature program GCHPS (50 m x 0.32 mm x 0.52 µm)FID (280 °C)(250 °C)50 °C (6 min) (20 K / min) to 250 °C for (7 min) (20 K / min), total run time = 23 minGC-MCHPS (30 m x 0.25 mm x 0.25 µm)FID (320 °C), MS (230 °C)(260°C)40 °C (5 min) (20 K / min) to 160 °C (0 min) (45 K / min) to 250 °C (17 min), total run time = 30 min Procedure testing iron(III) chloride

[0044] The reactions were realized as follows: at first, an autoclave was tested for leakage at 2 bar argon pressure. Afterwards, the autoclave was flushed several times with Cl 2 gas up to 1.8 bar at room temperature (at 22 °C). Whenever the pressure dropped to 0.5 bar, the inlet valve was opened for pressurizing the autoclave with fresh Cl 2 gas. This procedure was repeated until the pressure was constant (that means that the solution was saturated with dissolved chlorine). Subsequently, heating and stirring (700 rpm) was started until the reaction temperature, i.e. 50 °C. 60 °C, 70 °C or 80 °C, was reached. If the pressure inside the autoclave was higher than 2 bars due to the increase of temperature, the outlet valve was opened to release the excess pressure and to keep the pressure constant during the whole experiment close to 2 bars. As a result, there might be some loss of the reactants upon releasing the excess pressure. The experiment was left with the above conditions for 3 h. With this procedure, a high amount of ca. 30 mmol chlorine at 2 bar was applied for 30 g of EDC containing 2 mmol benzene. The amount of catalyst used was 0.01 mol% (= 100 mg Fe / liter substrate), 0.05 mol% (= 500 mg Fe / liter substrate) or 0.1 mol% (= 1000 mg Fe / liter substrate).Procedure testing iron-aluminium(oxide)

[0045] The procedure testing iron-aluminium(oxide) was performed as described for the iron(III) chloride. However, a low amount of Cl 2 gas of ca. 5 mmol was fed in order to achieve an incomplete conversion of benzene, to render the catalyst activity more comparable. The reaction temperature was fixed at 70°C. At first, the autoclave was checked for leakage at 2 bar argon pressure. Then it was purged two times with argon. The argon pressure inside the autoclave was fully released and heating to 70°C under stirring (700 rpm) started. When the temperature was reached, the inlet valve for Cl 2 gas was opened (one full round) for 10 sec. Initially, the internal pressure reached 1.5 bar while filling and then it decreased to 1-1.3 bar after closing the valve as Cl 2 gas was partially dissolved. The duration of an experiment was 1 h. The autoclave cooled down and then the pressure was released and a sample was taken for analysis on GC and / or GC / MS. The injection of the product samples was carried out instantly.

Claims

1. A process of removing by-products from a vinyl chloride comprising process stream from a 1,2-dichloroethane thermal cracking process comprising the steps of: (a) providing a starting material comprising 1,2-dichloroethane; (b) thermally cracking 1,2-dichloroethane by heating the starting material to obtain a product mixture comprising vinyl chloride, hydrogen chloride, uncracked 1,2-dichloroethane and by-products; (c) separating the hydrogen chloride and separating the vinyl chloride from the product mixture thereby obtaining a process stream comprising uncracked 1,2-dichloroethane and by-products; (d) chlorinating the obtained process stream by adding liquid and / or gaseous chlorine to the process stream in the presence of a heterogeneous catalyst, thereby obtaining a process stream comprising the uncracked 1,2-dichloroethane, chlorinated by-products and, optionally, still by-products from step c); (e) recovering the uncracked 1,2-dichloroethane from the process stream by separating the chlorinated by-products; (f) optionally regenerating the catalyst through backflushing; and wherein the heterogeneous catalyst is an iron-aluminium(oxide)-catalyst with a formula FeaAlbOc.

2. The process of claim 1, wherein in step c) the vinyl chloride and the hydrogen chloride are separated through distillation.

3. The process of any of claim 1 or 2, wherein in step e) the uncracked 1,2-dichloroethane is recovered by separating the chlorinated by-products through distillation.

4. The process of any of claims 1 to 3, wherein in step d) the chlorinated by-products comprise high boiling chlorinated by-product, having a boiling temperature of at least 85 °C.

5. The process of any of claims 1 to 4, wherein the by-products comprise one or more hydrocarbons selected from the list comprising benzene, chloroprene and other hydrocarbons.

6. The process of any of claims 1 to 5, wherein the iron-aluminium(oxide)-catalyst is a catalytic fixed bed reactor.

7. The process of any of claims 1 to 6, wherein the starting material in step a) comprises 70 wt.% or more 1,2-dichloroethane, preferably 80 wt.% or more 1,2-dichloroethane, further preferably 90 wt.% or more 1,2-dichloroethane.

8. The process of any of claims 1 to 7, wherein in step b) 1,2-dichloroethane is thermally cracked, in an endothermic reaction, by a temperature ranging from 450 to 650 °C, preferably 450 to 600 °C, further preferably 450 to 550 °C.

9. The process of any of claims 1 to 8, wherein the cracking reaction in step b) is incomplete, having a conversion rate of 20 to 99 % based on total throughput of 1,2-dichloroethane, preferably 50 to 60 % based on total throughput of 1,2-dichloroethane.

10. The process of any of claims 1 to 9, wherein in step d) the temperature for carrying out the chlorination is 20 to 100 °C, preferably 40 to 90 °C, further preferably 60 to 80 °C.

11. The process of any of claims 1 to 10, wherein in step d) the pressure for carrying out the chlorination is 0.5 to 3 bar, preferably 0.5 to 2 bar.

12. The process of any of claims 1 to 11, wherein in step d) the amount of chlorine per kg EDC for carrying out the chlorination is 0.1 to 20 g, preferably 1.5 to 15 g, further preferably 2 to 4 g.

13. The process of any of claims 1 to 12, wherein in step d) the chlorine is provided as a gaseous chlorine.

14. Use of a heterogeneous catalyst in a process of removing by-products from a vinyl chloride comprising process stream from a 1,2-dichloroethane thermal cracking process characterized in that the catalyst is an iron-aluminium(oxide)-catalyst with a formula FeaAlbOc.

15. The use of claim 14, wherein the by-products are chlorinated by adding liquid and / or gaseous chlorine to the process stream in the presence of the iron-aluminium(oxide)-catalyst.