PROCESS FOR THE PREPARATION OF VINYL CHLORIDE

Abstract

A process for the production of vinyl chloride comprises the step of passing a feed stream comprising ethylene dichloride (EDC) over a catalyst system comprising a dehydrochlorination catalyst and a hydrochlorination catalyst at a temperature, which may be in the range 150-350 C., sufficient to effect dehydrochlorination of the ethylene dichloride to produce vinyl chloride.

Claims

1. A process for the production of vinyl chloride, comprising: passing a feed stream comprising ethylene dichloride over a catalyst system comprising a dehydrochlorination catalyst and a hydrochlorination catalyst at a reaction temperature and reaction pressure sufficient to effect dehydrochlorination of the ethylene dichloride to produce vinyl chloride.

2. The process according to claim 1, wherein the feed stream comprising ethylene dichloride comprises at least 10% by weight of ethylene dichloride, more preferably at least 30% by weight of ethylene dichloride, especially at least 50% by weight of ethylene dichloride.

3. The process according to claim 2, wherein the feed stream comprising ethylene dichloride comprises at least 80% by weight of ethylene dichloride.

4. The process according to claim 1, wherein the reaction temperature is in the range in the range of from 150 C. to 350 C.

5. The process according to claim 1, wherein the reaction pressure is in the range of from 0 to 55 bar G.

6. The process according to claim 1, wherein acetylene is present in the feed stream.

7. The process according to claim 1, wherein the dehydrochlorination catalyst comprises a supported noble metal catalyst.

8. The process according to claim 7, wherein the dehydrochlorination catalyst comprises at least one of platinum, palladium, ruthenium, or rhodium.

9. The process according to claim 1, wherein the hydrochlorination catalyst comprises at least one metal selected from the group consisting of gold, mercury, palladium, silver, ruthenium, iridium, platinum, rhodium, copper, bismuth, tin, zirconium, antimony, and lead or a compound thereof.

10. The process according to claim 9, wherein the hydrochlorination catalyst comprises gold or a compound of gold on a catalyst support.

11. The process according to claim 1, wherein the hydrochlorination catalyst comprises a non-metallic catalyst.

12. The process according to claim 1, wherein the dehydrochlorination and hydrochlorination catalysts are present in separate reaction vessels.

13. The process according to claim 1, wherein the dehydrochlorination and hydrochlorination catalysts are present in the same vessel.

14. The process according to claim 13, wherein the catalyst system comprises particles of a dehydrochlorination catalyst and separate particles of a hydrochlorination catalyst present in the same reaction vessel.

15. The process according to claim 14, wherein the separate particles of dehydrochlorination and hydrochlorination catalysts are arranged in different regions of the reaction vessel.

16. The process according to claim 14, wherein the separate particles of dehydrochlorination and hydrochlorination catalysts are mixed together to form a mixed catalyst bed.

17. The process according to claim 13, wherein the dehydrochlorination and hydrochlorination catalysts are present in the same catalyst particle.

18. The process according to claim 17, wherein the hydrochlorination catalyst and the dehydrochlorination catalyst are supported on the same catalyst support.

19. The process according to claim 18, wherein the dehydrochlorination catalyst comprises a noble metal and said hydrochlorination catalyst comprises a compound containing boron, nitrogen, oxygen, phosphorus or sulphur.

Description

EXAMPLE 1 (Comparative)

[0029] 30 g of a commercial 0.8% palladium on carbon catalyst, from Johnson Matthey, (Pd on 3 mm extruded carbon support particles) was loaded into a 2 cm diameter glass tube, to give a bed length of about 40 cm. The tube was contained within a horizontal tube furnace. A flow of 31 ml/min of nitrogen was then initiated through the bed. The temperature of the bed was then raised to 300 C., and 1,2-dichloroethane (ethylene dichloride, EDC) was introduced into the nitrogen stream. This was achieved by passing the nitrogen stream through a metal coil heated to 120 C., EDC liquid being pumped into the coil via a GLC pump, at a flow of 0.25 ml/min. The reactor effluent was analysed by gas chromatography at different times during the reaction and the results (mass % in the effluent stream) are shown in Table 1. It can be seen that the EDC has been dehydrochlorinated to give approximately 50% VCM in the product stream, and about 0.6% acetylene. After about 400 minutes, the EDC flow was stopped, and the catalyst bed cooled under nitrogen.

TABLE-US-00001 TABLE 1 Time (minutes) 124 218 415 VCM concentration (%) 50.89 51.97 50.54 EDC Concentration (%) 48.54 47.50 48.91 Acetylene concentration (%) 0.57 0.53 0.55

EXAMPLE 2

[0030] 5 g of the Pd/C catalyst nearest the outlet of the catalyst bed as described in Example 1 were removed, and replaced by 5 g of a commercial 0.6% Au/C catalyst (from Johnson Matthey). The reactor tube loaded with the layered bed of catalyst was then purged with nitrogen, heated to 300 C., and EDC introduced as described above. The results (mass % in the effluent stream) are shown in Table 2. It can be seen that there is a significant reduction in the acetylene concentration to less than 0.2%, compared with Example 1, and a corresponding decrease in EDC and increase in VCM.

TABLE-US-00002 TABLE 2 Time (minutes) 38 60 257 303 VCM concentration (%) 53.23 54.1 52.76 52.29 EDC Concentration (%) 46.59 45.72 47.07 47.54 Acetylene concentration (%) 0.18 0.18 0.17 0.17