METHOD FOR REMOVING DIENES FROM A MATERIAL STREAM CONTAINING C3 TO C5 HYDROCARBONS BY SELECTIVE HYDROGENATION

Abstract

The invention relates to a process for removing dienes from a material stream comprising C.sub.3 to C.sub.5 hydrocarbons by selective hydrogenation at a specified reaction pressure and a specified reaction temperature in the presence of a hydrogenation catalyst, wherein the reaction pressure and the reaction temperature at the reactor inlet are regulated such that the reaction pressure at the reactor inlet does not deviate by more than 0.01 bar from the specified reaction pressure and the reaction temperature at the reactor inlet does not deviate by more than 0.1° C. from the specified reaction temperature and the proportion of hydrogen supplied to the selective hydrogenation is in the range from 2 to 20 moles per mole of diene present in the material stream comprising C.sub.3 to C.sub.5 hydrocarbons.

Claims

1.-13. (canceled)

14. A process for removing dienes from a material stream comprising C.sub.3 to C.sub.5 hydrocarbons by selective hydrogenation at a specified reaction pressure and a specified reaction temperature in the presence of a hydrogenation catalyst, wherein the reaction pressure and the reaction temperature at the reactor inlet are regulated such that the reaction pressure at the reactor inlet does not deviate by more than 0.01 bar from the specified reaction pressure and the reaction temperature at the reactor inlet does not deviate by more than 0.1° C. from the specified reaction temperature and the proportion of hydrogen supplied to the selective hydrogenation is in the range from 2 to 20 moles per mole of diene present in the material stream comprising C.sub.3 to C.sub.5 hydrocarbons.

15. A process for removing dienes from a material stream comprising C.sub.3 to C.sub.5 hydrocarbons by selective hydrogenation, comprising the following steps: (a) vaporizing part of a material stream comprising liquid C.sub.3 to C.sub.5 hydrocarbons, mixing a gaseous material stream comprising C.sub.3 to C.sub.5 hydrocarbons and a liquid one, or condensing part of a material stream comprising gaseous C.sub.3 to C.sub.5 hydrocarbons, with the result that 2 to 50 mol % of the material stream comprising C.sub.3 to C.sub.5 hydrocarbons is present in the gas phase after vaporization, (b) supplying the partially vaporized material stream comprising C.sub.3 to C.sub.5 hydrocarbons to a reaction step comprising a hydrogenation catalyst and adding hydrogen in a proportion of 2 to 20 moles per mole of diene present in the material stream comprising C.sub.3 to C.sub.5 hydrocarbons, wherein the hydrogen may be added together with the partially vaporized material stream comprising C.sub.3 to C.sub.5 hydrocarbons or via a separate addition point, (c) separating the gas phase and liquid phase and withdrawing the liquid phase as a product stream.

16. The process according to claim 15, wherein an inert gas is added to adjust the amount of the vaporized part of the material stream comprising C.sub.3 to C.sub.5 hydrocarbons.

17. The process according to claim 16, wherein the inert gas is selected from the group consisting of nitrogen, methane, carbon dioxide, noble gases, and mixtures thereof.

18. The process according to claim 15, wherein steps (a) and (b) are carried out in an apparatus having a vaporization part and a reaction part holding the catalyst bed comprising the hydrogenation catalyst, wherein the design of the vaporization part is such that, before entry into the catalyst bed, the material stream comprising C.sub.3 to C.sub.5 hydrocarbons is vaporized to an extent that 2 to 50 mol % of the material stream comprising C.sub.3 to C.sub.5 hydrocarbons is present in the gas phase.

19. The process according to claim 15, wherein vaporization of part of the material stream comprising C.sub.3 to C.sub.5 hydrocarbons in step (a) is done by splitting the material stream comprising C.sub.3 to C.sub.5 hydrocarbons into two streams, completely vaporizing one of the two streams, and mixing this again with the second of the two streams after vaporization.

20. The process according to claim 15, wherein the material stream comprising C.sub.3 to C.sub.5 hydrocarbons is heated at elevated pressure and then depressurized in the reactor, which is operated at lower pressure.

21. The process according to claim 15, wherein the reaction step comprises a separate reactor and the vaporization in step (a) is controlled such that, on entry of the material stream comprising C.sub.3 to C.sub.5 hydrocarbons into the reactor, a further part vaporizes, with the result that, after entry of the material stream comprising C.sub.3 to C.sub.5 hydrocarbons into the reactor, 2 to 50 mol % of the material stream comprising C.sub.3 to C.sub.5 hydrocarbons is present in the gas phase.

22. The process according to claim 14, wherein the material stream comprising C.sub.3 to C.sub.5 hydrocarbons comprises not less than 99% by weight of C.sub.3 to C.sub.5 alkenes having precisely one double bond.

23. The process according to claim 14, wherein the product stream comprises not less than 99% by weight of C.sub.3 to C.sub.5 alkenes having precisely one double bond.

24. The process according to claim 22, wherein the C.sub.3 to C.sub.5 alkene having precisely one double bond is but-1-ene.

25. The process according to claim 14, wherein the diene content in the material stream comprising C.sub.3 to C.sub.5 hydrocarbons is less than 1000 ppm.

26. The process according to claim 15, wherein the gas phase obtained in step (c) is cooled, resulting in condensation of the C.sub.3 to C.sub.5 alkenes having precisely one double bond that are present in the gas phase and withdrawal of the condensed C.sub.3 to C.sub.5 alkenes having precisely one double bond as product.

Description

EXAMPLES

[0062] 2.5 kg/h of a material stream having a but-1-ene content of 99.84 and containing 121 ppm and 182 ppm of butadiene was hydrogenated in a trickle-bed reactor holding 200 ml of a palladium/silver catalyst, obtainable for example as H0-43 from BASF SE, as hydrogenation catalyst. Before admission of the material stream to the trickle-bed reactor, the material stream was heated in an electrically operated evaporator and partially vaporized. The heat supply was adjusted such that about 15% by weight of the material stream used was present in the gas phase after vaporization.

[0063] The reaction was carried out such that the temperature at the reactor inlet was 40° C. or alternatively 30° C. The temperature at the reactor inlet was adjusted via the pressure at the reactor outlet.

[0064] The tables below show the composition of the product stream obtained in the selective hydrogenation, the proportion of hydrogen supplied, the temperature at the reactor inlet, and the pressure at the reactor outlet. Table 1 lists the process parameters for the individual examples and table 2 shows the respective composition of the product stream withdrawn from the trickle-bed reactor.

[0065] For examples 1 and 2, a feed stream was used that comprised 99.84% by weight of but-1-ene, 370 ppm of n-butane, 92 ppm of trans-but-2-ene, 112 ppm of cis-but-2-ene, and 121 ppm of butadiene; for examples 3, 4, and 5, a feed stream comprising 99.84% by weight of but-1-ene, 358 ppm of n-butane, 95 ppm of trans-but-2-ene, 112 ppm of cis-but-2-ene, and 182 ppm of butadiene was used. The remainder is mainly C.sub.3 and C.sub.5 hydrocarbons present as impurities and also other common impurities that arise in butene production.

TABLE-US-00001 TABLE 1 Process parameters Proportion in the gas phase in Ratio H.sub.2/ Pressure at Temperature at feed stream butadiene reactor outlet reactor inlet [wt.-%] [mol/mol] [bar(g)] [° C.] Example 1 15 4.7 3.17 40 Example 2 14 4.7 2.20 30 Example 3 15 2.1 3.17 40 Example 4 15 5.0 3.17 40 Example 5 15 3.1 3.17 40

TABLE-US-00002 TABLE 2 Composition of the product stream trans-But- cis-But- But-1-ene n-Butane 2-ene 2-ene Butadiene [wt.-%] [ppm] [ppm] [ppm] [ppm] Example 1 99.73 441 705 668  2 Example 2 99.81 391 242 252 65 Example 3 99.78 435 435 362 30 Example 4 99.55 656 1524 1421 not detectable Example 5 99.78 396 473 435 10

[0066] The examples show clearly that, by adjusting the proportion in the gas phase, it is possible to carry out a selective hydrogenation in which the butadiene reacts through hydrogenation. The proportion of but-1-ene can moreover be seen to decrease only slightly. The largest decrease in the but-1-ene content is seen when the hydrogen supply is increased. However, even here the but-1-ene content falls by only 0.29%, resulting in a 0.3% decrease in the material stream. On lowering the hydrogen proportion, a satisfactory decrease in the butadiene content can still be observed, alongside an even smaller decrease in the but-1-ene content.

[0067] A satisfactory product stream was obtained for a required specification for but-1-ene of 99.5% by weight.