SU1634700A1 - Process for producing hydrogenated fat - Google Patents

Abstract

The invention relates to the chemical industry and can be used in the catalytic hydrogenation of vegetable oils. The aim of the invention is to intensify the process and reduce the specific consumption of hydrogen, which is achieved due to the fact that hydrogenation is carried out at a stepwise decreasing pressure of hydrogen from 0.35 ML in the first reactor to 0.20 MPa in the latter , tarey consistently. 1 tab.

Description

The invention relates to the oil and fat industry and can be used in the catalytic hydrogenation of vegetable oils.

The goal is to intensify the hydrogenation process and reduce the specific consumption of hydrogen.

Vegetable oils are hydrogenated on a suspended nickel-Knoelguar catalyst at 190-230 ° C in a continuous battery from three reactors. In this case, the hydrogen pressure decreases stepwise in reactors from 0.35 MPa in the first reactor to 0.20 MPa in the latter, and it is fed first to the first reactor and then sequentially sent through the second and third reactors and removed for purification only from the third reactor. .

The method is illustrated by an example of the hydrogenation of sunflower oil. The parameters of the hydrogenation process and the results of the comparison with the known hydrogenation method are given in the table.

As can be seen from the table, the selectivity of the process according to the known and proposed methods is high and equal to 0.98 (for glycerols linoleic

acid).

The use of the proposed method of hydrogenation of vegetable oils in comparison with the known method improves battery performance from 6.0 to 8.5 t / h and reduces the specific consumption of hydrogen from 181.67 to

67.05 nm / ton fat,

As a justification for the use of variable pressure from 0.35 MPa in the first reactor to 0.20 MPa in the latter and the proposed method of hydrogen supply, we note the following.

Since an undesirable monone reaction is saturated with in x acids saturated to saturate with increasing pressure of hydrogen,

4 J

process, the higher the hydrogen pressure, the lower the selectivity. Moreover, for each type of catalyst (copper, nickel, platinum) there is such an optimal value of hydrogen pressure, after which the selectivity of the process sharply decreases. This is due to the different hydrogenating activity of the catalysts. For the nickel catalyst used, the optimum hydrogen pressure is 0.35 MPa. Above this value, the selectivity of the process drops sharply. Therefore, the optimum working pressure of hydrogen in the autoclaves used today is 0.35 MPao. At pressures above this optimum value, the products obtained contain an increased amount of stearic acid, which reduces their nutritional value.

On the other hand, when the pressure of hydrogen increases, the capacity of the hydrogenation plant increases. At the same time, the linear nature of the dependence of the plant performance on hydrogen pressure is observed after a value of 0.20 MPa. Below this value, the plant capacity is not increased enough. no stability effect is achieved.

Thus, hydrogenation at a variable hydrogen pressure of 0.35 MPa in the first reactor (autoclave

,

ten

15

20

25

thirty

35

be) to 0.20 MPa in the latter and with the successive transfer of hydrogen from the autoclave to the autoclave ensures an increase in the productivity of the installation while maintaining the high selectivity of the process, as well as reducing the specific consumption of hydrogen.

The decrease in the specific consumption of hydrogen can be explained by the fact that with increasing pressure of hydrogen its solubility and mass transfer to the catalyst surface increase, and consequently, it is used more efficiently in the process, moreover, when the hydrogen is fed in succession through all the battery reactors, reactor in the next.

Claims (1)

Invention Formula A method for producing a fat gun, including hydrogenating vegetable oils in a reactor battery on a suspended catalyst at a temperature of 190-230 ° C and supplying hydrogen under pressure, characterized in that, in order to intensify the process and reduce the specific consumption of hydrogen, hydrogenation is carried out at a stepwise decreasing pressure of hydrogen from 0.35 MPa in the first reactor to 0.20 MPa in the latter, with the hydrogen being directed through all the battery reactors in series. Battery capacity, t / h Hydrogenation duration. Hydrogen supply method Hydrogen pressure, MPa in the first reactor in the second reactor in the third reactor Consumption of hydrogen, nm} / h in the first reactor in the second reactor in the Third reactor Total hydrogen consumption battery, nm3 / h 6.0 3.0 arally in each of the reactions 0.20 0.20 0.20 530 320 240 10fO 8.5 2.1 Sequentially through reactors 0.35 0.25 0.20 570 315 160 570 Hydrogenation Conditions Famous Item I Offer Specific hydrogen consumption nm / ton fat181.67 67.06 The index of the selectivity of the process for glycerol linoleic acid 0,980,98 Melomas melting point, ° С32,232.8 Salomas hardness, g / cm 270280 1634701.6 Table continuation The way to get salomas Subject We offer