SU121893A1 - Turpentine preparation method - Google Patents

Description

The isolation of marketable turpentine from sulphate turpentine raw material presents known difficulties, due to the presence of a number of hardly separable, malodorous sulfur compounds in it. Therefore, for the treatment of sulphate turpentine, either distillation plants or plants for the preliminary removal of the bulk of sulfur compounds using the "boiling" method are used. At the same time, the yield of return turpentine raw does not exceed 40–45% in a number of cases, which markedly reduces the performance of the respective installations.

Currently, the main consumer of sulfate turpentine is enterprises producing technical terpineol. However, the content of a-pinene, necessary for the production of terpineol, in the manufactured commercial sulphate turpentine is not high enough.

The bottoms obtained during the distillation of sulphate turpentine with steam and containing terpene alcohols, have hitherto been discharged into the sewage system. True, it is possible to use these residues as a flotation reagent - foaming agent in the enrichment of coal, but they are ineffective due to the low content of terpene alcohols, non-standard and unpleasant smell.

A method is proposed for producing turpentine by separating it from sulphate raw turpentine, for example, by steam distillation, which means that the raw turpentine raw is oxidized with air before distillation. This pretreatment makes it possible to obtain turpentine with a new content of α-pinene and a bottom residue containing at least 60% terpene alcohols and suitable as a flotation reagent.

Example. 1240 oz of sulphate raw turpentine comes through a measuring device 1 (see the diagram) into the distillation cube 2, with a capacity of 1.5 I1, equipped with a bubbler for supplying air and direct steam, with coils for supplying steam

No. 121893-2 -

and cold water, a spray bar 3 and a refrigerator 4. Air is supplied to the cube in an amount of 80-100 mHh and the temperature is raised to 85 ° for 30-40 minutes. After that, using steam heating and water cooling (the oxidation reaction is exothermic), the temperature of the mass is maintained within 95-105 ° until 30-35% content of terpenes of alcohols is reached, which takes 4-5 hours.

The fumes of sulphate turpentine released during the oxidation process are condensed in the refrigerator 4, and the condensate enters through the florentin 5 into the tanks for the sulphate hydrodietary raw material. Air containing volatile sulfur compounds is emitted into the atmosphere.

Upon reaching the required content of terpene alcohols, the air is turned off and hot steam is released into the bubbler (2 atm); at the same time steam pressure of 2 ata is fed into the coils, heating the cube Distillate enters florentin 6, from which commercial turpentine with a high content of α-pinene is selected. The distillation is carried out until a refractive index of no more than 1.471 is reached and the turpentine appears to have a light yellowness. Then the steam is turned off and the contents of the cube (which is flotation oil) are discharged into the barrels. Just get 180-220 l of return turpentine raw, 600-650 l of commercial turpentine, containing more than 70% a-pinene and not more than 0.03% sulfur, and 300-325 l of oil, containing at least 60% of terpene alcohols.

Subject invention

Claims (2)

1. A method of producing turpentine by separating it from sulphate turpentine raw, for example, steam distillation, characterized in that, in order to increase the content of α-pinene and increase the content of terpene alcohols in the resulting bottoms, sulphate turpentine is pre-oxidized Yut air. 2. Application of the vat residue, obtained according to claim 1 as a flotation reagent.