CS254206B1 - Liquid Phase Chlorination Reactor - Google Patents

Abstract

The solution relates to a reactor for chlorination of hydrocarbons in the liquid phase without forced circulation of the reaction product. The reactor is formed by a continuous vessel, in the arms of which, where the height:diameter ratio is 6 to 10, there are tube systems separating the reaction mixture from the cooling medium, while the feed of the input raw materials is located below the lower edge of the tube system, preferably located coaxially with the lower part of the continuous vessel, and the arms of the continuous vessel above the tube system are interconnected and at least one arm is connected to the exhaust gas and the overflow for the product is located with the lower edge above the upper level of the connection of the arms.

Description

The solution relates to a reactor for the chlorination of liquid hydrocarbons without forced circulation of the reaction product.

The reactor is a continuous vessel in which arms, where the height-to-diameter ratio is 6 to 10, are tubular systems separating the reaction mixture from the cooling medium, wherein the feedstock feed is located below the lower edge of the tubular system, preferably located coincident with the lower portion of the continuous the vessels and the arms of the continuous vessel above the tubular system are interconnected and at least one arm is connected to the off-gas and the overflow for the product is situated at the lower edge above the upper level of arm connection. 254206 254206

The present invention relates to a reactor for chlorination of unsaturated organic compounds in a liquid phase without forced circulation of the reaction product.

In the industrial production of chlorinated hydrocarbons, tower-type reactors are used without filler or Rashig's iron rings are used as reactor fillers. iron spheres in order to better distribute the released heat of reaction into the entire reactor space, which is also used by forced circulation by the pump is a heat exchanger for isothermal chlorination conduction. A disadvantage of the process is the energy consumption for forced circulation of a considerable amount of the reaction product and the possibility of a local increase in the reaction temperature.

The drawbacks of the hydrocarbon chlorination reactor in the forced circulation liquid phase are eliminated by the reactor of the present invention, wherein the liquid phase reactor is a continuous vessel in which arms, where the height to diameter ratio is 6 to 10, are tubular systems separating the reaction mixture from the refrigerant media, wherein the feedstock feed is located below the lower edge of the tubular system, preferably positioned coaxially with the lower portion of the continuous vessel, and the arms of the continuous vessel above the tubular system are interconnected and at least one arm is connected to the offflow and the overflow for the product is located at the lower edge above upper level by shoulder-to-shoulder.

The main advantage of the liquid phase chlorination reactor is that the circulation of the product in the arms of a continuous vessel with tube-like systems is guaranteed by changing the density of the reaction product at the top and bottom of the continuous vessels without forced circulation, thereby saving energy to drive the circulation pump. Another advantage of the reactor according to the invention is that part of the reaction space is formed by a tube-like system with very good heat transfer, where there is practically no local increase in the reaction temperature.

The following examples illustrate the possibilities of application of the invention. Example 1

Liquid Phase Chlorination Laboratory Iron Reactor Built as a Continuous Container where the shoulder diameter was 125 mm and their height 821 mm, representing a height / diameter ratio of 6.62, was provided in the arms with a tube-like system where was 10 millimeters. The total reactor volume was 18 liters. In the chlorination of wooll chloride to 1,1,2-trichloroethane by injecting chlorine 4.03 kg / h into the reaction space at a vinyl chloride / chlorine molar ratio of 1.02, the reactor produced a reaction temperature of 40 ° C of 500 g / h crude 1.1.2 -trichloroethane per liter of reactor space. The reaction temperature in the reaction zone was maintained at an accuracy of + 0.7 ° C. After 49 hours of reactor overflow, there was no reaction temperature variation in the reaction zone. Example 2 In the same iron reactor as in Example 1, only at a shoulder diameter of 125 mm and a length of 1200 mm, the length / diameter ratio = = 9.6 was injected into the reaction space with 290 g of ethylene per hour per liter of reaction space at a molar ratio of ethylene / chlorine = 1.0. The reactor produced 400 grams of crude 1,2-dichloroethane per hour per liter of reaction volume. At 120 h operation of ethylene chlorination at 60 ° C, no uncontrolled chlorination occurred and the reaction temperature was maintained at 60-60.5 ° C in the reaction space.

Claims (1)

SUBJECT Liquid-phase chlorination reactor equipped with a chlorine and chlorinated material supply with a cooling device, characterized in that it consists of a continuous vessel in which the arms, where the height: diameter ratio is 6 to 10, are tubular systems separating the reaction mixture from the cooling medium. wherein the feedstock feed is located below the lower edge of the tubular system, preferably coaxial with the bottom of the continuous vessel, and the arms of the continuous vessel above the tubular system are interconnected and at least one arm is connected with gas and overflow for the product situated above the upper level linked arms.