PL39421B1 - - Google Patents

Description

OF THE REPUBLIC OF PEOPLE PATENT DESCRIPTION.

No. 39421 KL 12 ly 8 Inowroclawskie Zaklady Sodowe *) Inowroclaw-Matwy, Poland Carbonization method in the soda production process and device for using this method The patent has been valid since May 28, 1955

In the production of soda, the carbonization process carried out in columns equipped with pastes proceeds with a large loss of reacting components, and it is impossible to bring the system to the state of optimal equilibrium.

The process according to the invention eliminates the above-mentioned disadvantages and allows for a significant reduction of the losses of raw materials taking part in the reaction, and thus enables an increase in the yield.

The method according to the invention introduces changes to the process parameters, namely the concentration of solutions, temperature and pressure, which are related to the design changes of the device.

It is known that the speed of the processes taking place in a heterogeneous system and taking place on the interface of the phases is proportional. *) The owner of the patent stated that the inventors of the invention are engineer Leon Mischke and Dr. Ernest Pischinger. to this surface. Since chemical exchange can only take place as a result of meetings between molecules, and these meetings can only take place on the surface of two phases, it is necessary to strive to ensure that the largest possible number of reacting particles is on this surface.

Thus, the application of the principle of developing the largest possible reaction surface determines the speed of bringing the state of the system to the optimal equilibrium, for the given temperature, pressure and concentration conditions in which the process takes place.

In the existing design of the column, the principle of developing the largest possible reaction surface has not been fully applied. The carbonization process takes place almost along the entire height of the apparatus, and the height of the column is probably the resultant of the reactions taking place. In the device, according to the invention * presented in the figure, the column has been divided into 3 functional parts: crystallizer A, reactor B and swanger C. '*' So far the strips used at the top of the column have been eliminated. Crystallizer A remains the unchanging lower part of the known column, in which the liquid cools down after the reaction with a simultaneous precipitation of the NaHCO2 crystal, which should be as large as possible.

In order to maintain the most appropriate conditions for the crystallization process, cooling should be slow and gradual.

In order to keep the given conditions, the currently used method of double cooling was changed to single-flow cooling.

Reactor B is located in the center of the column and occupies about 1 / of the height of the known columnar mass. In this part of the column, the main reaction is taking place, it is forming. crystallization of NaHCOg and there is a large transfer of solution depending on the temperature in the reactor. The column of liquid between reactor B and plugger C is broken.

The overhead gas is fed at point 2 above the liquid table in the crystallizer, the composition of which, mixed with the rest of the unreacted downstream gas, fed to the column at point 4 via a special device for gaseous phase development, is stored through a column of carbonized liquid. According to the invention, 100% NHs is added to the overhead gas in amounts resulting from the concentration of the solutions.

The reactions should be carried out at a temperature elevated to about 70% C.

The volumetric C p of the scrubber structure takes up the remaining trade-off portion of the column, and its task is to absorb it, to return unreacted CQ2 to the process and entrained from the reactor with the gas of ammonia particles.

The new structure of the column creates different conditions for the carbonization and crystallization process.

The temperature, pressure and concentration of fCO's, WH''s and CV in individual parts of the column undergo changes, and the basic parameters of both the chemical reaction and the crystallization process.

As a result of these structural changes and the changes they cause in the parameters of the chemical reaction and the crystallization process, in the new system there is a more strict delimitation of the individual strong phases of the process taking place at the same time, starting from the entry of the liquid into the column at point 1 in In part C, the so-called scavenger takes place by trapping unreacted COt, thereby increasing the concentration of HCO's and, consequently, reducing the ammonia pellet capacity, which again prevents ammonia blowing out. The effect is greater the lower the temperature of the liquid supplied from the carbonator.

As a result, a liquid with a higher concentration of HCO's and NH4 enters the reactor B of the main reaction zone, which has a favorable effect on the course of the reaction. The effect of Teaction is the release of large amounts of heat per unit time in a relatively small space. This results in a different temperature distribution in the so-called crystallizer A, the higher concentration of HCO's, the relatively high temperature and the reduced total pressure in the reactor due to the broken liquid column between the reactor and the scrubber require an increase in the NH.sub.4 concentration. ? In this way, the detrimental effect of high temperature on the equilibrium state is completely eliminated and an increase in HCO's concentration is used.

In the high temperature reactor, the carbonization process takes place rapidly and a high saturation state is achieved, while the number of crystallization nuclei is relatively small.

In the crystallizer A - provided that the cooling process is carried out evenly and gradually, differently from the previous one, the crystallization process takes place, which at a relatively high temperature of 35 ° Cr with a relatively small number of seeds in the liquid introduced through the conduit 5 to the crystallizer, allows to obtain thick, clear crystal that can be easily drained and washed away. The liquid is drained from the crystallizer A at point 3.

The introduction of changes in the ammonia concentration and temperature allowed to increase the efficiency of the process and to obtain a thicker crystal. 2. Patent reference 1. Carbonization method in the soda production process, characterized in that 100% NH * is introduced into the reactor in order to increase the concentration of NH * 4 ions and the reactions are carried out at an elevated temperature of about 70 ° C .2. The method according to p. The process of claim 1, characterized in that the crystallization is carried out at a temperature of 35 ° C. 3. Device for applying the method according to claim Device according to Claim 1, 2, characterized in that it is divided into 3 functional parts, namely crystallizer A, reactor B, and plugger C. 3. The bulkhead of claim 3, characterized in that it has a mesh or fabric barrier for the overhead gas.

Inowroclawskie Zaklady Sodowe