Teacher friends, please talk about how to cooperate with reaction fractionation to improve product quality?

In the actual production process of organizational refining, for a given raw material, within a certain period of time, under a basically certain market environment, the production plan and technical indicators are basically constant. That is to say, the reaction depth is generally strictly required and controlled, and cannot be changed casually by the operator. . . Therefore, the adjustment of product quality indicators in fractionation positions is generally basically stable. . . If there is a problem in the raw material replacement stage or the depth of response of the reaction post is adjusted, generally the factory technical department or the production scheduling department and the workshop will make adjustment arrangements. The fractionation post can follow up in a timely manner based on the adjustment of the previous post, that is, the reaction post. . . If the reaction temperature is raised, the total amount of oil and gas may increase, and the oil and gas temperature will increase a lot. . . Then pay attention to suppressing the load at the top of the tower at all times to avoid overheating, causing the tower to flush or the crude gasoline and diesel distillation range to fail. . . Adjust and control all processes of the oil slurry system, and keep the temperature to about 385. In particular, the liquid phase temperature must not exceed 400 for too long, otherwise the density of the oil slurry will rise quickly and gradually coke and block. . . Don’t say more and just emphasize these points. . . :lol

:funk: Adjust and control all processes of the oil slurry system, and keep the temperature to about 385. In particular, the liquid phase temperature should never exceed 400 for too long, otherwise the density of the oil slurry will rise quickly and gradually coke and block. . . :lol :lol Who dares to raise the temperature to such a high temperature? Unless you want to stop work, don't say 385. Even if it is 365, you have to consider it. Even wax 385 is enough:D

Haha, the liquid phase temperature of the oil slurry system is generally controlled below 390 degrees... and the gas phase temperature is below 400 degrees... This is correct...

The bottom temperature of the tower in my unit is controlled below 350°. The reaction depth is large and the bottom temperature of the tower is high. I use raw materials to supplement the tower to lower the bottom temperature.

It seems that the conditions of each device are different. The temperature at the bottom of our tower is controlled below 350°C, and generally does not exceed 340°C.

Under normal circumstances, the temperature of the fractionation tower should be adjusted in time according to the reaction temperature, and the dry point of gasoline and oil slurry temperature should be controlled well. If the reaction temperature is raised, the total amount of oil and gas will increase, and the temperature of oil and gas will increase a lot. Care should be taken to suppress the load on the top of the tower and not to overheat, causing tower flushing or unqualified distillation ranges of naphtha and diesel.

Thank you to the senior masters for their teachings. , now I finally understand. Referring to some parameters, it is believed that the general conclusion is that the control should not be greater than 350 degrees. If it is too high, it will increase the chance of coking.

In the fractional distillation operation, under the condition of controlling the temperature at the bottom of the tower, the adjustment of the product should be adjusted according to the device plan and product requirements, and the top temperature, middle section, diesel extraction and other parameters should be adjusted. But stress is controlled by reaction.

The main effects of reaction on fractionation are: 1. The higher the reaction temperature and the greater the depth, the more heat is brought to the fractionation tower. Under the same conversion rate, the gas volume increases. For the operation of the fractionation tower, it is necessary to appropriately increase the reflux of each section, especially to increase the flow rate of the oil slurry returning to the tower and reduce the temperature of the herringbone plate to prevent the liquid level at the bottom of the tower from being too low and the rising gas phase being too large, resulting in unqualified product quality. 2. Changes in the total reaction feed, oil slurry refining, temperature and pressure changes in the fractionation tower, and adjustment of reflux temperature and flow. 3. Changes in the amount of reaction steam directly affect the interface of the oil and gas separator and the dry point of naphtha, because the partial pressure of oil and gas in the fractionating tower changes. 4. When the reaction pressure is high, the fractionation will also increase, and the partial pressure of oil and gas in the fractionation tower will increase. Therefore, the top temperature of the fractionation tower should be appropriately increased to ensure that the dry point of naphtha is qualified. In addition, I am a little confused about the statement on the second floor. According to the current nature of the raw materials, the bottom temperature of the fractionation tower cannot be that high. Our original wax bottom temperature is generally controlled at 375, which is the upper limit, and coking at the bottom of the tower is serious during maintenance. Now our heavy oil catalytic bottom temperature is controlled at around 320-335, and the herringbone plate temperature is around 325.

The operation of fractionation must be adjusted according to the properties of the raw materials and the depth of reaction, and the heat balance must be controlled. Nowadays, the properties of raw materials are getting worse and worse. Special attention should be paid to the temperature at the bottom of the tower not to exceed 350° and the temperature at the top of the tower not to be lower than 110°.

The reaction and fractionation systems are integrated, not separate. Various operations of the reaction will definitely affect the control of fractionation. The key is to coordinate well, prevent in advance, and reduce excessive fluctuations. Reaction is the cause and fractionation is the effect. In addition, the temperature at the bottom of the fractionation tower generally does not exceed 355 degrees. When the temperature is too high, polycyclic aromatic hydrocarbons will generate condensed ring aromatic hydrocarbons and further condense into coke. The temperature at the bottom of the tower cannot be too high to reduce the residence time.

1. The liquid level in the fractionation tower is higher than the reaction oil and gas inlet line, which will cause the reaction pressure to be extremely high. 2. Excessive cold reflux in the fractionating tower will cause the reaction pressure to be extremely high. 3. If the liquid level in the oil and gas fractionation tank at the top of the fractionation tower is too high, it will also affect the reaction pressure. 3. Reaction depth, reaction temperature, reaction feed volume, and reaction accidents will all affect fractionation. 4. The amount of reaction stripping steam and other steam directly affects the liquid level of the oil and gas separator at the top of the tower, as well as the dry point of the naphtha.