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CN-121971873-A - Rectification system and process of diisobutyl ketone

CN121971873ACN 121971873 ACN121971873 ACN 121971873ACN-121971873-A

Abstract

A rectification system of diisobutyl ketone is prepared as connecting feed port of dehydration column to diisobutyl ketone material source, feeding dehydration column by bottom of dehydration column, feeding MIBK recovery column by bottom of reflux tank of dehydration column, feeding reflux port of dehydration column, feeding DIBK column by bottom of dehydration column, connecting top of reflux tank of DIBK column to negative pressure source, feeding DIBK product to reflux port of DIBK column by bottom of reflux tank of DIBK column, discharging heavy component to outside by bottom of DIBK column, connecting top of reflux tank of MIBK recovery column to negative pressure source, feeding MIBK to reflux port of MIBK recovery column by bottom of reflux tank of MIBK recovery column and discharging light component to outside by bottom of MIBK recovery column. The invention has simple structure and stable operation, and can realize industrialized separation and recovery of diisobutyl ketone materials.

Inventors

  • JIANG GUOXIN

Assignees

  • 华峰集团上海工程有限公司

Dates

Publication Date
20260505
Application Date
20260126

Claims (10)

  1. 1. A rectification system of diisobutyl ketone is characterized by comprising a dehydration tower (1), an acetone recovery tower (6), a light component removal tower (10), a DIBK tower (16) and a MIBK recovery tower (22), The feed inlet of the dehydration tower (1) is connected with a diisobutylketone material source, the top of the dehydration tower is connected with a negative pressure source through a dehydration tower condenser (3), the bottom of the dehydration tower reflux tank (4) is used for feeding an acetone recovery tower (6), the reflux inlet of the dehydration tower (1) is used for feeding acetone, the acetone recovery tower (6) overflows outwards, the bottom of the dehydration tower (1) is used for feeding a light-off tower (10), the top of the light-off tower (10) is used for feeding a light-off tower reflux tank (13) through a light-off tower condenser (12), the top of the light-off tower reflux tank (13) is connected with a negative pressure source, the bottom of the light-off tower reflux tank (13) is used for feeding an MIBK recovery tower (22), the reflux inlet of the light-off tower (10) is used for feeding a DIBK tower (16), The top of the DIBK tower (16) is used for feeding a DIBK tower reflux tank (19) through a DIBK tower condenser (18), the tank top of the DIBK tower reflux tank (19) is connected with a negative pressure source, the tank bottom of the DIBK tower reflux tank (19) is used for feeding a reflux outlet of the DIBK tower (16) and discharging a DIBK product outwards, the bottom of the DIBK tower (16) is used for discharging a heavy component outwards, The top of the MIBK recovery tower (22) is used for feeding the MIBK recovery tower reflux tank (25) through the MIBK recovery tower condenser (24), the tank top of the MIBK recovery tower reflux tank (25) is connected with a negative pressure source, the tank bottom of the MIBK recovery tower reflux tank (25) is used for feeding the reflux port of the MIBK recovery tower (22) and discharging MIBK outwards, and the bottom of the MIBK recovery tower (22) is used for discharging light components outwards.
  2. 2. The rectification system of diisobutyl ketone according to claim 1, wherein the dehydration column (1), the acetone recovery column (6), the light ends column (10), the DIBK column (16) and the MIBK recovery column (22) are all fed in the middle.
  3. 3. The rectification system of diisobutyl ketone as claimed in claim 1, wherein the bottom of the acetone recovery column (6) is fed with effluent to an effluent treatment plant.
  4. 4. A process for rectifying diisobutylketone material using the system of any one of claims 1-3, comprising the steps of: 1) The diisobutyl ketone material enters a dehydration tower, the pressure of the dehydration tower is controlled to be 0.02Mpa (G), the reflux ratio is controlled to be 4:1, the tower top temperature is 58-62 ℃, the tower bottom temperature is 98-102 ℃, the tower top material is sent to an acetone recovery tower, and the tower bottom liquid is sent to a light component removal tower; 2) Controlling the temperature of the acetone recovery tower to be 45+/-3 ℃ and normal pressure, and extracting acetone from the tower top and sewage from the tower bottom; 3) Controlling the pressure of the light component removal tower to be 40kPa (A), the reflux ratio to be 3:1, the tower top temperature to be 68-72 ℃ and the tower bottom temperature to be 113-117 ℃, and sending the tower top material to a MIBK recovery tower and sending the tower bottom liquid to a DIBK tower; 4) Controlling the pressure of the DIBK tower to be 20Kpa (A), the reflux ratio to be 4:1, the tower top temperature to be 86-90 ℃ and the tower bottom temperature to be 126-130 ℃, extracting the DIBK product from the tower top, and extracting heavy components from the tower bottom; 5) Controlling the pressure of the MIBK recovery tower to be 35Kpa (A), the reflux ratio to be 4:1, the tower top temperature to be 63-67 ℃ and the tower bottom temperature to be 100-104 ℃, extracting MIBK from the tower top, and extracting light components from the tower bottom.
  5. 5. The process of claim 4, wherein the diisobutylketone feed in step 1) has a temperature of 58-62 ℃, wherein the acetone content is 40.71%, the MIBK content is 3.05%, the DIBK content is 44.15%, the water content is 6.5%, the light component content is 0.28%, and the heavy component content is 5.32%.
  6. 6. The process of claim 4, wherein the temperature at the top of the column in step 1) is 60 ℃ and the temperature at the bottom of the column is 100 ℃.
  7. 7. The process according to claim 4, wherein the temperature of the acetone recovery column in step 2) is 45 ℃.
  8. 8. The process of claim 4, wherein the temperature at the top of the light component removing column in the step 3) is 70 ℃ and the temperature at the bottom of the light component removing column is 115 ℃.
  9. 9. The process according to claim 4, wherein the temperature at the top of the DIBK column in step 4) is 88℃and the temperature at the bottom of the column is 128 ℃.
  10. 10. The process according to claim 4, wherein the temperature of the top of the MIBK recovery column in step 5) is 65 ℃ and the temperature of the bottom of the column is 102 ℃.

Description

Rectification system and process of diisobutyl ketone Technical Field The invention relates to the field of chemical industry, in particular to a rectification system and a rectification process of diisobutyl ketone. Background Diisobutyl ketone (DIBK) is an important solvent and organic synthesis intermediate. MIBK and acetone are used as raw materials, an intermediate is prepared through condensation, and the intermediate is subjected to hydrogenation reaction to obtain a material containing DIBK. The material contains unreacted MIBK, acetone, byproduct water, and a small amount of byproduct light components and high boiling point heavy components. The traditional separation process has the problems of high separation energy consumption, low purity of separated products and the like. Therefore, how to design a rectification system with low energy consumption, stable operation and easy industrial application is a problem to be solved by the technicians in the field. Disclosure of Invention The invention aims at overcoming the defects of the prior art, and provides a rectifying system for diisobutyl ketone, which has a simple structure and stable operation and can realize industrialized separation and recovery of diisobutyl ketone materials. The second purpose of the invention is to provide a process for separating and recovering diisobutyl ketone materials by using the system, which has low parameter temperature and energy consumption and is easy for industrial application. The technical scheme for achieving the purpose of the invention is that the rectification system of the diisobutyl ketone comprises a dehydration tower, an acetone recovery tower, a light ends removal tower, a DIBK tower and a MIBK recovery tower, wherein a feed inlet of the dehydration tower is connected with a diisobutyl ketone material source, the top of the dehydration tower is connected with a dehydration tower reflux tank through a dehydration tower condenser, the bottom of the dehydration tower reflux tank is connected with the acetone recovery tower, the reflux inlet of the dehydration tower is connected with a negative pressure source, the acetone recovery tower overflows outwards, the bottom of the dehydration tower is connected with the light ends removal tower reflux tank through the dehydration tower condenser, the top of the dehydration tower reflux tank is connected with a negative pressure source, the bottom of the dehydration tower reflux tank is connected with a MIBK recovery tower, the MIBK reflux tank is connected with the MIBK recovery tower, and the MIBK recovery tower is connected with the MIBK reflux tank, and the MIBK recovery tower is connected with the MIBK recovery tower. The dehydration tower, the acetone recovery tower, the light component removal tower, the DIBK tower and the MIBK recovery tower are all fed in the middle. And the tower bottom of the acetone recovery tower is used for discharging sewage to the outside and sending the sewage to a sewage treatment device. The second technical scheme for realizing the purpose of the invention is that the process for rectifying the diisobutyl ketone material by adopting any one of the systems comprises the following steps: 1) The diisobutyl ketone material enters a dehydration tower, the pressure of the dehydration tower is controlled to be 0.02Mpa (G), the reflux ratio is controlled to be 4:1, the tower top temperature is 58-62 ℃, the tower bottom temperature is 98-102 ℃, the tower top material is sent to an acetone recovery tower, and the tower bottom liquid is sent to a light component removal tower; 2) Controlling the temperature of the acetone recovery tower to be 45+/-3 ℃ and normal pressure, and extracting acetone from the tower top and sewage from the tower bottom; 3) Controlling the pressure of the light component removal tower to be 40kPa (A), the reflux ratio to be 3:1, the tower top temperature to be 68-72 ℃ and the tower bottom temperature to be 113-117 ℃, and sending the tower top material to a MIBK recovery tower and sending the tower bottom liquid to a DIBK tower; 4) Controlling the pressure of the DIBK tower to be 20Kpa (A), the reflux ratio to be 4:1, the tower top temperature to be 86-90 ℃ and the tower bottom temperature to be 126-130 ℃, extracting the DIBK product from the tower top, and extracting heavy components from the tower bottom; 5) Controlling the pressure of the MIBK recovery tower to be 35Kpa (A), the reflux ratio to be 4:1, the tower top temperature to be 63-67 ℃ and the tower bottom temperature to be 100-104 ℃, extracting MIBK from the tower top, and extracting light components from the tower bottom. The temperature of the diisobutyl ketone material in the step 1) is 58-62 ℃, wherein the acetone content is 40.71%, the MIBK content is 3.05%, the DIBK content is 44.15%, the water content is 6.5%, the light component content is 0.28% and the heavy component content is 5.32%. The temperature of the tower top in the step 1) is 60 ℃