CN111100095A - Method for separating propylene oxide, acrolein and acetone which are propylene oxidation products - Google Patents
Method for separating propylene oxide, acrolein and acetone which are propylene oxidation products Download PDFInfo
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- CN111100095A CN111100095A CN201911347759.6A CN201911347759A CN111100095A CN 111100095 A CN111100095 A CN 111100095A CN 201911347759 A CN201911347759 A CN 201911347759A CN 111100095 A CN111100095 A CN 111100095A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D303/00—Compounds containing three-membered rings having one oxygen atom as the only ring hetero atom
- C07D303/02—Compounds containing oxirane rings
- C07D303/04—Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/40—Extractive distillation
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- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
- C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C45/82—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
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- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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- C07C45/78—Separation; Purification; Stabilisation; Use of additives
- C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C45/82—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
- C07C45/83—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation by extractive distillation
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- C—CHEMISTRY; METALLURGY
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- C07D—HETEROCYCLIC COMPOUNDS
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- C07D301/32—Separation; Purification
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Abstract
The invention relates to a method for separating propylene oxide, acrolein and acetone which are propylene oxide products, and belongs to the technical field of separation of propylene oxide products. The material to be separated enters a propylene oxide separation tower from the middle section of the tower section for rectification separation, propylene oxide is extracted from the tower top, and acrolein and acetone extracted from the tower bottom go to an extraction rectification tower; the mixture of acrolein and acetone and the extractant to be separated enter an extraction rectifying tower in two paths for extraction, rectification and separation, and acetone is extracted from the top of the tower; the acrolein and the extractant distilled from the tower bottom enter a solvent recovery tower for rectification and separation, the acrolein is extracted from the tower top, and the extractant is extracted from the tower bottom; the extractant is recycled to the extraction rectifying tower for use. The invention has scientific and reasonable design, realizes the separation of high purity and high recovery rate of materials, realizes more economic separation on the basis of comprehensively considering the process cost of energy consumption, material consumption and the like, and has larger application prospect in industry.
Description
Technical Field
The invention relates to a method for separating propylene oxide, acrolein and acetone which are propylene oxide products, and belongs to the technical field of separation of propylene oxide products.
Background
As a large industrial process, the oxidation reaction of propylene has important application, and main products comprise propylene oxide, acrolein, acetone and the like. The three components have similar structures, especially the boiling points of the acrolein and the acetone are similar, the polarities are similar, although an azeotrope is not formed, because the relative volatility is very small, if the acrolein and the acetone are separated by adopting common rectification, the required theoretical plate number and the reflux ratio are very large, and the economic feasibility is not realized.
Chinese patent CN201810852178.7 discloses a method for separating acrolein, a volatile substance of automotive upholstery, from acetone and a method for measuring the same, wherein liquid chromatographic columns are used for the separation of the acrolein and the acetone, but the chromatographic method is difficult to apply on an industrial scale. Currently, no relevant industrial process for the specific separation of acrolein and acetone has been found for a while.
U.S.9,115,067 proposes a method for producing acrolein by using a conventional rectification process with side draw for purifying acrolein, but because the process uses water to quench the reaction gas phase discharge and acrolein is azeotroped with water, only acrolein with a purity of 93.45% can be obtained at the side draw position near the top of the tower, which is difficult to meet the application requirements. U.S. Pat. No. 4,620,901, U.S. Pat. No. 4,931,145 and others propose azeotropic distillation and extractive distillation to separate and purify acetone, which achieves good separation effect and economy, but the impurities in the system to be separated are mainly methanol, benzene and the like, and do not contain acrolein.
Disclosure of Invention
The technical problem to be solved by the invention is to overcome the defects in the prior art, provide a separation method of propylene oxide products, namely propylene oxide, acrolein and acetone, and have scientific and reasonable design, so that the separation of high purity and high recovery rate of materials is realized, more economic separation is realized on the basis of comprehensively considering process costs of energy consumption, material consumption and the like, and the separation method has a wide application prospect in industry.
According to the method for separating propylene oxide, acrolein and acetone, materials to be separated comprise three types of propylene oxide, acrolein and acetone, the materials enter a propylene oxide separation tower from the middle section of a tower section, rectification separation is carried out under certain conditions, the propylene oxide is extracted from the top of the tower, and the acrolein and the acetone extracted from the bottom of the tower go to an extraction rectification tower. The mixture of acrolein and acetone and the extractant to be separated enter an extractive distillation tower in two paths, and are subjected to extractive distillation separation under certain operating conditions. The acetone is extracted from the top of the tower, and the acrolein and the extractant distilled from the bottom of the tower enter a solvent recovery tower for separation. In a solvent recovery tower, rectification separation is carried out under certain operating conditions, acrolein is extracted from the tower top, and an extracting agent is extracted from the tower kettle; the extractant is recycled to the extraction rectifying tower for use. Thereby, the high-efficiency separation of propylene oxide, acrolein and acetone is realized.
Preferably, the operating conditions of the propylene oxide separation column are as follows: the theoretical plate number is 40-60, the tower top operating pressure is 0.1-0.3 MPa, the reflux ratio is 2-4: 1, the temperature of the top of the tower is 30-55 ℃, and the temperature of the bottom of the tower is 50-80 ℃; the feeding position is between 25 th theoretical plates and 35 th theoretical plates. After the propylene oxide separation column is pressurized, the heat of the propylene oxide separation column can be integrated into a solvent recovery column and the like below for use.
Preferably, the extractant is one or more of toluene, furfural, amyl acetate, phenol, ethylene glycol, glycerol, benzaldehyde, dimethyl sulfoxide (DMSO), N-Dimethylformamide (DMF), aniline, ethylene glycol monomethyl ether, dipropylene glycol dimethyl ether, or methyl pyrrolidone (NMP).
Preferably, the operating conditions of the extractive distillation column are as follows: the theoretical plate number is 25-50, the operation pressure at the top of the tower is 0.02-0.1 MPa, the reflux ratio is 0.5-3: 1, the temperature at the top of the tower is 10-70 ℃, and the temperature at the bottom of the tower is 60-130 ℃; the raw material feeding position is between 10 th theoretical plate and 30 th theoretical plate. On the premise of ensuring the separation effect, the invention respectively adopts a sequential method, a particle swarm method and a traditional sensitivity analysis method to innovate each parameter in the process by aiming at the minimum total cost TAC of the process year.
The extractive distillation process, which can be operated at virtually atmospheric pressure, is preferred in the present invention to reduce the distillation temperature by reducing the pressure, taking into account the tendency of acrolein to polymerize; in addition, the heating time is reduced by continuous feeding and rectification, so that the polymerization reaction of the acrolein is inhibited, and the recovery rate and the purity of the acrolein are improved.
Preferably, the feeding flow ratio of the extracting agent entering the extraction and rectification tower to the raw material is 0.5-3: 1, and the feeding position of the extracting agent is between 2 nd and 8 th theoretical plates of the extraction and rectification tower.
Preferably, the operating conditions of the solvent recovery column are as follows: the theoretical plate number is 5-25, the operation pressure at the top of the tower is 0.01-0.1 MPa, the temperature at the top of the tower is 0-70 ℃, the reflux ratio is (0.05-1): 1, and the temperature at the bottom of the tower is 130-210 ℃; the material feeding position is between the 3 rd theoretical plate and the 15 th theoretical plate. In order to prevent acrolein from generating polymerization reaction, the invention carries out reduced pressure and temperature reduction treatment on the solvent recovery tower.
In the invention, the separation of acrolein, acetone mixture and propylene oxide is realized by normal pressure rectification, and the propylene oxide with the purity of more than 99.8 percent is extracted from the tower top; then an extractive distillation tower and a solvent recovery tower are combined, and an extractant is added for extractive distillation, so that the acrolein and acetone with the concentration of more than or equal to 99.5 wt% and the product recovery rate of more than or equal to 90 wt% can be obtained through purification.
In the invention, when the process cost such as energy consumption, material consumption and the like is comprehensively considered, the factors such as the separation degree, the heat integration degree, the heat sensitivity and the like are also considered.
The process design and research are carried out by taking acrolein and acetone byproducts generated by 10 ten thousand tons of propylene oxide produced every year as an example. Assuming that the annual operation time is 8000 hours, the total feeding amount converted to the acrolein and acetone separation section is 1980kg/hr, wherein the acrolein is 900kg/hr, the acetone is 1080kg/hr, and the design requirement is as follows: the content of the acrolein product is more than or equal to 99.5 wt%, and the recovery rate of the acrolein is more than 99.5 wt%; the content of acetone products is more than or equal to 99 wt%, and the recovery rate of acetone is more than or equal to 99%. The total loss of extractant is not more than 3 kg/hr.
The algorithms take the total annual cost and optimization time as high and low indexes on the basis of meeting the design requirements. Two new algorithms, namely a sequential method and a particle swarm method, can obtain faster convergence, are favorable for improving the operation precision, can obtain overall better process parameters and reduce the cost.
The invention has the following beneficial effects:
(1) the invention provides a mild and efficient rectification separation process for three components with similar structures and high activity in a propylene oxidation product, and particularly aims at an acrolein and acetone system which is difficult to separate in conventional rectification, and the extraction agent is introduced to change the relative volatility of the materials and realize the separation of the materials with high purity and high recovery rate;
(2) on the premise of ensuring the separation effect, the invention combines some new simulation algorithms (such as a sequential method and a particle swarm method) to adjust the process parameters on the basis of comprehensively considering the process cost of energy consumption, material consumption and the like, thereby realizing more economic separation and having greater application prospect in industry.
Drawings
FIG. 1 is a process flow diagram of the present invention;
in the figure: a C-101 propylene oxide column; c-102 extractive distillation column; a C-103 solvent recovery column; a reboiler of a tower kettle of the E-101 epoxypropane tower; an E-102 propylene oxide tower top condenser; e-103 extracting rectifying tower kettle reboiler; a condenser at the top of the E-104 extractive distillation tower; a reboiler at the tower bottom of the E-105 solvent recovery tower; a condenser at the top of the E-105 solvent recovery tower; e-107 extractant circulating heat exchanger; a reflux tank at the top of the T-101 epoxypropane tower; a reflux tank at the top of the T-102 extractive distillation tower; a reflux tank at the top of the T-103 solvent recovery tower; a P-101 propylene oxide column feed pump; a material pump is arranged at the top of the P-102 propylene oxide tower; a tower bottom circulating pump of the P-103 propylene oxide tower; a P-104 extractant make-up feed pump; a material ejection pump of the P-105 extractive distillation tower; a discharge pump at the bottom of the P-106 solvent recovery tower; a circulating pump at the bottom of the P-108 extraction rectifying tower.
Detailed Description
The present invention is further illustrated by the following examples, which are not intended to limit the practice of the invention.
Example 1
The material to be separated is a mixture of propylene oxide, acrolein and acetone, and the mass ratio is 5: 1: 0.9. the material enters a propylene oxide tower C-101 from a 30 th theoretical plate, the tower has 45 theoretical plates in total, the operating pressure at the top of the tower is 0.2MPa, the reflux ratio is 3.5, the temperature at the top of the tower is 54.9 ℃, the temperature at the bottom of the tower is 76.3 ℃, propylene oxide with the purity of 99.8 percent is obtained at the top of the tower, and the product recovery rate reaches 98.9 percent.
Materials at the bottom of the propylene oxide tower mainly comprise acrolein and acetone, ethylene glycol is used as an extracting agent, the acrolein and the acetone enter an extraction rectifying tower in two paths, and normal pressure rectification is adopted, wherein the extraction rectifying tower C-102 is provided with 30 theoretical plates, the material to be separated is fed from the 20 th theoretical plate, the extracting agent is fed from the 5 th theoretical plate, and the feeding flow ratio of the extracting agent to the raw material is 1: 1. The reflux ratio is 1, the temperature at the top of the tower is 56.1 ℃, the temperature at the bottom of the tower is 107.2 ℃, acetone products with the purity of 99.5 wt% are obtained at the top of the tower, and the product recovery rate reaches 96.5%.
The tower bottom material of the extraction and rectification tower enters an extractant recovery tower C-103, the number of theoretical plates is 10, the feeding position is the 5 th plate, normal pressure operation is adopted, the reflux ratio is 0.34, the tower top temperature is 52.8 ℃, the tower bottom temperature is 198.3 ℃, an acrolein product with the purity of 99.5 wt% is obtained at the tower top, and the product recovery rate reaches 89.7%. The tower bottom is used as extractant of glycol and very little acrolein, and the extractant is returned to C-102 for recycling after heat exchange and temperature reduction to 40 ℃.
Example 2
Selecting a system to be separated which is the same as that in the embodiment 1, wherein the material to be separated is a mixture of propylene oxide, acrolein and acetone, and the mass ratio is 5: 1: 0.9. the material enters a propylene oxide tower C-101 from a 25 th theoretical plate, the tower has 40 theoretical plates, the operation pressure at the top of the tower is normal pressure, the reflux ratio is 2.71, the temperature at the top of the tower is 34.2 ℃, the temperature at the bottom of the tower is 54.4 ℃, a propylene oxide product with the purity of 99.9 percent is obtained at the top of the tower, and the product recovery rate reaches 98.5 percent.
The materials at the bottom of the epoxypropane tower mainly comprise acrolein and acetone, N-dimethyl Diamide (DMF) is taken as an extracting agent, the acrolein and the acetone are divided into two paths to enter an extraction rectifying tower, and normal pressure rectification is adopted. Wherein, the extractive distillation column C-102 is provided with 50 theoretical plates, the material to be separated is fed from the 30 th theoretical plate, the extracting agent is added from the 6 th theoretical plate, and the feeding flow ratio of the extracting agent to the raw material is 2: 1. The reflux ratio is 2.5, the temperature at the top of the tower is 56.1 ℃, the temperature at the bottom of the tower is 121.8 ℃, acetone with the purity of 99.5 wt% is obtained at the top of the tower, and the product recovery rate reaches 98.1%.
The material in the bottom of the extraction and rectification tower enters an extractant recovery tower C-103, the number of theoretical plates is 24, the feeding position is the 12 th plate, normal pressure operation is adopted, the reflux ratio is 0.2, the temperature at the top of the tower is 52.8 ℃, the temperature in the bottom of the tower is 154.6 ℃, acrolein with the purity of 99.5 wt% is obtained at the top of the tower, and the product recovery rate reaches 92.6%. The tower bottom is used as an extractant DMF and a little acrolein, and the extractant DMF and the little acrolein are cooled to 40 ℃ and then returned to C-102 to be used as the extractant for recycling.
Example 3
Selecting a system to be separated as in example 1, wherein the material to be separated is a mixture of propylene oxide, acrolein and acetone, and the mass ratio is 5: 1: 0.9. the material enters a propylene oxide tower C-101 from a 25 th theoretical plate, the tower has 40 theoretical plates, the operation pressure at the top of the tower is normal pressure, the reflux ratio is 2.85, the temperature at the top of the tower is 34.2 ℃, the temperature at the bottom of the tower is 54.4 ℃, propylene oxide with the purity of 99.9 percent is obtained at the top of the tower, and the product recovery rate reaches 98.5 percent.
The materials at the bottom of the epoxypropane tower mainly comprise acrolein and acetone, ethylene glycol is used as an extracting agent, and the acrolein and the acetone enter an extraction rectifying tower in two ways and are rectified at normal pressure. Wherein, the extractive distillation column C-102 is provided with 37 theoretical plates, the material to be separated is fed from the 18 th theoretical plate, the extracting agent is added from the 4 th theoretical plate, and the feeding flow ratio of the extracting agent to the raw material is 1.8: 1. The reflux ratio is 2.1, the temperature at the top of the tower is 56.1 ℃, the temperature at the bottom of the tower is 107.6 ℃, acetone with the purity of 99.5 wt% is obtained at the top of the tower, and the product recovery rate reaches 98.8%.
The material in the bottom of the extraction and rectification tower enters an extractant recovery tower C-103, the number of theoretical plates is 14, the feeding position is 7 th plate, normal pressure operation is adopted, the reflux ratio is 0.18, the temperature of the top of the tower is 52.8 ℃, the temperature of the bottom of the tower is 198.5 ℃, acrolein with the purity of 99.5 wt% is obtained at the top of the tower, and the product recovery rate reaches 88.4%. The tower bottom is provided with extractant ethylene glycol and a little acrolein, and the extractant ethylene glycol and the little acrolein return to C-102 after being cooled to 40 ℃ to be used as the extractant for recycling.
Example 4
Selecting a system to be separated which is the same as that in the embodiment 1, wherein the material to be separated is a mixture of propylene oxide, acrolein and acetone, and the mass ratio is 5: 1: 0.9. the material enters a propylene oxide tower C-101 from a 25 th theoretical plate, the tower has 40 theoretical plates, the operation pressure at the top of the tower is normal pressure, the reflux ratio is 2.85, the temperature at the top of the tower is 34.2 ℃, the temperature at the bottom of the tower is 57.4 ℃, propylene oxide with the purity of 99.9 percent is obtained at the top of the tower, and the product recovery rate reaches 98.1 percent.
Materials at the bottom of the propylene oxide tower mainly comprise acrolein and acetone, ethylene glycol is used as an extracting agent, the acrolein and the acetone enter an extraction rectifying tower C-102 in two paths, the reduced pressure rectifying operation is adopted, and the operating pressure at the top of the tower is 0.03 MPa. C-102 has 30 theoretical plates, the material to be separated is fed from the 12 th theoretical plate, the extractant is fed from the 4 th theoretical plate, and the feeding flow ratio of the extractant to the raw material is 1.5: 1. The reflux ratio is 1.78, the temperature at the top of the tower is 24.4 ℃, the temperature at the bottom of the tower is 68.1 ℃, an acetone product with the purity of 99.7 wt% is obtained at the top of the tower, and the product recovery rate reaches 99.2%.
The materials in the bottom of the extraction and rectification tower enter an extractant recovery tower C-103, the number of theoretical plates is 14, the feeding position is 7 th plate, the reduced pressure rectification operation is adopted, the operation pressure at the top of the tower is 0.02MPa, the reflux ratio is 0.12, the temperature at the top of the tower is 11.01 ℃, the temperature at the bottom of the tower is 155.4 ℃, the acrolein with the purity of 99.6 wt% is obtained at the top of the tower, and the product recovery rate reaches 94.2%. The tower bottom is provided with extractant ethylene glycol and a little acrolein, and the extractant ethylene glycol and the little acrolein return to C-102 after being cooled to 40 ℃ to be used as the extractant for recycling.
Comparative example 1
The same system to be separated as in example 1 was selected and the extractant was changed from ethylene glycol to water. Because the boiling points of the extracting agents are different, the temperature parameters of the extraction rectifying tower and the solvent recovery tower are correspondingly adjusted, and the rest parameters of the whole process are the same as those of the embodiment 1. The temperature of the top of the extraction and rectification tower is 54.7 ℃, the temperature of the bottom of the tower is 78.4 ℃, acetone with the purity of 63.7 wt% is obtained at the top of the tower, and the product recovery rate is 65.4%. The temperature of the top of the solvent recovery tower is 53.2 ℃, the temperature of the bottom of the tower is 99.5 ℃, acrolein with the purity of 59.2 wt% is obtained at the top of the tower, and the product recovery rate is 49.1%. The bottom of the solvent recovery tower is filled with extracting agent water and acrolein, and the content of the acrolein is 2.45 wt%.
It can be seen that the use of water as the extractant, using essentially the same process parameters as in example 1, does not achieve an effective separation of acrolein and acetone.
Comparative example 2
Further, whether the effective separation of the acrolein and the acetone can be realized by taking water as an extracting agent and optimizing process parameters is examined. Selecting a system to be separated as in example 1, taking water as an extracting agent aiming at the separation of acrolein and acetone, and enabling the acrolein and the acetone to enter an extraction rectifying tower in two ways and adopting normal pressure rectification. Wherein the extractive distillation column C-102 is provided with 60 theoretical plates, the material to be separated is fed from the 32 th theoretical plate, the extracting agent is added from the 5 th theoretical plate, and the feeding flow ratio of the extracting agent to the raw material is 2: 1. The reflux ratio is 3.5, the temperature at the top of the tower is 52.78 ℃, the temperature at the bottom of the tower is 101.15 ℃, and an acetone product with the purity of 98.46 wt% is obtained at the top of the tower, wherein the water content is 1.18wt 5%, and the acrolein content is 0.3 wt%.
The tower bottom material enters an extractant recovery tower C-103, the theoretical plate number is 33, the feeding position is the 25 th plate, the pressure reduction operation is adopted, the tower top pressure is 0.7bar, the reflux ratio is 15, the tower top temperature is 45.58 ℃, the tower bottom temperature is 93.25 ℃, and the acrolein product with the purity of 98.9 wt% is obtained at the tower top. The tower bottom is extracting agent water and 1.03 wt% acetone, and the extracting agent water and the acetone are cooled to 40 ℃ and then returned to C-101 to be used as the extracting agent for recycling.
Therefore, when water is selected as an extracting agent, even if more rigorous distillation process parameters are adopted (such as increasing the number of theoretical plates of an extraction and distillation tower to 60, increasing the reflux ratio of a solvent recovery tower to 15, increasing the relative volatility among components by introducing vacuum distillation and other measures), the energy consumption and equipment cost are greatly increased, the final distillation effect cannot meet the requirements, and both the acrolein and the acetone cannot reach the purity in the embodiment.
Claims (6)
1. A method for separating propylene oxide, acrolein and acetone which are propylene oxidation products is characterized in that: feeding the material to be separated into a propylene oxide separation tower from the middle section of the tower section for rectification separation, extracting propylene oxide from the tower top, and sending acrolein and acetone extracted from the tower bottom to an extraction rectification tower; the mixture of acrolein and acetone and the extractant to be separated enter an extraction rectifying tower in two paths for extraction, rectification and separation, and acetone is extracted from the top of the tower; the acrolein and the extractant distilled from the tower bottom enter a solvent recovery tower for rectification and separation, the acrolein is extracted from the tower top, and the extractant is extracted from the tower bottom; the extractant is recycled to the extraction rectifying tower for use.
2. The process according to claim 1 for the separation of propylene oxide, acrolein and acetone, which are products of the oxidation of propylene, characterized in that: the operating conditions of the propylene oxide separation column were as follows: the theoretical plate number is 40-60, the tower top operating pressure is 0.1-0.3 MPa, the reflux ratio is 2-4: 1, the temperature of the top of the tower is 30-55 ℃, and the temperature of the bottom of the tower is 50-80 ℃; the feeding position is between 25 th theoretical plates and 35 th theoretical plates.
3. The process according to claim 1 for the separation of propylene oxide, acrolein and acetone, which are products of the oxidation of propylene, characterized in that: the extractant is one or more of toluene, furfural, amyl acetate, phenol, ethylene glycol, glycerol, benzaldehyde, dimethyl sulfoxide, N-dimethylformamide, aniline, ethylene glycol monomethyl ether, dipropylene glycol dimethyl ether or methyl pyrrolidone.
4. The process according to claim 1 for the separation of propylene oxide, acrolein and acetone, which are products of the oxidation of propylene, characterized in that: the operating conditions of the extractive distillation column were as follows: the theoretical plate number is 25-50, the operation pressure at the top of the tower is 0.02-0.1 MPa, the reflux ratio is 0.5-3: 1, the temperature at the top of the tower is 10-70 ℃, and the temperature at the bottom of the tower is 60-130 ℃; the raw material feeding position is between 10 th theoretical plate and 30 th theoretical plate.
5. The process according to claim 1 for the separation of propylene oxide, acrolein and acetone, which are products of the oxidation of propylene, characterized in that: the feed flow ratio of the extracting agent entering the extraction and rectification tower to the raw material is 0.5-3: 1, and the feed position of the extracting agent is between 2 nd to 8 th theoretical plates of the extraction and rectification tower.
6. The process according to claim 1 for the separation of propylene oxide, acrolein and acetone, which are products of the oxidation of propylene, characterized in that: the operating conditions of the solvent recovery column were as follows: the theoretical plate number is 5-25, the operation pressure at the top of the tower is 0.01-0.1 MPa, the temperature at the top of the tower is 0-70 ℃, the reflux ratio is (0.05-1): 1, and the temperature at the bottom of the tower is 130-210 ℃; the material feeding position is between the 3 rd theoretical plate and the 15 th theoretical plate.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114191837A (en) * | 2021-12-07 | 2022-03-18 | 大连理工大学 | Device and method for separating methanol-benzene-acetonitrile azeotrope system by extractive distillation |
| CN116041162A (en) * | 2022-10-28 | 2023-05-02 | 江苏扬农化工集团有限公司 | Method for separating and recovering acrolein from product system for preparing 3-hydroxy propanal by hydration of acrolein |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114191837A (en) * | 2021-12-07 | 2022-03-18 | 大连理工大学 | Device and method for separating methanol-benzene-acetonitrile azeotrope system by extractive distillation |
| CN114191837B (en) * | 2021-12-07 | 2023-02-14 | 大连理工大学 | Device and method for separating methanol-benzene-acetonitrile azeotrope system by extractive distillation |
| CN116041162A (en) * | 2022-10-28 | 2023-05-02 | 江苏扬农化工集团有限公司 | Method for separating and recovering acrolein from product system for preparing 3-hydroxy propanal by hydration of acrolein |
| CN116041162B (en) * | 2022-10-28 | 2024-04-12 | 江苏扬农化工集团有限公司 | Method for separating and recovering acrolein from product system for preparing 3-hydroxy propanal by hydration of acrolein |
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