CN108947777B - Enrichment and separation process of low-concentration multi-component phenol-containing mixture - Google Patents
Enrichment and separation process of low-concentration multi-component phenol-containing mixture Download PDFInfo
- Publication number
- CN108947777B CN108947777B CN201810547922.2A CN201810547922A CN108947777B CN 108947777 B CN108947777 B CN 108947777B CN 201810547922 A CN201810547922 A CN 201810547922A CN 108947777 B CN108947777 B CN 108947777B
- Authority
- CN
- China
- Prior art keywords
- dimethylphenol
- mesitylene
- rectification
- purification
- percent
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/68—Purification; separation; Use of additives, e.g. for stabilisation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
- C07C2601/16—Systems containing only non-condensed rings with a six-membered ring the ring being unsaturated
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides an enrichment and separation process of a low-concentration multi-component phenol-containing mixture, which sequentially comprises the following steps: the method comprises the steps of a 3, 5-dimethylphenol purification process, a 3, 4-dimethylphenol and m-cresol purification process, an isophorone purification process, an mesitylene and mesitylene purification process, wherein the 3, 5-dimethylphenol purification process comprises crystallization purification and decoloration rectification, the 3, 4-dimethylphenol and m-cresol purification process comprises alkalization phase separation, acidification phase separation, primary rectification and secondary rectification, the isophorone purification process comprises molecular distillation and vacuum rectification of reflux, and the mesitylene and mesitylene purification process comprises vacuum rectification of distillate. The method carries out efficient and clean deep treatment on a plurality of byproducts generated in the process of preparing the 3, 5-dimethylphenol by aromatizing the isophorone, can realize the maximization of the utilization rate of the raw materials, and has remarkable economic and social benefits.
Description
Technical Field
The invention belongs to the field of separation and purification processes, and particularly relates to an enrichment and separation process of a low-concentration multi-component phenol-containing mixture.
Background
Isophorone (Isophorone, ISO) is the product of the condensation of acetone, with a chemical name: 3,5, 5-trimethyl-2-cyclohexen-1-one, molecular formula: C9H14O, molecular weight: 138.21, colorless or light yellow transparent liquid, high boiling point, low hygroscopicity, and good dissolving ability, dispersibility, and leveling property. Isophorone is a good solvent for high molecular materials, and can dissolve nitrocellulose, acrylate, alkyd resin, polyester, epoxy resin and the like. Since isophorone has the structure of unsaturated ketone, double bonds can further react to generate important products such as alcohol, acid, amine, ester, isocyanate and the like, and the isophorone has wide application in industries such as plastics, pesticides, medicines, coatings and the like.
3, 5-dimethylphenol is a white crystal with the molecular formula C8H10O, molecular weight 122.17, melting point: 63-66 ℃, boiling point: 222 ℃, density: 0.968, CAS 108-68-9, dissolved in water and ethanol. The 3, 5-dimethylphenol can be used for preparing phenolic resin, medicines, insecticides, dyes and explosives, is an intermediate for preparing carbamate insecticide-carboximide, and can also be used for producing rubber accelerators, anti-aging agents, medicines, spices, phenolic resin and the like. 3, 5-dimethylphenol is also used as an additive of steel rolling cold rolling oil, and can prolong the service life of the cold rolling oil.
The reaction process for preparing 3, 5-dimethylphenol by aromatizing isophorone is mainly carried out by two competitive routes. One of the processes is a phenolic ketone rearrangement process after the demethanization of isophorone, and 3, 5-dimethylphenol is mainly generated; the other process is the decomposition process of isophorone, which can generate various byproducts such as 1,3, 5-trimethylbenzene, m-xylene, toluene, m-cresol, diacetone alcohol, mesityl oxide, acetone and the like.
At the temperature of 550 ℃,3, 5-dimethylphenol formed by demethanization of isophorone is mainly reacted, wherein the content of the 3, 5-dimethylphenol in a reactor can reach 90 percent, and light components and heavy components formed by various byproducts respectively account for about 2 percent.
The main reaction equation is:
the reaction process for preparing 3, 5-dimethylphenol by aromatizing isophorone is as follows:
at present, there are many documents and patent reports on the process for preparing 3, 5-dimethylphenol from isophorone as a raw material, and the documents and patent reports both focus on the research of the reaction process to improve the yield and reduce the consumption, but have less published data on the by-products generated in the reaction process. Particularly, a large amount of research data of low boiling point substances generated in the reaction process are less, the low boiling point substances can cause serious harm to the environment if not collected and treated, and the materials can be fully utilized by classifying, collecting and recycling, so that the economic benefit is obviously improved.
Disclosure of Invention
The invention aims to provide an enrichment and separation process of a low-concentration multi-component phenol-containing mixture, which can realize the full utilization of materials.
According to one aspect of the present invention, there is provided a process for the enrichment separation of a low-concentration multi-component phenol-containing mixture, comprising, in order,: a purification process of 3, 5-dimethylphenol, a purification process of 3, 4-dimethylphenol and m-cresol, a purification process of isophorone, a purification process of mesitylene and mesitylene,
the purification process of the 3, 5-dimethylphenol comprises crystallization purification and decoloration rectification,
the crystallization purification takes a multi-component phenol-containing mixture as a raw material, takes frozen brine as a refrigerant to reduce the multi-component phenol-containing mixture from the normal temperature to 0-1 ℃ at the speed of 5 ℃/h, carries out solid-liquid separation after the temperature reduction is finished, respectively obtains a solid crude product and a secondary mother liquor of 3, 5-dimethylphenol with the mass content of 96-98 percent,
decoloring and rectifying: heating and melting the solid crude product obtained by self-crystallization purification, then feeding the solid crude product into a decoloring and rectifying tower for secondary purification to obtain a finished product with the mass content of 3, 5-dimethylphenol being more than or equal to 98 percent,
the purification process of the 3, 4-dimethylphenol and the m-cresol comprises alkalization phase separation, acidification phase separation, primary rectification and secondary rectification,
alkalization and phase separation: reacting with the secondary mother liquor at normal temperature by using 15% NaOH solution as an alkalizer to generate sodium phenolate dissolved in a water phase, respectively obtaining the water phase and an organic phase through an oil-water separator after the alkalization reaction is finished, controlling the pH value of the water phase to be 9-10,
acidifying and phase splitting: performing acid-base neutralization reaction on a 15% hydrochloric acid solution and the water phase obtained by the alkalization phase separation under normal temperature and pressure and at a reaction pH of 5-6 to generate phenolic substances and water, separating by an oil-water separator to respectively obtain an organic phase and a water phase,
primary rectification: the organic phase obtained by the acidification phase separation enters a primary rectifying tower kettle, and a finished product with the mass content of m-cresol not less than 98 percent is extracted under the conditions that the tower kettle temperature is not higher than 130 ℃, the tower top temperature is not higher than 110 ℃ and the vacuum degree is-0.098 Mpa,
secondary rectification: performing secondary rectification on the kettle liquid obtained by the primary rectification at the kettle temperature of 155 ℃, the top temperature of 135-,
the isophorone purification process comprises molecular distillation and vacuum rectification of reflux liquid,
molecular distillation: the organic phase obtained by alkalization and phase splitting enters molecular distillation equipment, reflux liquid and distillate are respectively obtained by molecular distillation,
vacuum rectification of the reflux: delivering reflux obtained by molecular distillation into a vacuum distillation tower to obtain a finished product with the mass content of isophorone being more than or equal to 98 percent under the conditions of tower kettle temperature of 145-148 ℃, tower top temperature of 105-107 ℃ and vacuum degree of-0.098 Mpa,
the purification process of the mesitylene and the mesitylene comprises the vacuum rectification of distillate,
vacuum rectification of the distillate: separating mesitylene from the distillate after molecular distillation by vacuum rectification under the conditions of tower still temperature not more than 110 ℃, tower top temperature 65-70 ℃ and vacuum degree-0.085 Mpa, and separating mesitylene from the distillate after molecular distillation under the conditions of tower still temperature not more than 130 ℃, tower top temperature not more than 105 ℃ and vacuum degree-0.085 Mpa.
In some embodiments, the multi-component phenol-containing mixture includes, in mass percent, 3.66% mesitylene, 5.25% mesitylene, 9.83% m-cresol, 6.55% isophorone, 68.9% 3, 5-dimethylphenol, 2.08% 3, 4-dimethylphenol, 3.73% other components.
In some embodiments, the secondary mother liquor has mass characteristic contents of: 8.75% of mesitylene, 12.55% of mesitylene, 23.51% of m-cresol, 15.65% of Isophorone (IP), 25.65% of 3, 5-dimethylphenol (MX), 4.97% of 3, 4-dimethylphenol and 8.92% of other components.
In some embodiments, the technological parameters of the decoloring and rectifying are that the temperature of a tower kettle is less than or equal to 130 ℃, the temperature of a tower top is less than or equal to 110 ℃, and the vacuum of a rectifying tower is-0.098 MPa.
In some embodiments, the mass content of the main component of the organic phase obtained by the alkalization phase separation is 19.43% of mesitylene, 27.87% of mesitylene, 34.76% of isophorone and 17.92% of other components.
In some embodiments, the water phase obtained from the acidification phase separation is returned to the dilute hydrochloric acid preparation section for reuse, and is sent to a sewage treatment device of an enterprise for desalination and biochemical treatment after repeated use.
In some embodiments, the mass content of the main components of the organic phase obtained by the acidification phase separation is: 42.76% of m-cresol, 46.65% of 3, 5-dimethylphenol, 9.04% of 3, 4-dimethylphenol and the balance of 1.55%.
In some embodiments, the main components of the still after the primary rectification have the mass contents of 81.5% of 3, 5-dimethylphenol, 15.8% of 3, 4-dimethylphenol and the other 2.7%.
In some embodiments, the crude product obtained by the second rectification and the crude product obtained by the crystallization purification enter a decoloring rectification tower together for purification again.
In some embodiments, the reflux comprises 66% isophorone and 44% other components by mass as the major components, and the distillate comprises 41% mesitylene and 59% mesitylene as the major components.
The beneficial effects are as follows: the method carries out efficient and clean deep treatment on a plurality of byproducts generated in the process of preparing the 3, 5-dimethylphenol by aromatizing the isophorone, can realize the maximization of the utilization rate of the raw materials, and has remarkable economic and social benefits. The invention sequentially separates and purifies the enriched multi-component phenol-containing mixture, realizes the high-efficiency utilization of the raw materials, and has the obvious characteristics of energy conservation and environmental protection.
Drawings
FIG. 1 is a schematic flow diagram of a process for the enrichment separation of a low-concentration multi-component phenol-containing mixture according to one embodiment of the present invention.
Detailed Description
In the process of preparing 3, 5-dimethylphenol by taking isophorone as a raw material, various byproducts such as 3, 4-dimethylphenol, m-cresol, mesitylene, and the like are generated, the products of the reaction can form a large amount of low-content multi-component mixture besides the 3, 5-dimethylphenol product after washing, decoking and crystallization respectively, and the substances separated by crystallization are called multi-component phenol-containing mixture collectively. The mixture will be crystallized at normal temperature, and can be dissolved completely when the temperature is raised to about 40 ℃, which is also commonly referred to as primary mother liquor in industry. The primary mother liquor or multi-component phenol-containing mixture referred to below refers to the above. The following components are all in percentage by mass.
The mass percentage content of the multi-component phenol-containing mixture is as follows: 3.66% of mesitylene, 5.25% of mesitylene, 9.83% of m-cresol, Isophorone (IP): 6.55 percent, 68.9 percent of 3, 5-dimethylphenol (MX), 2.08 percent of 3, 4-dimethylphenol and 3.73 percent of other components.
FIG. 1 schematically illustrates a process for the enrichment separation of a low-concentration multi-component mixture according to one embodiment of the present invention. As shown in fig. 1, the process for enriching and separating the low-concentration multi-component phenol-containing mixture comprises: 3, 5-dimethylphenol (MX) purification process, 3, 4-dimethylphenol and m-cresol purification process, Isophorone (IP) purification process, mesitylene and mesitylene purification process. The purification process of the 3, 5-dimethylphenol (MX) comprises crystallization purification and decoloration purification; the purification process of the 3, 4-dimethylphenol and the m-cresol comprises alkalization phase separation, acidification phase separation, primary rectification and secondary rectification; the Isophorone (IP) purification process includes molecular distillation; the mesitylene and mesitylene purifying process includes vacuum rectification.
3, 5-dimethylphenol (MX) purification Process: the process mainly comprises the steps of obtaining a 3, 5-dimethylphenol crude product through crystallization and rectification, and then obtaining a finished product of 3, 5-dimethylphenol (MX) through rectification and decoloration. Comprises the steps of carrying out crystallization and purification on a multi-component phenol-containing mixture to obtain a crude product and carrying out decoloration and rectification on the crude product obtained by crystallization and purification to obtain a finished product of 3, 5-dimethylphenol (MX).
And (3) crystallization and purification processes: taking a multi-component phenol-containing mixture as a raw material, using frozen brine as a refrigerant to reduce the temperature of the multi-component phenol-containing mixture from normal temperature to 0-1 ℃ at a speed of 5 ℃/h, and performing solid-liquid separation after the temperature reduction is finished to respectively obtain a solid crude product containing 96-98% of 3, 5-dimethylphenol and a liquid secondary mother liquor. The secondary mother liquor has the mass characteristic content as follows: 8.75% of mesitylene, 12.55% of mesitylene, 23.51% of m-cresol, 15.65% of Isophorone (IP), 25.65% of 3, 5-dimethylphenol (MX), 4.97% of 3, 4-dimethylphenol and 8.92% of other components.
Decoloring and purifying: since the 3, 5-dimethylphenol obtained by crystallization purification has poor color and luster, the decolorization treatment is needed, and the total content of the crude product does not meet the requirement of the finished product, the purity of the crude product needs to be further improved by rectification so as to meet the requirement of the finished product. Heating and melting the crude product obtained by self-crystallization purification, and then feeding the molten crude product into a decoloring and rectifying tower for secondary purification to obtain a finished product of 3, 5-dimethylphenol (MX) with the main content of more than or equal to 98 percent. The technological parameters of the decoloring and rectifying are that the temperature of a tower kettle is less than or equal to 130 ℃, the temperature of a tower top is less than or equal to 110 ℃, and the vacuum of a rectifying tower is-0.098 Mpa.
2. 3, 4-dimethylphenol and m-cresol purification process: and (3) firstly, dissolving sodium phenolate generated after the reaction of phenolic substances in the secondary mother liquor obtained by crystallization and purification in a water phase through alkalization phase splitting, and respectively obtaining the water phase and the organic phase through oil-water separation of other organic matters in the organic phase and then respectively treating the water phase and the organic phase.
The process mainly comprises the steps of alkalization phase splitting, acidification phase splitting, primary rectification and secondary rectification.
Alkalization and phase separation: the method takes 15% NaOH solution as an alkalizer to react with secondary mother liquor, and the reaction principle is that phenolic substances are in weak acidity and undergo neutralization reaction with NaOH to generate sodium phenolate and water, the sodium phenolate generated by the reaction can be dissolved in a water phase, and oil and water of the secondary mother liquor are separated. The alkalization process is carried out at normal temperature and normal pressure, the pH value of the water phase is controlled to be 9-10, and the water phase and the organic phase are obtained through an oil-water separator after alkalization is finished. The mass contents of the main components of the organic phase are 19.43 percent of mesitylene, 27.87 percent of mesitylene, 34.76 percent of isophorone and 17.92 percent of other components. The organic phase is subjected to molecular distillation, while the aqueous phase is subjected to an acidification phase separation process.
Acidifying and phase splitting: the sodium phenolate in the water phase is weak acid and strong base salt which can react with strong acid, and 15% hydrochloric acid solution and the water phase obtained from the last step of alkalization phase are subjected to acid-base neutralization reaction to generate phenolic substances and water. The phenols can float above the water phase, and the organic phase and the water phase are respectively obtained by separating through an oil-water separator. The organic phase is mainly that the crude phenols enter into primary rectification for purification, the water phase returns to the dilute hydrochloric acid preparation working section for reuse, and the water phase is sent into a sewage treatment device of an enterprise for desalination and biochemical treatment after repeated use. The mass content of the main components of the organic phase obtained by acidification and phase separation is as follows: 42.76% of m-cresol, 46.65% of 3, 5-dimethylphenol, 9.04% of 3, 4-dimethylphenol and the balance of 1.55%. The main control parameters are normal temperature and pressure, and the PH value of the reaction is 5-6.
Primary rectification and purification: the organic phase obtained by acidification and phase separation enters a primary rectifying tower kettle, and a finished product with the m-cresol content not less than 98 percent is obtained under the conditions that the tower kettle temperature is not higher than 130 ℃, the tower top temperature is not higher than 110 ℃ and the vacuum degree is-0.098 Mpa. Because the melting boiling point of the m-cresol is lower, the m-cresol is most easily separated and extracted during rectification, and the kettle liquid after primary rectification enters secondary rectification for secondary separation. The mass content of the main components of the primary rectified kettle liquid is 81.5 percent of 3, 5-dimethylphenol, 15.8 percent of 3, 4-dimethylphenol and 2.7 percent of others.
Secondary rectification and purification: and (3) rectifying the primary rectifying kettle liquid at the kettle temperature of 155 ℃, the top temperature of 135-. And the substance which is rich in the crude product of the 3, 4-dimethylphenol and obtained after the secondary purification is directly purified again in the tower kettle to obtain the finished product of the 3, 4-dimethylphenol. The secondary rectification purification process can finish the purification operation in a rectification tower, the rectification purification is intermittent operation, firstly, the crude product of the 3, 5-dimethylphenol is obtained by purification, and then, the qualified finished product of the 3, 4-dimethylphenol is obtained by continuous rectification.
Isophorone (IP) purification process: the organic phase obtained by alkalization and phase splitting enters molecular distillation, and the separation of substances is realized by utilizing the difference of the average free path of movement of molecules of the mesitylene, mesitylene and isophorone, and the process is mainly used for separating the mesitylene and the mesitylene from the organic phase system so as to facilitate the next separation. The molecular distillation equipment model is MK/FEEL-6.0, the vacuum degree is 0.13Pa, reflux liquid and distillate are respectively obtained through molecular distillation, the reflux liquid is also used for weighing components, and the distillate is also called as light components. The mass content of the main component of the reflux liquid is 66 percent of isophorone, and the mass content of the other components is 44 percent; the major components of the distillate were 41% and mesitylene 59%.
Because the components of the organic phase are particularly complex and have dozens of components, the purification of the components is difficult to realize by adopting the conventional rectification method, and therefore, a method which is different from the traditional separation method relying on the difference of boiling points is required to be adopted.
Vacuum rectification of the reflux: delivering reflux obtained by molecular distillation into a vacuum distillation tower to obtain a finished product with the mass content of isophorone being more than or equal to 98% under the conditions of tower kettle temperature of 145-148 ℃, tower top temperature of 105-107 ℃ and vacuum degree of-0.098 Mpa.
After the extraction of the isophorone is finished, continuously extracting an organic phase under the conditions of the kettle temperature of 155-. The high boiling point solvent has mixed components, mainly comprising some aromatic and ketone compounds.
The purification process of the mesitylene and the mesitylene comprises the following steps: the distillate obtained after molecular distillation is a relatively pure mixture of mesitylene and mesitylene. According to the characteristic that the difference between the boiling points of the two components is large, the components can be separated by the traditional vacuum rectification. The specific technological parameters of the isopropylidene acetone rectification process are that the temperature of a tower kettle is less than or equal to 110 ℃, the temperature of a tower top is 65-70 ℃, and the vacuum degree is-0.085 Mpa; the technological parameters of mesitylene rectification are tower still temperature not more than 130 deg.c, tower top temperature not more than 105 deg.c and vacuum degree-0.085 MPa. Vacuum rectification is carried out to respectively obtain two valuable components of finished products of mesitylene and mesitylene, wherein the mass content of the main components of the finished products is higher than 98%.
What has been described above are merely some embodiments of the present invention. It will be apparent to those skilled in the art that various changes and modifications can be made without departing from the inventive concept thereof, and these changes and modifications can be made without departing from the spirit and scope of the invention.
Claims (9)
1. A process for the enrichment separation of a low-concentration multi-component phenol-containing mixture, comprising, in order: a purification process of 3, 5-dimethylphenol, a purification process of 3, 4-dimethylphenol and m-cresol, a purification process of isophorone, a purification process of mesitylene and mesitylene,
the multi-component phenol-containing mixture comprises 3.66 percent of mesitylene, 5.25 percent of mesitylene, 9.83 percent of m-cresol, 6.55 percent of isophorone, 68.9 percent of 3, 5-dimethylphenol, 2.08 percent of 3, 4-dimethylphenol and 3.73 percent of other components according to mass percentage,
the purification process of the 3, 5-dimethylphenol comprises crystallization purification and decoloration rectification,
the crystallization purification takes a multi-component phenol-containing mixture as a raw material, takes frozen brine as a refrigerant to reduce the multi-component phenol-containing mixture from the normal temperature to 0-1 ℃ at the speed of 5 ℃/h, carries out solid-liquid separation after the temperature reduction is finished, respectively obtains a solid crude product and a secondary mother liquor of 3, 5-dimethylphenol with the mass content of 96-98 percent,
decoloring and rectifying: heating and melting the solid crude product obtained by self-crystallization purification, then feeding the solid crude product into a decoloring and rectifying tower for secondary purification to obtain a finished product with the mass content of 3, 5-dimethylphenol being more than or equal to 98 percent,
the purification process of the 3, 4-dimethylphenol and the m-cresol comprises alkalization phase separation, acidification phase separation, primary rectification and secondary rectification,
alkalization and phase separation: reacting with the secondary mother liquor at normal temperature by using 15% NaOH solution as an alkalizer to generate sodium phenolate dissolved in a water phase, respectively obtaining the water phase and an organic phase through an oil-water separator after the alkalization reaction is finished, controlling the pH value of the water phase to be 9-10,
acidifying and phase splitting: performing acid-base neutralization reaction on a 15% hydrochloric acid solution and the water phase obtained by the alkalization phase separation under normal temperature and pressure and at a reaction pH of 5-6 to generate phenolic substances and water, separating by an oil-water separator to respectively obtain an organic phase and a water phase,
primary rectification: the organic phase obtained by the acidification phase separation enters a primary rectifying tower kettle, and a finished product with the m-cresol content not less than 98 percent is extracted under the conditions that the tower kettle temperature is not higher than 130 ℃, the tower top temperature is not higher than 110 ℃ and the vacuum degree is-0.098 Mpa,
secondary rectification: the kettle liquid obtained by the primary rectification is subjected to secondary rectification under the conditions of the kettle temperature of 155 ℃, the top temperature of 135-,
the isophorone purification process comprises molecular distillation and vacuum rectification of reflux liquid,
molecular distillation: the organic phase obtained by alkalization and phase splitting enters molecular distillation equipment, reflux liquid and distillate are respectively obtained by molecular distillation,
vacuum rectification of the reflux: delivering reflux obtained by molecular distillation into a vacuum distillation tower to obtain a finished product with the mass content of isophorone being more than or equal to 98 percent under the conditions of tower kettle temperature of 145-148 ℃, tower top temperature of 105-107 ℃ and vacuum degree of-0.098 Mpa,
the purification process of the mesitylene and the mesitylene comprises the vacuum rectification of distillate,
vacuum rectification of the distillate: separating mesitylene from the distillate after molecular distillation by vacuum rectification under the conditions of tower still temperature not more than 110 ℃, tower top temperature 65-70 ℃ and vacuum degree-0.085 Mpa, and separating mesitylene from the distillate after molecular distillation under the conditions of tower still temperature not more than 130 ℃, tower top temperature not more than 105 ℃ and vacuum degree-0.085 Mpa.
2. The process of claim 1, wherein the secondary mother liquor comprises the following mass characteristic contents: 8.75% of mesitylene, 12.55% of mesitylene, 23.51% of m-cresol, 15.65% of isophorone, 25.65% of 3, 5-dimethylphenol, 4.97% of 3, 4-dimethylphenol and 8.92% of other components.
3. The process of claim 1, wherein the decolorization and rectification process is carried out at a temperature of 130 ℃ or less at the bottom of the column, 110 ℃ or less at the top of the column, and-0.098 MPa in vacuum in the rectification column.
4. The process according to claim 1, wherein the organic phase obtained from the alkalized phase separation has a main component content of 19.43% by mass of mesitylene, 27.87% by mass of mesitylene, 34.76% by mass of isophorone and 17.92% by mass of other components.
5. The process for enriching and separating a low-concentration multi-component phenol-containing mixture according to claim 1, wherein the aqueous phase obtained from the acidification phase separation is returned to a dilute hydrochloric acid preparation section for reuse, and is sent to a sewage treatment device of an enterprise for desalination and biochemical treatment after being reused for multiple times.
6. The process for the enrichment and separation of a low-concentration multi-component phenol-containing mixture according to claim 1, wherein the mass content of the main components of the organic phase obtained from the acidification phase separation is: 42.76% of m-cresol, 46.65% of 3, 5-dimethylphenol, 9.04% of 3, 4-dimethylphenol and the balance of 1.55%.
7. The process for the enrichment and separation of a low-concentration multi-component phenol-containing mixture according to claim 1, wherein the mass content of the main components of the still after the primary rectification is 81.5% of 3, 5-dimethylphenol, 15.8% of 3, 4-dimethylphenol and 2.7% of the others.
8. The process for the enrichment and separation of a low-concentration multi-component phenol-containing mixture according to claim 1, wherein the crude product obtained by the secondary distillation and the crude product obtained by the crystallization and purification are fed into a decoloring and rectifying tower for secondary purification.
9. The process according to claim 1, wherein the reflux comprises 66% by mass of isophorone and 44% by mass of other components, and the distillate comprises 41% by mass of mesitylene and 59% by mass of mesitylene.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810547922.2A CN108947777B (en) | 2018-05-31 | 2018-05-31 | Enrichment and separation process of low-concentration multi-component phenol-containing mixture |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810547922.2A CN108947777B (en) | 2018-05-31 | 2018-05-31 | Enrichment and separation process of low-concentration multi-component phenol-containing mixture |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108947777A CN108947777A (en) | 2018-12-07 |
| CN108947777B true CN108947777B (en) | 2021-09-10 |
Family
ID=64492456
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810547922.2A Active CN108947777B (en) | 2018-05-31 | 2018-05-31 | Enrichment and separation process of low-concentration multi-component phenol-containing mixture |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108947777B (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102417248A (en) * | 2010-09-27 | 2012-04-18 | 新奥科技发展有限公司 | Method for processing and recycling waste water containing phenolic compounds |
| CN104151143A (en) * | 2014-07-24 | 2014-11-19 | 连云港科铭化工有限公司 | Paracresol production crude distillation residue recovery treatment method |
| CN104230669A (en) * | 2014-09-11 | 2014-12-24 | 苏州飞翔新材料研究院有限公司 | Separation and purification method of m-cresol |
| CN107573227A (en) * | 2017-08-30 | 2018-01-12 | 中国石油大学(华东) | Acetone vapour phase condensation prepares the device and method of isophorone |
| CN107721826A (en) * | 2017-10-27 | 2018-02-23 | 陕西煤业化工集团神木天元化工有限公司 | The method and device of a variety of phenol is separated in a kind of therefrom coalite tar crude phenols |
-
2018
- 2018-05-31 CN CN201810547922.2A patent/CN108947777B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102417248A (en) * | 2010-09-27 | 2012-04-18 | 新奥科技发展有限公司 | Method for processing and recycling waste water containing phenolic compounds |
| CN104151143A (en) * | 2014-07-24 | 2014-11-19 | 连云港科铭化工有限公司 | Paracresol production crude distillation residue recovery treatment method |
| CN104230669A (en) * | 2014-09-11 | 2014-12-24 | 苏州飞翔新材料研究院有限公司 | Separation and purification method of m-cresol |
| CN107573227A (en) * | 2017-08-30 | 2018-01-12 | 中国石油大学(华东) | Acetone vapour phase condensation prepares the device and method of isophorone |
| CN107721826A (en) * | 2017-10-27 | 2018-02-23 | 陕西煤业化工集团神木天元化工有限公司 | The method and device of a variety of phenol is separated in a kind of therefrom coalite tar crude phenols |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108947777A (en) | 2018-12-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP1845079B1 (en) | Method for manufacturing aniline | |
| DE10329304A1 (en) | Process for working up the wastewater produced during the production of dinitrotoluene | |
| CN102241606B (en) | Clean production method of N-cyanoethylaniline | |
| EP3374347B1 (en) | Process for reprocessing alkane sulfonic acid | |
| EP2989078B1 (en) | Method for the preparation of di- and polyamines of the diphenyl methane series | |
| EP2028176A1 (en) | Method for purifying aromatic amines | |
| CN108558609A (en) | A kind of polyphenol mixture recycling purifying technique | |
| CN101928205B (en) | Method for compositely extracting, rectifying and separating chlorophenol-parachlorophenol mixed system | |
| CN108947777B (en) | Enrichment and separation process of low-concentration multi-component phenol-containing mixture | |
| CN103772185B (en) | Device and method for removing moisture and heteroacids in acetic acid | |
| CN106008186A (en) | Method for separating acetone, isopropanol and water mixed solution | |
| EP2828233B1 (en) | Method for cleaning aniline from gas phase hydrogenation | |
| CN109704908B (en) | Method for preparing hexane from aromatic raffinate oil | |
| CN106008160A (en) | Glycine discharging mother solution treating technology | |
| CN102527072A (en) | Batch extraction distillation separation method for propyl alcohol-propyl formate azeotropic mixture | |
| EP3941894B1 (en) | Process to recover 3-methyl-but-3-en-1-ol | |
| US5811598A (en) | Process for the recovery of phenol from an aqueous stream containing NA.sub. SO4 | |
| CN101062886A (en) | Method for extracting 3,5-dimethylphenol from coal tar | |
| EP0021211B1 (en) | Process for the preparation of dimethyl carbonate | |
| US7416645B2 (en) | Continuous process for recovering acetone from a waste stream resulting from acetone purification | |
| CN105175260A (en) | DL-sec-butyl acetate-isobutanol azeotropic mixture continuous extraction rectification separation method | |
| US20240124328A1 (en) | Method for purifying brine generated in aromatic compound producing process | |
| RU2782625C1 (en) | Method for isolation of cyclohexanone from reaction mixture of cyclohexene oxidation in aqueous medium of n-methyl-2-pyrrolidone | |
| EP1188737A1 (en) | Process for treating material streams comprising mesityloxide | |
| CN217612990U (en) | Reflux water replenishing system of azeotropic distillation tower in acetic acid recovery process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |