CN115557825B - Method for separating high-purity mesitylene from reformed carbon nine by utilizing composite solvent - Google Patents
Method for separating high-purity mesitylene from reformed carbon nine by utilizing composite solvent Download PDFInfo
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- CN115557825B CN115557825B CN202211308916.4A CN202211308916A CN115557825B CN 115557825 B CN115557825 B CN 115557825B CN 202211308916 A CN202211308916 A CN 202211308916A CN 115557825 B CN115557825 B CN 115557825B
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- 239000002904 solvent Substances 0.000 title claims abstract description 134
- AUHZEENZYGFFBQ-UHFFFAOYSA-N mesitylene Substances CC1=CC(C)=CC(C)=C1 AUHZEENZYGFFBQ-UHFFFAOYSA-N 0.000 title claims abstract description 91
- 125000001827 mesitylenyl group Chemical group [H]C1=C(C(*)=C(C([H])=C1C([H])([H])[H])C([H])([H])[H])C([H])([H])[H] 0.000 title claims abstract description 91
- 239000002131 composite material Substances 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 38
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 22
- 239000000463 material Substances 0.000 claims abstract description 79
- 238000000605 extraction Methods 0.000 claims abstract description 39
- HYFLWBNQFMXCPA-UHFFFAOYSA-N 1-ethyl-2-methylbenzene Chemical compound CCC1=CC=CC=C1C HYFLWBNQFMXCPA-UHFFFAOYSA-N 0.000 claims description 31
- NXXYKOUNUYWIHA-UHFFFAOYSA-N 2,6-Dimethylphenol Chemical compound CC1=CC=CC(C)=C1O NXXYKOUNUYWIHA-UHFFFAOYSA-N 0.000 claims description 30
- 239000000203 mixture Substances 0.000 claims description 25
- 238000010992 reflux Methods 0.000 claims description 16
- XKEFYDZQGKAQCN-UHFFFAOYSA-N 1,3,5-trichlorobenzene Chemical compound ClC1=CC(Cl)=CC(Cl)=C1 XKEFYDZQGKAQCN-UHFFFAOYSA-N 0.000 claims description 15
- 238000000895 extractive distillation Methods 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 12
- 150000001875 compounds Chemical class 0.000 claims description 9
- 238000004064 recycling Methods 0.000 claims description 3
- 230000000295 complement effect Effects 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 4
- GWHJZXXIDMPWGX-UHFFFAOYSA-N 1,2,4-trimethylbenzene Chemical compound CC1=CC=C(C)C(C)=C1 GWHJZXXIDMPWGX-UHFFFAOYSA-N 0.000 description 14
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 9
- 238000003795 desorption Methods 0.000 description 9
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 6
- 238000009835 boiling Methods 0.000 description 5
- 238000011084 recovery Methods 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- FYGHSUNMUKGBRK-UHFFFAOYSA-N 1,2,3-trimethylbenzene Chemical compound CC1=CC=CC(C)=C1C FYGHSUNMUKGBRK-UHFFFAOYSA-N 0.000 description 2
- JRLPEMVDPFPYPJ-UHFFFAOYSA-N 1-ethyl-4-methylbenzene Chemical compound CCC1=CC=C(C)C=C1 JRLPEMVDPFPYPJ-UHFFFAOYSA-N 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- 125000003118 aryl group Chemical group 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- 230000006978 adaptation Effects 0.000 description 1
- 229910052936 alkali metal sulfate Inorganic materials 0.000 description 1
- -1 alkyl aromatic hydrocarbon Chemical class 0.000 description 1
- 229940100198 alkylating agent Drugs 0.000 description 1
- 239000002168 alkylating agent Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910001510 metal chloride Inorganic materials 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000000066 reactive distillation Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- NBRKLOOSMBRFMH-UHFFFAOYSA-N tert-butyl chloride Chemical compound CC(C)(C)Cl NBRKLOOSMBRFMH-UHFFFAOYSA-N 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- 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
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
- C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- 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 a method for separating high-purity mesitylene from reformed carbon nine by utilizing a composite solvent, which has the following advantages compared with the prior art: (1) The components in the composite solvent adopted by the invention are cheap and easy to obtain, and the cost of the solvent is greatly reduced. (2) The composite solvent adopted by the invention has good extraction effect and selectivity on mesitylene, reduces the solvent ratio, and greatly reduces the running cost and the fixed investment; meanwhile, the yield of the mesitylene reaches more than 96 percent, and the purity of the mesitylene reaches more than 99 percent (mass percent). (3) When the concentration of mesitylene in the material to be separated is higher, the content is more than or equal to 70 percent (mass percent), and the process is particularly suitable for saving energy consumption.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to a method for separating high-purity mesitylene from reformed carbon nine by using a composite solvent.
Background
In recent years, with the progress of petroleum processing technology, the yield of reformed C9 aromatics in catalytic reformers has been increasing. And the hemimellitene, the pseudocumene, the mesitylene and the like are separated from the reformed C9 aromatic hydrocarbon, so that the method has very important practical significance for developing and utilizing the reformed C9 aromatic hydrocarbon resources, conforming to the development strategy that petrochemical products are to be extended towards the middle and downstream, and improving the economic benefit. However, because the content of mesitylene in the reformed C9 aromatic hydrocarbon is not high, and is generally 6-16% wt, the boiling points of all components in the C9 aromatic hydrocarbon are very close, and particularly, the boiling points of o-methyl ethylbenzene (165.2 ℃) and mesitylene (164.7 ℃) are only 0.5 ℃ different, the relative volatility is 1.009, and the high-purity mesitylene is extremely difficult to obtain by a common rectification separation method.
Current methods for separating mesitylene from reformed C9 are: separating by reactive distillation, firstly using tert-butyl chloride as an alkylating agent and metal chloride as a catalyst, converting o-, m-, p-methyl ethylbenzene and pseudocumene in C9 aromatic hydrocarbon into alkyl aromatic hydrocarbon with high boiling point, and then rectifying to obtain the mesitylene with the purity of 98%.
For example, chinese patent CN1513818 discloses a process for separating C9 aromatic hydrocarbons by combining rectification and extraction in a staggered manner, wherein the separation steps in the process are as follows: the C9 aromatic hydrocarbon enters a rectifying tower, the temperature of the tower top is controlled to be less than or equal to 162.5 ℃, the distillate at the tower top is light C9, and the boiling range of the tower bottom is heavy C9 with the boiling range of more than 162.5 ℃; the heavy C9 enters an extraction tower, more than 89% of p-methyl ethyl benzene can be obtained at the top of the extraction tower, and the tower bottom is mixed liquid; feeding the tower kettle mixed solution into a regeneration tower for treatment; the distillate at the top of the regeneration tower is a mixed solution of mesitylene, o-methyl ethylbenzene and pseudocumene, and enters a second rectifying tower, and the extractant at the bottom of the second rectifying tower is recycled; the distillate at the top of the second rectifying tower is mixed liquor rich in mesitylene, o-methyl ethylbenzene and trace amount of mesitylene, and the bottom of the second rectifying tower is mixed liquor rich in more than 83% of mesitylene; the distillate at the top of the second rectifying tower enters a third rectifying tower, and is extracted to obtain more than 98.5 percent mesitylene; the mixed liquid at the bottom of the tower is treated in a regeneration tower, more than 88% of o-methyl ethylbenzene is distilled from the top of the regeneration tower, and the solvent at the bottom of the tower is recycled.
The existing high-purity mesitylene production process has the following problems: 1. the reformed carbon nine contains 0.5-5% of non-aromatic components, a small amount of light non-aromatic components cannot be removed through common rectification and extractive rectification, the purity of mesitylene is seriously influenced, and the purity cannot reach more than 99%; 2. the process for producing the mesitylene by an isomerization method has low yield and insufficient purity of the final mesitylene, and influences downstream use; 3. the enrichment of the sym-trialkylation method has the advantages of total yield and purity of mesitylene, but the catalyst used in the process is toxic and easy to pollute the environment; 4. the extraction and rectification process has poor single solvent extraction effect, so that the yield of mesitylene is low; the extractant energy consumption in the solvent recovery process is excessive.
Disclosure of Invention
The invention aims to provide a method for separating high-purity mesitylene from reformed carbon nine by utilizing a composite solvent, wherein the composite solvent has good selectivity to the mesitylene, the relative volatility between the mesitylene and o-methyl-ethylbenzene is increased, the circulation quantity of the solvent is reduced, the energy consumption and the fixed investment of a device are reduced, the yield of the mesitylene reaches more than 96%, and the purity reaches 99%.
The invention provides a method for separating high-purity mesitylene from reformed carbon nine by utilizing a composite solvent, which comprises the following steps:
A) Removing light components and heavy components from the reformed carbon nine raw materials to obtain a material flow 1 with the total mass fraction of mesitylene and o-methyl ethylbenzene being more than or equal to 98%;
b) The material flow 1 enters an extraction rectifying tower from the middle lower part, the composite solvent material flow 2 enters an extraction rectifying tower I from the middle upper part, the mesitylene is subjected to extraction rectification, a mixed material flow 3 of o-methyl ethylbenzene and a trace amount of composite solvent is obtained at the tower top, and a mixed material flow 4 of mesitylene and the composite solvent is obtained at the tower bottom;
the compound solvent is a mixture of 1,3, 5-trichlorobenzene and 2, 6-xylenol, and the mass ratio of the 1,3, 5-trichlorobenzene to the 2, 6-xylenol is (80-90): (20-10);
C) The material flow 4 enters a solvent resolving tower from the middle lower part, a mesitylene material flow 5 is obtained at the top of the tower, and a resolved composite solvent material flow 6 is obtained at the bottom of the tower.
Preferably, the theoretical plate number of the extractive distillation column is 60 to 200.
Preferably, the feed temperature of the complex solvent stream 2 is 70-100 ℃.
Preferably, the temperature of the tower bottom of the extraction rectifying tower is 140-180 ℃, the temperature of the tower top is 90-170 ℃, and the operating pressure is 10-90 KPa.
Preferably, the reflux ratio of the extractive distillation column is 1.4-5.
Preferably, the mass ratio of the composite solvent stream 2 to the stream 1 is (2-12): 1.
Preferably, the theoretical plate number of the solvent-resolving tower is 30 to 80.
Preferably, the temperature of the tower bottom of the solvent resolving tower is 160-210 ℃, the temperature of the tower top is 80-160 ℃, and the operating pressure is 5-105 KPa.
Preferably, the reflux ratio of the solvent-resolving tower is 1 to 3.5.
Preferably, the composite solvent stream 6 is mixed with the complementary composite solvent stream 2 for recycling after being cooled down.
The invention provides a method for separating high-purity mesitylene from reformed carbon nine by utilizing a composite solvent, which comprises the following steps: a) Removing light components and heavy components from the reformed carbon nine raw materials to obtain a material flow 1 with the total mass fraction of mesitylene and o-methyl ethylbenzene being more than or equal to 98%; b) The material flow 1 enters an extraction rectifying tower from the middle lower part, the composite solvent material flow 2 enters an extraction rectifying tower I from the middle upper part, the mesitylene is subjected to extraction rectification, a mixed material flow 3 of o-methyl ethylbenzene and a trace amount of composite solvent is obtained at the tower top, and a mixed material flow 4 of mesitylene and the composite solvent is obtained at the tower bottom; the compound solvent is a mixture of 1,3, 5-trichlorobenzene and 2, 6-xylenol, and the mass ratio of the 1,3, 5-trichlorobenzene to the 2, 6-xylenol is (80-90): (20-10); c) The material flow 4 enters a solvent resolving tower from the middle lower part, a mesitylene material flow 5 is obtained at the top of the tower, and a resolved composite solvent material flow 6 is obtained at the bottom of the tower.
Compared with the prior art, the invention has the following advantages:
(1) The components in the composite solvent adopted by the invention are cheap and easy to obtain, and the cost of the solvent is greatly reduced.
(2) The composite solvent adopted by the invention has good extraction effect and selectivity on mesitylene, reduces the solvent ratio, and greatly reduces the running cost and the fixed investment; meanwhile, the yield of the mesitylene reaches more than 96 percent, and the purity of the mesitylene reaches more than 99 percent (mass percent).
(3) When the concentration of mesitylene in the material to be separated is higher, the content is more than or equal to 70 percent (mass percent), and the process is particularly suitable for saving energy consumption.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings that are required to be used in the embodiments or the description of the prior art will be briefly described below, and it is obvious that the drawings in the following description are only embodiments of the present invention, and that other drawings can be obtained according to the provided drawings without inventive effort for a person skilled in the art.
FIG. 1 is a process flow diagram of the present invention;
Wherein I is an extraction rectifying tower, II is a solvent resolving tower, and III is a solvent cooler; 1-6 represent streams 1-6, respectively.
Detailed Description
The invention provides a method for separating high-purity mesitylene from reformed carbon nine by utilizing a composite solvent, which comprises the following steps:
A) Removing light components and heavy components from the reformed carbon nine raw materials to obtain a material flow 1 with the total mass fraction of mesitylene and o-methyl ethylbenzene being more than or equal to 98%;
b) The material flow 1 enters an extraction rectifying tower from the middle lower part, the composite solvent material flow 2 enters an extraction rectifying tower I from the middle upper part, the mesitylene is subjected to extraction rectification, a mixed material flow 3 of o-methyl ethylbenzene and a trace amount of composite solvent is obtained at the tower top, and a mixed material flow 4 of mesitylene and the composite solvent is obtained at the tower bottom;
the compound solvent is a mixture of 1,3, 5-trichlorobenzene and 2, 6-xylenol, and the mass ratio of the 1,3, 5-trichlorobenzene to the 2, 6-xylenol is (80-90): (20-10);
C) The material flow 4 enters a solvent resolving tower from the middle lower part, a mesitylene material flow 5 is obtained at the top of the tower, and a resolved composite solvent material flow 6 is obtained at the bottom of the tower.
The source of the reformed carbon nine raw material is not particularly limited, and reformed carbon nine raw materials commonly used by those skilled in the art may be used. In the present invention, the methods for removing light components and heavy components are all common methods for those skilled in the art, and the present invention is not described herein.
In the present invention, the complex solvent is preferably a mixture of 1,3, 5-trichlorobenzene and 2, 6-xylenol, and the mass ratio of 1,3, 5-trichlorobenzene to 2, 6-xylenol is preferably (80 to 90): (20 to 10), more preferably (82 to 88): (18-12), such as 80:20, 81:19, 82:18, 83:17, 84:16, 85:15, 86:14, 87:13, 88:12, 89:11, 90:10, preferably a range value having any of the above values as an upper limit or a lower limit.
In the present invention, the feed temperature of the complex solvent stream 2 is preferably 70 to 100 ℃, more preferably 80 to 90 ℃, such as 70 ℃,75 ℃,0 ℃,85 ℃,90 ℃,95 ℃,100 ℃, preferably in a range having any of the above values as an upper or lower limit. The mass ratio of the compound solvent stream 2 to the stream 1 is preferably (2-12): 1, more preferably (5 to 10): 1, such as 2:1,3:1,4:1,5:1,6:1,7:1,8:1,9:1,10: 1,11: 1,12: 1, preferably a range value having any of the above values as an upper limit or a lower limit.
In the present invention, the theoretical plate number of the extractive distillation column is preferably 60 to 200, more preferably 100 to 180, such as 60, 70, 80, 90, 100, 110, 120, 130, 140, 150, 160, 170, 180, 190, 200, preferably a range value having any of the above values as an upper limit or a lower limit; the temperature of the tower kettle is preferably 140-180 ℃, more preferably 150-170 ℃, such as 140 ℃,145 ℃,150 ℃,155 ℃,160 ℃,165 ℃,170 ℃,175 ℃,180 ℃, preferably a range value with any of the above values as an upper limit or a lower limit; the temperature of the tower top is preferably 90-170 ℃, more preferably 100-150 ℃, such as 90 ℃,95 ℃,100 ℃,105 ℃,110 ℃,115 ℃,120 ℃,125 ℃,130 ℃,135 ℃,140 ℃,145 ℃,150 ℃,155 ℃,160 ℃,165 ℃,170 ℃, preferably ranges from any of the above values as upper or lower limits; the reflux ratio of the extractive distillation column is preferably 1.4 to 5, more preferably 2 to 4, and for example 1.4,1.5,1.6,1.7,1.8,1.9,2,2.1,2.2,2.3,2.4,2.5,2.6,2.7,2.8,2.9,3,3.1,3.2,3.3,3.4,3.5,3.6,3.7,3.8,3.9,4,4.1,4.2,4.3,4.4,4.5,4.6,4.7,4.8,4.9,5,, the reflux ratio is preferably a range value having any of the above values as an upper limit or a lower limit; the operating pressure is preferably 10 to 90KPa, more preferably 20 to 80KPa, such as 10KPa,20KPa,30KPa,40KPa,50KPa,60KPa,70KPa,80KPa,90KPa, preferably a range of values having any of the above values as an upper or lower limit.
In the present invention, the theoretical plate number of the solvent-resolving column is preferably 30 to 80, more preferably 40 to 70, such as 30, 35, 40, 45, 50, 55, 60, 65, 70, 75, 80, preferably a range value having any of the above values as an upper limit or a lower limit; the temperature of the tower kettle is preferably 160-210 ℃, more preferably 170-200 ℃, such as 160 ℃,165 ℃,170 ℃,175 ℃,180 ℃,185 ℃,190 ℃,195 ℃,200 ℃,205 ℃,210 ℃, and preferably ranges from any of the above values to the upper or lower limit; the temperature of the tower top is preferably 80-160 ℃, more preferably 100-150 ℃, such as 80 ℃,85 ℃,90 ℃,95 ℃,100 ℃,105 ℃,110 ℃,115 ℃,120 ℃,125 ℃,130 ℃,135 ℃,140 ℃,145 ℃,150 ℃,155 ℃,160 ℃, preferably ranges from any of the above values as upper or lower limits; the reflux ratio is preferably 1 to 3.5, more preferably 2 to 3, such as 1,1.1,1.2,1.3,1.4,1.5,1.6,1.7,1.8,1.9,2,2.1,2.2,2.3,2.4,2.5,2.6,2.7,2.8,2.9,3, preferably a range value having any of the above values as an upper limit or a lower limit; the operating pressure is preferably 5 to 105KPa, more preferably 10 to 100KPa, and for example 5KPa,10KPa,15KPa,20KPa,25KPa,30KPa,35KPa,40KPa,45KPa,50KPa,55KPa,60KPa,65KPa,70KPa,75KPa,80KPa,85KPa,90KPa,95KPa,100KPa,105KPa,, the range of any of the above values is preferably the upper or lower limit.
The composite solvent material flow 6 obtained from the tower kettle is cooled by a cooler, and then is mixed with the composite solvent material flow 2 to enter the middle upper part of the extraction rectifying tower for recycling.
The invention provides a method for separating high-purity mesitylene from reformed carbon nine by utilizing a composite solvent, which comprises the following steps: a) Removing light components and heavy components from the reformed carbon nine raw materials to obtain a material flow 1 with the total mass fraction of mesitylene and o-methyl ethylbenzene being more than or equal to 98%; b) The material flow 1 enters an extraction rectifying tower from the middle lower part, the composite solvent material flow 2 enters an extraction rectifying tower I from the middle upper part, the mesitylene is subjected to extraction rectification, a mixed material flow 3 of o-methyl ethylbenzene and a trace amount of composite solvent is obtained at the tower top, and a mixed material flow 4 of mesitylene and the composite solvent is obtained at the tower bottom; the compound solvent is a mixture of 1,3, 5-trichlorobenzene and 2, 6-xylenol, and the mass ratio of the 1,3, 5-trichlorobenzene to the 2, 6-xylenol is (80-90): (20-10); c) The material flow 4 enters a solvent resolving tower from the middle lower part, a mesitylene material flow 5 is obtained at the top of the tower, and a resolved composite solvent material flow 6 is obtained at the bottom of the tower.
Compared with the prior art, the invention has the following advantages:
(1) The components in the composite solvent adopted by the invention are cheap and easy to obtain, and the cost of the solvent is greatly reduced.
(2) The composite solvent adopted by the invention has good extraction effect and selectivity on mesitylene, reduces the solvent ratio, and greatly reduces the running cost and the fixed investment; meanwhile, the yield of the mesitylene reaches more than 96 percent, and the purity of the mesitylene reaches more than 99 percent (mass percent).
(3) When the concentration of mesitylene in the material to be separated is higher, the content is more than or equal to 70 percent (mass percent), and the process is particularly suitable for saving energy consumption.
In order to further illustrate the present invention, a method for separating high purity mesitylene from reformed carbon nine using a complex solvent is described in detail below with reference to examples, but should not be construed as limiting the scope of the present invention.
Example 1
According to the process flow of FIG. 1, a mixture of 1,3, 5-trichlorobenzene and 2, 6-xylenol is adopted as a composite solvent, wherein the mass percentage ratio is as follows: 80%:20%.
(1) Firstly, the mesitylene and the o-methyl ethylbenzene to be separated are subjected to light and heavy removal in a common rectification mode, the total mass percentage of the mesitylene and the o-methyl ethylbenzene is more than or equal to 98 percent, the mesitylene and the o-methyl ethylbenzene are recorded as a material flow 1, the material flow enters a tower I from the middle lower part, and the composite solvent 2 enters the tower I from the middle upper part for extraction rectification. Obtaining a mixed material flow 3 of o-methyl ethylbenzene and a small amount of composite solvent at the top of the tower, and obtaining a mixed material flow 4 of mesitylene and the composite solvent at the bottom of the tower;
(2) The mixed material flow 4 of the compound solvent and the mesitylene enters a solvent desorption tower II from the middle part, a mixed material flow 5 of the mesitylene and a small amount of solvent is obtained at the top of the solvent desorption tower, and a desorbed solvent material flow 6 is obtained at the bottom of the solvent desorption tower;
(3) The desorbed solvent material flow 6 is mixed with the composite solvent material flow 2 after being cooled by the solvent cooler III, and is recycled to enter the middle upper part of the extraction rectifying tower I.
In the above-described flow, the operation conditions of each operation unit are as follows:
(1) Operating conditions of extractive distillation column I: the theoretical plate number is 150, the feeding temperature of the composite solvent material flow 2 is 75 ℃, the tower bottom temperature is 178.4 ℃, the tower top temperature is 102.9 ℃, the reflux ratio is 2.7, the operating pressure is 65KPa, and the mass ratio of the solvent 2 to the material flow 1 to be separated is 4;
(2) Operating conditions of solvent desorber II: the theoretical plate number is 50, the tower bottom temperature is 183.2 ℃, the tower top temperature is 137.6 ℃, the reflux ratio is 3.2, and the operating pressure is 74KPa;
the yield of mesitylene is 96.6% and the purity reaches 99.49% (mass percent) by combining the flow chart of figure 1.
TABLE 1 raw material composition and product quality
Example 2
According to the process flow of FIG. 1, a mixture of 1,3, 5-trichlorobenzene and 2, 6-xylenol is adopted as a composite solvent, wherein the mass percentage ratio is as follows: 85%:15%.
(1) Firstly, the mesitylene and the o-methyl ethylbenzene to be separated are subjected to light and heavy removal in a common rectification mode, the total mass percent of the mesitylene and the o-methyl ethylbenzene in a material flow 1 is more than or equal to 98 percent, the mesitylene and the o-methyl ethylbenzene enter a tower I from a 90 th theoretical plate (1-180 pieces from top to bottom), a composite solvent 2 enters the tower I from a 5 th theoretical plate, extraction rectification is carried out, a mixture flow 3 of the o-methyl ethylbenzene and a small amount of solvent is obtained at the tower top, and a mixture flow 4 of the mesitylene and the composite solvent is obtained at the tower bottom;
(2) The mixed material flow 4 of the compound solvent and the mesitylene enters a solvent desorption tower II from the middle part, a mixed material flow 5 of the mesitylene and a small amount of solvent is obtained at the top of the solvent desorption tower, and a desorbed solvent material flow 6 is obtained at the bottom of the solvent desorption tower;
(3) The desorbed solvent material flow 6 is mixed with the composite solvent material flow 2 after being cooled by the solvent cooler VI, and is recycled to enter the middle upper part of the extraction rectifying tower I.
In the above-described flow, the operation conditions of each operation unit are as follows:
(1) Operating conditions of extractive distillation column I: the theoretical plate number is 180, the feeding temperature of the solvent material flow 2 is 95 ℃, the tower bottom temperature is 167.2 ℃, the tower top temperature is 100.9 ℃, the reflux ratio is 2.8, the operating pressure is 78KPa, and the mass ratio of the solvent material flow 2 to the material flow 1 to be separated is 6;
(2) Operating conditions of solvent desorber II: the theoretical plate number is 80, the tower bottom temperature is 197.2 ℃, the tower top temperature is 155.6 ℃, the reflux ratio is 3.1, and the operating pressure is 80KPa;
the yield of mesitylene is 97.2% and the purity reaches 99.36% (mass percent) by combining the flow chart of the figure 1.
TABLE 2 composition of raw materials and quality of products
Example 3
According to the process flow of FIG. 1, a mixture of 1,3, 5-trichlorobenzene and 2, 6-xylenol is adopted as a composite solvent, wherein the mass percentage ratio is as follows: 90% >: 10%.
(1) Firstly, the mesitylene and the o-methyl ethylbenzene to be separated are subjected to light and heavy removal in a common rectification mode, the total mass percent of the mesitylene and the o-methyl ethylbenzene is more than or equal to 98 percent, the flow 1 is recorded, the 60 th theoretical plates (1-140 from top to bottom) enter a tower I, and the composite solvent 2 enters the tower I from the 7 th theoretical plates for extraction and rectification. Obtaining a mixed material flow 3 of o-methyl ethylbenzene and a small amount of composite solvent at the top of the tower, and obtaining a mixed material flow 4 of mesitylene and the composite solvent at the bottom of the tower;
(2) The mixed material flow 4 of the compound solvent and the mesitylene enters a solvent desorption tower II from the middle part, a mixed material flow 5 of the mesitylene and a small amount of solvent is obtained at the top of the solvent desorption tower, and a desorbed solvent material flow 6 is obtained at the bottom of the solvent desorption tower;
(3) The desorbed solvent material flow 6 is mixed with the composite solvent material flow 2 after being cooled by the solvent cooler VI, and is recycled to enter the middle upper part of the extraction rectifying tower I.
In the above-described flow, the operation conditions of each operation unit are as follows:
(1) Operating conditions of extractive distillation column I: the theoretical plate number is 140, the feeding temperature of the solvent material flow 2 is 100 ℃, the tower bottom temperature is 156.6 ℃, the tower top temperature is 87.8 ℃, the reflux ratio is 3.1, the operating pressure is 50KPa, and the mass ratio of the solvent material flow 2 to the material flow 1 to be separated is 8;
(2) Operating conditions of solvent desorber II: the theoretical plate number is 70, the tower bottom temperature is 160 ℃, the tower top temperature is 86.5 ℃, the reflux ratio is 2.8, and the operating pressure is 50KPa;
The yield of mesitylene is 97.5% and the purity reaches 99.32% (mass percent) by combining the flow chart of the figure 1.
TABLE 3 composition of raw materials and quality of products
Comparative example 1
This comparative example 1 is example 10 of patent CN102924212a, using extractive distillation, with the solvent being a complex solvent comprising N-methyl-2-pyrrolidone and alkali metal sulfate.
The raw materials used are a mixture of carbon nine aromatic hydrocarbons with light components removed, wherein the mixture contains 35.10 weight percent of mesitylene, and the extractive distillation solvent adopts a solvent composition which comprises 93 parts by weight of N-methyl-2-pyrrolidone and 7 parts by weight of sodium sulfate.
The mixture of the light component removed carbon nine aromatic hydrocarbon enters the middle lower part of a pseudocumene column, enriched fractions containing mesitylene and part of methyl ethylbenzene are discharged from the top of the pseudocumene column, a material flow mainly containing mesitylene is led out from the bottom of the pseudocumene column, the column plate number of the pseudocumene column is 85, the reflux ratio is 15, the top temperature is 165 ℃, and the temperature of the kettle is 188.3 ℃. The enriched fraction containing mesitylene and part of methyl ethylbenzene flowing out from the top of the meta-trimethyl benzene tower enters the middle lower part of the extraction rectifying tower, the circulating solvent composition enters the extraction rectifying tower from the upper part, the tower plate number of the extraction rectifying tower is 95, the reflux ratio is 4, the top temperature is 164 ℃, the kettle temperature is 204.1 ℃, the purity of the mesitylene at the top of the tower is 98.5% after extraction rectifying separation, the material flow mainly containing o-methyl ethylbenzene and the solvent composition is discharged from the bottom of the extraction rectifying tower, the material flow mainly containing o-methyl ethylbenzene and the solvent composition is introduced into the solvent composition recovery tower, the tower plate number is 20, the reflux ratio is 1, the top temperature is 164.6 ℃, the kettle temperature is 202 ℃, the material flow containing 97.55% o-methyl ethylbenzene is discharged from the solvent composition recovery tower, and the solvent composition is recycled after being discharged from the bottom of the solvent composition recovery tower.
In comparative example 1, the extraction solvent is N-methyl-2-pyrrolidone and sodium sulfate, and the yield of mesitylene is 98.1% and the purity is 98.5% by extractive distillation. The temperature of the extraction rectifying tower of the composite solvent used in the invention is reduced, the energy consumption is reduced, and the purity of mesitylene is improved from 98.5% to 99.49%.
The foregoing is merely a preferred embodiment of the present invention and it should be noted that modifications and adaptations to those skilled in the art may be made without departing from the principles of the present invention, which are intended to be comprehended within the scope of the present invention.
Claims (10)
1. A method for separating high purity mesitylene from reformed carbon nine by using a composite solvent, comprising the following steps:
a) Removing light components and heavy components from the reformed carbon nine raw materials to obtain a material flow 1 with the total mass fraction of mesitylene and o-methyl ethylbenzene being more than or equal to 98%; the weight percentage of mesitylene in the reformed carbon nine raw material is more than or equal to 70%;
B) The material flow 1 enters an extraction rectifying tower from the middle lower part, the composite solvent material flow 2 enters an extraction rectifying tower I from the middle upper part, the mesitylene is subjected to extraction rectification, a mixed material flow 3 of o-methyl ethylbenzene and a trace amount of composite solvent is obtained at the tower top, and a mixed material flow 4 of mesitylene and the composite solvent is obtained at the tower bottom;
The compound solvent is a mixture of 1,3, 5-trichlorobenzene and 2, 6-xylenol, and the mass ratio of the 1,3, 5-trichlorobenzene to the 2, 6-xylenol is 80:20, 85:15 or 90:10;
c) The material flow 4 enters a solvent resolving tower from the middle lower part, a mesitylene material flow 5 is obtained at the top of the tower, and a resolved composite solvent material flow 6 is obtained at the bottom of the tower.
2. The method according to claim 1, wherein the theoretical plate number of the extractive distillation column is 60 to 200.
3. The method according to claim 2, wherein the feed temperature of the complex solvent stream 2 is 70-100 ℃.
4. The method according to claim 3, wherein the temperature of the tower bottom of the extraction rectifying tower is 140-180 ℃, the temperature of the tower top is 90-170 ℃, and the operation pressure is 10-90 KPa.
5. The method according to claim 4, wherein the reflux ratio of the extractive distillation column is 1.4 to 5.
6. The method according to claim 5, wherein the mass ratio of the composite solvent stream 2 to the stream 1 is (2-12): 1.
7. The method according to claim 1, wherein the theoretical plate number of the solvent-resolving tower is 30 to 80.
8. The method according to claim 7, wherein the solvent-resolving tower has a tower bottom temperature of 160-210 ℃, a tower top temperature of 80-160 ℃ and an operating pressure of 5-105 kpa.
9. The method according to claim 8, wherein the reflux ratio of the solvent-resolving tower is 1 to 3.5.
10. The method according to any one of claims 1 to 9, wherein the complex solvent stream 6 is mixed with the complementary complex solvent stream 2 for recycling after being cooled.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5972172A (en) * | 1996-12-23 | 1999-10-26 | Berg; Lloyd | Separation of 1,2,4-trimethylbenzene from 1,2,3-trimethylbenzene by extractive distillation |
| CN112250536A (en) * | 2020-11-04 | 2021-01-22 | 成都宏鼎石化有限公司 | Method and device for separating carbon nonaarene mixture |
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| NL64177C (en) * | 1943-02-08 | |||
| JPS643137A (en) * | 1987-06-25 | 1989-01-06 | Mitsui Toatsu Chem Inc | Purification of 2,4-xylenol |
| CN112194553B (en) * | 2020-11-04 | 2023-04-28 | 成都宏鼎石化有限公司 | Method and device for separating mixture of carbon nine aromatic hydrocarbon |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5972172A (en) * | 1996-12-23 | 1999-10-26 | Berg; Lloyd | Separation of 1,2,4-trimethylbenzene from 1,2,3-trimethylbenzene by extractive distillation |
| CN112250536A (en) * | 2020-11-04 | 2021-01-22 | 成都宏鼎石化有限公司 | Method and device for separating carbon nonaarene mixture |
Non-Patent Citations (1)
| Title |
|---|
| Separation of the C9 Alkylbenzenes by Induced Extractive CrystaIlization;F. P. McCandless et al.;Ind. Eng. Chem. Prod. Res. Dev.;19801201;第19卷;612-616 * |
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