CN115557825A - Method for separating high-purity mesitylene from reformed carbon nine by using composite solvent - Google Patents
Method for separating high-purity mesitylene from reformed carbon nine by using composite solvent Download PDFInfo
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- CN115557825A CN115557825A CN202211308916.4A CN202211308916A CN115557825A CN 115557825 A CN115557825 A CN 115557825A CN 202211308916 A CN202211308916 A CN 202211308916A CN 115557825 A CN115557825 A CN 115557825A
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- 239000002904 solvent Substances 0.000 title claims abstract description 140
- AUHZEENZYGFFBQ-UHFFFAOYSA-N mesitylene Substances CC1=CC(C)=CC(C)=C1 AUHZEENZYGFFBQ-UHFFFAOYSA-N 0.000 title claims abstract description 88
- 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 88
- 239000002131 composite material Substances 0.000 title claims abstract description 74
- 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 85
- 238000000605 extraction Methods 0.000 claims abstract description 29
- HYFLWBNQFMXCPA-UHFFFAOYSA-N 1-ethyl-2-methylbenzene Chemical compound CCC1=CC=CC=C1C HYFLWBNQFMXCPA-UHFFFAOYSA-N 0.000 claims description 30
- 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 23
- 238000000895 extractive distillation Methods 0.000 claims description 19
- XKEFYDZQGKAQCN-UHFFFAOYSA-N 1,3,5-trichlorobenzene Chemical compound ClC1=CC(Cl)=CC(Cl)=C1 XKEFYDZQGKAQCN-UHFFFAOYSA-N 0.000 claims description 15
- 238000010992 reflux Methods 0.000 claims description 15
- 238000003795 desorption Methods 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 11
- 238000004064 recycling Methods 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 230000000694 effects Effects 0.000 abstract description 4
- 150000001875 compounds Chemical class 0.000 abstract description 3
- GWHJZXXIDMPWGX-UHFFFAOYSA-N 1,2,4-trimethylbenzene Chemical compound CC1=CC=C(C)C(C)=C1 GWHJZXXIDMPWGX-UHFFFAOYSA-N 0.000 description 10
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 7
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 6
- 238000009835 boiling Methods 0.000 description 4
- 239000011259 mixed solution Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 239000007788 liquid Substances 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
- 238000005034 decoration Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- 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
- 238000005194 fractionation 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
- 239000003208 petroleum Substances 0.000 description 1
- 238000000066 reactive distillation Methods 0.000 description 1
- 239000000243 solution Substances 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
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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
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- 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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- 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 using 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 easily obtained, and the cost of the solvent is greatly reduced. (2) The compound solvent adopted by the invention has good extraction effect and selectivity on mesitylene, reduces the solvent ratio, and greatly reduces the operation 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 the mesitylene in the material to be separated is higher, particularly the content is more than or equal to 70 percent (mass percent), the process is particularly suitable for being adopted, and the energy consumption is saved.
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. Hemimellitene, pseudocumene, mesitylene and the like are separated from reformed C9 aromatic hydrocarbon, and the method has very important practical significance for developing and utilizing reformed C9 aromatic hydrocarbon resources, meeting development strategies that petrochemical products need to extend to the middle and lower reaches and improving economic benefits. However, it is very difficult to obtain high-purity mesitylene by a conventional fractionation method because the content of mesitylene in the reformed C9 aromatic hydrocarbon is not so high, and is generally 6 to 16% by weight, and the boiling points of the respective components in the C9 aromatic hydrocarbon are very close to each other, and particularly, the boiling points of o-methylethylbenzene (165.2 ℃ C.) and mesitylene (164.7 ℃ C.) are different by only 0.5 ℃ C.and the relative volatility is 1.009.
The current methods for separating mesitylene from reformed C9 include: separating by a reactive distillation mode, firstly using chloro-tert-butane as an alkylating agent and metal chloride as a catalyst to convert o-, m-, p-methyl-ethyl benzene 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 separation process combining rectification and extraction interleaving of C9 aromatic hydrocarbons, in which the separation steps are as follows: c9 aromatic hydrocarbon enters a rectifying tower, the temperature at the top of the tower is controlled to be less than or equal to 162.5 ℃, the distillate at the top of the tower is light C9, and the boiling range of the tower kettle is larger than 162.5 ℃ heavy C9; the heavy C9 enters an extraction tower, over 89 percent of p-methyl ethyl benzene can be obtained at the top of the extraction tower, and the tower kettle is mixed liquid; treating the mixed liquid in the tower kettle in a regeneration tower; the distillate at the top of the regeneration tower is a mixed solution of mesitylene, o-methyl-ethylbenzene and pseudocumene, the mixed solution enters a second rectification tower, and the extractant at the bottom of the tower is recycled; the distillate at the top of the second rectifying tower is a mixed solution rich in mesitylene, o-methyl-ethylbenzene and trace amount of pseudocumene, and the mixed solution rich in pseudocumene with the concentration of more than 83 percent is at the bottom of the second rectifying tower; the distillate at the top of the second rectifying tower enters a third rectifying tower, and the distillate at the top of the second rectifying tower can obtain more than 98.5 percent of mesitylene after extraction; the mixed liquid at the bottom of the tower is treated in a regeneration tower, more than 88 percent of o-methyl-ethyl benzene is distilled from the top of the regeneration tower, and the solvent at the bottom of the tower is recycled.
The prior production process of high-purity mesitylene has the following problems: 1. the reformed carbon nine contains 0.5 to 5 percent of non-aromatic components, a small amount of light non-aromatic components can not be removed by common rectification and extractive rectification, the purity of the mesitylene is seriously influenced, and the purity can not reach more than 99 percent; 2. in the process for producing mesitylene by an isomerization method, the final mesitylene has low yield and purity, and the downstream use is influenced; 3. the enrichment of the sym-trialkyl method has the advantages of the total yield and purity of the mesitylene, but the catalyst used in the process is toxic and easily pollutes the environment; 4. the extraction rectification process has poor extraction effect of a single solvent, so that the yield of the mesitylene is low; the energy consumption of the extractant in the solvent recovery process is too high.
Disclosure of Invention
The invention aims to provide a method for separating high-purity mesitylene from reformed carbon nine by using a composite solvent, the composite solvent has good selectivity on the mesitylene, the relative volatility between the mesitylene and o-methyl-ethyl benzene is increased, the circulation amount of the solvent is reduced, the energy consumption and fixed investment of a device are reduced, the yield of the mesitylene reaches over 96 percent, and the purity of the mesitylene reaches 99 percent.
The invention provides a method for separating high-purity mesitylene from reformed carbon nine by using a composite solvent, which comprises the following steps of:
a) Removing light and heavy components from a reformed carbon nine raw material 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 and rectification tower from the middle lower part, the composite solvent material flow 2 enters an extraction and rectification tower I from the middle upper part, the mesitylene is extracted and rectified, a mixed material flow 3 of the o-methyl-ethyl benzene and the trace composite solvent is obtained at the top of the tower, and a mixed material flow 4 of the mesitylene and the composite solvent is obtained at the bottom of the tower;
the composite 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) And the material flow 4 enters a solvent desorption tower from the middle lower part, a mesitylene material flow 5 is obtained at the top of the tower, and a desorbed composite solvent material flow 6 is obtained at the bottom of the tower.
Preferably, the number of theoretical plates of the extractive distillation column is 60 to 200.
Preferably, the feeding temperature of the composite solvent stream 2 is 70 to 100 ℃.
Preferably, the temperature of the bottom of the extraction and rectification tower is 140-180 ℃, the temperature of the top of the extraction and rectification tower is 90-170 ℃, and the operating pressure is 10-90 KPa.
Preferably, the reflux ratio of the extractive distillation column is 1.4 to 5.
Preferably, the mass ratio of the composite solvent material flow 2 to the material flow 1 is (2-12): 1.
preferably, the number of theoretical plates of the solvent stripping column is 30 to 80.
Preferably, the temperature of the bottom of the solvent analysis tower is 160-210 ℃, the temperature of the top of the solvent analysis tower is 80-160 ℃, and the operating pressure is 5-105 KPa.
Preferably, the reflux ratio of the solvent desorption column is 1 to 3.5.
Preferably, the composite solvent stream 6 is mixed with the supplemented composite solvent stream 2 for recycling after being cooled.
The invention provides a method for separating high-purity mesitylene from reformed carbon nine by using a composite solvent, which comprises the following steps: a) Removing light and heavy components from a reformed carbon nine raw material 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 and rectification tower from the middle lower part, the composite solvent material flow 2 enters an extraction and rectification tower I from the middle upper part, the mesitylene is extracted and rectified, a mixed material flow 3 of the o-methyl-ethyl benzene and the trace composite solvent is obtained at the top of the tower, and a mixed material flow 4 of the mesitylene and the composite solvent is obtained at the bottom of the tower; the composite 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) And the material flow 4 enters a solvent desorption tower from the middle lower part, a mesitylene material flow 5 is obtained at the top of the tower, and a desorbed 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 easily available, and the solvent cost is greatly reduced.
(2) The compound solvent adopted by the invention has good extraction effect and selectivity on mesitylene, reduces the solvent ratio, and greatly reduces the operation cost and the fixed investment; meanwhile, the yield of the mesitylene reaches over 96 percent, and the purity of the mesitylene reaches over 99 percent (mass percent).
(3) When the concentration of the mesitylene in the material to be separated is higher, and particularly, the content is more than or equal to 70 percent (mass percentage), the process is particularly suitable for being adopted, and the energy consumption is saved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the prior art descriptions will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a process flow diagram of the present invention;
wherein, I is an extraction and rectification tower, II is a solvent analysis tower, and III is a solvent cooler; 1 to 6 represent streams 1 to 6, respectively.
Detailed Description
The invention provides a method for separating high-purity mesitylene from reformed carbon nine by using a composite solvent, which comprises the following steps of:
a) Removing light and heavy components from a reformed carbon nine raw material 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 and rectification tower from the middle lower part, the composite solvent material flow 2 enters an extraction and rectification tower I from the middle upper part, the mesitylene is extracted and rectified, a mixed material flow 3 of the o-methyl-ethyl benzene and the trace composite solvent is obtained at the top of the tower, and a mixed material flow 4 of the mesitylene and the composite solvent is obtained at the bottom of the tower;
the composite 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) And the material flow 4 enters a solvent desorption tower from the middle lower part, a mesitylene material flow 5 is obtained at the top of the tower, and a desorbed 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 in the present invention, and a reformed carbon nine raw material commonly used by those skilled in the art may be used. In the present invention, the methods for removing light and heavy components are all methods commonly used by those skilled in the art, and the present invention is not described herein again.
In the present invention, the composite solvent is preferably 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 preferably (80-90): (20 to 10), more preferably (82 to 88): (18 to 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, a range value having any of the above values as an upper limit or a lower limit is preferred.
In the present invention, the feeding temperature of the composite 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 with any of the above values as the upper or lower limit. The mass ratio of the composite solvent material flow 2 to the material flow 1 is preferably (2-12): 1, more preferably (5 to 10): 1, as 2:1,3:1,4:1,5:1,6:1,7:1,8:1,9:1,10: 1,11: 1,12: 1, a range value having any of the above values as an upper limit or a lower limit is preferable.
In the present invention, the number of theoretical plates 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 within a range 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 ℃ and 180 ℃, and preferably the range value taking any value as the upper limit or the lower limit; the overhead temperature is preferably 90 to 170 ℃, more preferably 100 to 150 ℃, such as 90 ℃,95 ℃,100 ℃,105 ℃,110 ℃,115 ℃,120 ℃,125 ℃,130 ℃,135 ℃,140 ℃,145 ℃,150 ℃,155 ℃,160 ℃,165 ℃ and 170 ℃, and is preferably a range value taking any value as an upper limit or a lower limit; the reflux ratio of the extractive distillation column is preferably 1.4 to 5, more preferably 2 to 4, such as 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, preferably a range value with 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, and is preferably a range value having any of the above values as an upper limit or a lower limit.
In the present invention, the number of theoretical plates of the solvent stripping 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 within a range having any of the above values as an upper or 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 ℃ and 210 ℃, and is preferably a range value taking any value as an upper limit or a lower limit; the overhead temperature is preferably 80 to 160 ℃, more preferably 100 to 150 ℃, such as 80 ℃,85 ℃,90 ℃,95 ℃,100 ℃,105 ℃,110 ℃,115 ℃,120 ℃,125 ℃,130 ℃,135 ℃,140 ℃,145 ℃,150 ℃,155 ℃,160 ℃, and preferably ranges with any value as an upper limit or a lower limit; 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 with any of the above values as upper or lower limits; the operating pressure is preferably 5 to 105KPa, more preferably 10 to 100KPa, such as 5KPa,10KPa, 5KPa,2 KPa,25KPa,30KPa,35KPa,40KPa,45KPa,50KPa,55KPa,60KPa,65KPa,70KPa,75KPa,80KPa,85KPa,90KPa,95KPa,100KPa,105KPa, and is preferably a range value in which any of the above values is an upper limit or a lower limit.
In the invention, preferably, the composite solvent material flow 6 obtained at the bottom of the tower is cooled by a cooler, and then mixed with the composite solvent material flow 2 to enter the middle upper part of the extractive distillation tower for recycling.
The invention provides a method for separating high-purity mesitylene from reformed carbon nine by using a composite solvent, which comprises the following steps of: a) Removing light and heavy components from a reformed carbon nine raw material 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 and rectification tower from the middle lower part, the composite solvent material flow 2 enters an extraction and rectification tower I from the middle upper part, the mesitylene is extracted and rectified, a mixed material flow 3 of the o-methyl-ethyl benzene and the trace composite solvent is obtained at the top of the tower, and a mixed material flow 4 of the mesitylene and the composite solvent is obtained at the bottom of the tower; the composite 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) And the material flow 4 enters a solvent desorption tower from the middle lower part, a mesitylene material flow 5 is obtained at the top of the tower, and a desorbed 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 easily available, and the solvent cost is greatly reduced.
(2) The compound solvent adopted by the invention has good extraction effect and selectivity on mesitylene, reduces the solvent ratio, and greatly reduces the operation cost and the fixed investment; meanwhile, the yield of the mesitylene reaches over 96 percent, and the purity of the mesitylene reaches over 99 percent (mass percent).
(3) When the concentration of the mesitylene in the material to be separated is higher, particularly the content is more than or equal to 70 percent (mass percent), the process is particularly suitable for being adopted, and the energy consumption is saved.
In order to further illustrate the present invention, the method for separating high purity mesitylene from reformed carbon nine using a complex solvent according to the present invention will be described in detail with reference to the following examples, which should not be construed as limiting the scope of the present invention.
Example 1
According to the process flow of figure 1, the adopted composite solvent is a mixture of 1,3, 5-trichlorobenzene and 2, 6-xylenol, and the mass percent ratio is as follows: 80%:20 percent.
(1) Firstly, removing light and heavy components from mesitylene and o-methyl-ethyl benzene to be separated in a common rectification mode, marking the total mass percent of the mesitylene and the o-methyl-ethyl benzene to be more than or equal to 98 percent as material flow 1, feeding the material flow into a tower I from the middle lower part, feeding a composite solvent 2 into the tower I from the middle upper part, and carrying out extractive rectification. A mixed material flow 3 of o-methyl ethyl benzene and a small amount of composite solvent is obtained at the tower top, and a mixed material flow 4 of mesitylene and composite solvent is obtained at the tower bottom;
(2) A mixed material flow 4 of the composite solvent and the mesitylene enters a solvent desorption tower II from the middle part, the mesitylene and a mixed material flow 5 containing a small amount of solvent are obtained at the top of the tower, and a desorbed solvent material flow 6 is obtained at the bottom of the tower;
(3) And the desorbed solvent material flow 6 is cooled by the solvent cooler III, mixed with the composite solvent material flow 2 and recycled to enter the middle upper part of the extraction and rectification tower I.
In the above-described flow, the operating conditions of the respective operating units are as follows:
(1) The operating conditions of the extractive distillation column I are as follows: the theoretical plate number is 150, the feeding temperature of the composite solvent material flow 2 is 75 ℃, the temperature of a tower kettle is 178.4 ℃, the temperature of a tower top is 102.9 ℃, the reflux ratio is 2.7, the operation 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 the solvent stripper II: the number of theoretical plates is 50, the temperature of a tower kettle is 183.2 ℃, the temperature of a tower top is 137.6 ℃, the reflux ratio is 3.2, and the operation pressure is 74KPa;
the composite solvent is combined with the flow of a figure 1, the yield of the mesitylene is 96.6 percent, and the purity reaches 99.49 percent (mass percent).
TABLE 1 raw material composition and product quality
Example 2
According to the process flow of figure 1, the adopted composite solvent is a mixture of 1,3, 5-trichlorobenzene and 2, 6-xylenol, and the mass percent ratio is as follows: 85%:15 percent.
(1) Firstly, removing light and heavy components from mesitylene and o-methylethylbenzene to be separated by a common rectification mode, then enabling the total mass percent of mesitylene and o-methylethylbenzene in a material flow 1 to be more than or equal to 98%, enabling the mesitylene and o-methylethylbenzene to enter a tower I from a 90 th theoretical plate (1-180 pieces from top to bottom), enabling a composite solvent 2 to enter the tower I from a 5 th theoretical plate, carrying out extractive rectification, obtaining a mixed material flow 3 of the o-methylethylbenzene and a small amount of solvent at the tower top, and obtaining a mixed material flow 4 of the mesitylene and the composite solvent at the tower bottom;
(2) A mixed material flow 4 of the composite solvent and the mesitylene enters a solvent desorption tower II from the middle part, the mesitylene and a mixed material flow 5 containing a small amount of solvent are obtained at the top of the tower, and a desorbed solvent material flow 6 is obtained at the bottom of the tower;
(3) And the desorbed solvent material flow 6 is cooled by a solvent cooler VI, then is mixed with the composite solvent material flow 2, and is recycled and enters the middle upper part of the extraction rectifying tower I.
In the above-described flow, the operating conditions of the respective operation units are as follows:
(1) The operating conditions of the extractive distillation column I are as follows: the theoretical plate number is 180, the feeding temperature of the solvent material flow 2 is 95 ℃, the temperature of a tower bottom is 167.2 ℃, the temperature of a tower top is 100.9 ℃, the reflux ratio is 2.8, the operation pressure is 78KPa, and the mass ratio of the solvent 2 to the material flow 1 to be separated is 6;
(2) Operating conditions of the solvent stripper II: the theoretical plate number is 80, the temperature of the tower bottom is 197.2 ℃, the temperature of the tower top is 155.6 ℃, the reflux ratio is 3.1, and the operation pressure is 80KPa;
the composite solvent is combined with the flow of a figure 1, the yield of the mesitylene is 97.2 percent, and the purity reaches 99.36 percent (mass percentage).
TABLE 2 raw material composition and product quality
Example 3
According to the process flow shown in figure 1, the adopted composite solvent is a mixture of 1,3, 5-trichlorobenzene and 2, 6-xylenol, and the mass percent ratio is as follows: 90%:10 percent.
(1) Firstly, after light component removal and heavy component removal are carried out on mesitylene and o-methylethylbenzene to be separated in a common rectification mode, the total mass percent of the mesitylene and the o-methylethylbenzene is more than or equal to 98 percent and is marked as material flow 1, the material flow enters a tower I from a 60 th theoretical plate (1-140 pieces from top to bottom), and a composite solvent 2 enters the tower I from a 7 th theoretical plate for extractive rectification. A mixed material flow 3 of o-methyl ethyl benzene and a small amount of composite solvent is obtained at the tower top, and a mixed material flow 4 of mesitylene and composite solvent is obtained at the tower bottom;
(2) A mixed material flow 4 of the composite solvent and the mesitylene enters a solvent desorption tower II from the middle part, the mesitylene and a mixed material flow 5 containing a small amount of solvent are obtained at the top of the tower, and a desorbed solvent material flow 6 is obtained at the bottom of the tower;
(3) And 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 rectification tower I.
In the above-described flow, the operating conditions of the respective operating units are as follows:
(1) The operating conditions of the extractive distillation column I are as follows: the number of theoretical plates is 140, the feeding temperature of the solvent material flow 2 is 100 ℃, the temperature of a tower kettle is 156.6 ℃, the temperature of a tower top is 87.8 ℃, the reflux ratio is 3.1, the operation pressure is 50KPa, and the mass ratio of the solvent 2 to the material flow 1 to be separated is 8;
(2) Operating conditions of the solvent stripper II: the theoretical plate number is 70, the temperature of the tower kettle is 160 ℃, the temperature of the tower top is 86.5 ℃, the reflux ratio is 2.8, and the operation pressure is 50KPa;
the composite solvent combines the flow of the figure 1, the yield of the mesitylene is 97.5 percent, and the purity reaches 99.32 percent (mass percentage).
TABLE 3 raw material composition and product quality
Comparative example 1
This comparative example 1 is patent CN102924212A, example 10, using extractive distillation, and the solvent is a complex solvent comprising N-methyl-2-pyrrolidone and alkali metal sulfate.
The raw material is a carbon nonaromatic hydrocarbon mixture without light components, wherein the carbon nonaromatic hydrocarbon mixture contains 35.10 weight percent of mesitylene, and the extractive distillation solvent adopts a solvent composition which comprises 93 parts of N-methyl-2-pyrrolidone and 7 parts of sodium sulfate in parts by weight.
The mixture of carbon nonaromatic hydrocarbon from which light components are removed enters the middle-lower part of a metatriphenylene tower, enriched fraction containing mesitylene and partial methyl ethylbenzene is discharged from the top of the tower, material flow mainly containing mesitylene is led out from the bottom of the tower, the number of tower plates of the metatriphenylene tower is 85, the reflux ratio is 15, the top temperature is 165 ℃, and the temperature of the bottom is 188.3 ℃. The method comprises the steps of enabling an enriched fraction containing mesitylene and partial methyl ethylbenzene flowing out of the top of a metatriphenylene tower to enter the middle lower portion of an extractive distillation tower, enabling a circulating solvent composition to enter the extractive distillation tower from the upper portion, enabling the number of plates of the extractive distillation tower to be 95, the reflux ratio to be 4, the top temperature to be 164 ℃, the kettle temperature to be 204.1 ℃, enabling the purity of mesitylene distilled out of the top to be 98.5% through extractive distillation separation, enabling a material flow mainly containing o-methyl ethylbenzene and a solvent composition to be discharged from the bottom of the extractive distillation tower, enabling the material flow mainly containing o-methyl ethylbenzene and the solvent composition to be introduced into a solvent composition recovery tower, enabling the number of the plates to be 20, the reflux ratio to be 1, the top temperature to be 164.6 ℃, enabling the material flow mainly containing 97.55% of o-methyl ethylbenzene to be discharged from the top of the solvent composition recovery tower, and enabling the solvent composition to be recycled after being discharged from the bottom of the solvent composition recovery tower.
In comparative example 1, N-methyl-2-pyrrolidone and sodium sulfate are used as extraction solvent, and mesitylene is obtained by extraction and rectification, wherein the yield is 98.1% and the purity is 98.5%. The temperature of the extraction and rectification tower of the composite solvent used in the invention is reduced, the energy consumption is reduced, and the purity of the mesitylene is improved from 98.5 percent to 99.49 percent.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (10)
1. A method for separating high-purity mesitylene from reformed carbon nine by using a composite solvent comprises the following steps:
a) Removing light and heavy components from a reformed carbon nine raw material 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 and rectification tower from the middle lower part, the composite solvent material flow 2 enters an extraction and rectification tower I from the middle upper part, the mesitylene is subjected to extraction and rectification, a mixed material flow 3 of the o-methyl-ethyl benzene and the trace composite solvent is obtained at the top of the tower, and a mixed material flow 4 of the mesitylene and the composite solvent is obtained at the bottom of the tower;
the composite 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) And the material flow 4 enters a solvent desorption tower from the middle lower part, a mesitylene material flow 5 is obtained at the top of the tower, and a desorbed composite solvent material flow 6 is obtained at the bottom of the tower.
2. The method of claim 1, wherein the number of theoretical plates of the extractive distillation column is 60 to 200.
3. The method according to claim 2, characterized in that the feeding temperature of the composite solvent stream 2 is between 70 and 100 ℃.
4. The method as claimed in claim 3, wherein the temperature of the bottom of the extractive distillation column is 140-180 ℃, the temperature of the top of the extractive distillation column is 90-170 ℃, and the operating pressure is 10-90 KPa.
5. The method as claimed in 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 number of theoretical plates of the solvent stripper is 30 to 80.
8. The method according to claim 7, wherein the temperature of the bottom of the solvent desorption tower is 160-210 ℃, the temperature of the top of the solvent desorption tower is 80-160 ℃, and the operating pressure is 5-105 KPa.
9. The method as claimed in claim 8, wherein the reflux ratio of the solvent stripper is 1 to 3.5.
10. The method according to any one of claims 1 to 9, wherein the composite solvent stream 6 is cooled and mixed with the supplemented composite solvent stream 2 for recycling.
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| US2360861A (en) * | 1943-02-08 | 1944-10-24 | Shell Dev | Solvent extraction process |
| JPS643137A (en) * | 1987-06-25 | 1989-01-06 | Mitsui Toatsu Chem Inc | Purification of 2,4-xylenol |
| US5972172A (en) * | 1996-12-23 | 1999-10-26 | Berg; Lloyd | Separation of 1,2,4-trimethylbenzene from 1,2,3-trimethylbenzene by extractive distillation |
| CN112194553A (en) * | 2020-11-04 | 2021-01-08 | 成都宏鼎石化有限公司 | Method and device for separating carbon nonaarene mixture |
| 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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| US2360861A (en) * | 1943-02-08 | 1944-10-24 | Shell Dev | Solvent extraction process |
| JPS643137A (en) * | 1987-06-25 | 1989-01-06 | Mitsui Toatsu Chem Inc | Purification of 2,4-xylenol |
| US5972172A (en) * | 1996-12-23 | 1999-10-26 | Berg; Lloyd | Separation of 1,2,4-trimethylbenzene from 1,2,3-trimethylbenzene by extractive distillation |
| CN112194553A (en) * | 2020-11-04 | 2021-01-08 | 成都宏鼎石化有限公司 | Method and device for separating carbon nonaarene mixture |
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